EP0139092A1 - Entaschungsapparat für Wirbelbettvergaser - Google Patents

Entaschungsapparat für Wirbelbettvergaser Download PDF

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Publication number
EP0139092A1
EP0139092A1 EP84107712A EP84107712A EP0139092A1 EP 0139092 A1 EP0139092 A1 EP 0139092A1 EP 84107712 A EP84107712 A EP 84107712A EP 84107712 A EP84107712 A EP 84107712A EP 0139092 A1 EP0139092 A1 EP 0139092A1
Authority
EP
European Patent Office
Prior art keywords
ash
vessel
floor
gas
particles
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Withdrawn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
EP84107712A
Other languages
English (en)
French (fr)
Inventor
John Peter Carrera
Kanwal Mahajan
Lawrence Karl Rath
Yang Wen-Ching
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.)
KRW Energy Systems Inc
Original Assignee
KRW Energy Systems Inc
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 KRW Energy Systems Inc filed Critical KRW Energy Systems Inc
Publication of EP0139092A1 publication Critical patent/EP0139092A1/de
Withdrawn legal-status Critical Current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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • C10J3/523—Ash-removing devices for 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
    • C10J3/482—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
    • C10J3/50—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
    • C10J3/52—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
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/74—Construction of shells or jackets
    • 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
    • C10J2300/09—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
    • 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
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • This invention relates to gasification of carbonaceous materials and more particularly to a method and apparatus for separation, cooling and removal of ash from fluidized bed gasifiers.
  • a combustible product gas is produced as well as solid waste products such as agglomerated ash.
  • coal particles are pneumatically transported by a gas into the hot gasifier.
  • Process mediums such as steam, coal in particle form, and a gaseous source of oxygen, such as air or pure oxygen, are injected, as well as, perhaps, a clean recycled product gas.
  • This process results in fluidization of the coal particles in a bed above the nozzle.
  • the injection of coal and oxygen into the hot gasifier results in combustion of a portion of the coal, and the,heat thereby released maintains the temperature in the gasifier.
  • the non-combusted coal particles are heated, rapid evaporation, or devolatilization, of volatiles in the coal occurs.
  • the average temperature within the vessel typically runs between 870°C and 1100°C or higher and this high temperature ensures that the products of devolatilization, such as tars and oils, etc., are broken down, or cracked, and gasified to form methane, carbon monoxide and hydrogen.
  • devolatilization is completed and particles of coal become pieces predominantly of ungasified carbon, or char. As this char circulates throughout the fluidized bed, the carbon in the char is gradually consumed by combustion and gasification, leaving ash-rich particles that have a high ash content.
  • the ash-rich particles contain mineral compounds and eutectics that melt at temperatures of between 540°C to 1100°C and typically consist of compounds of any or all of S, Fe, Na, Al, K and Si, which compounds are typically denser than carbon compounds. These liquid compounds within the particles extrude through pores to the surfaces where they cause the particles to stick to each other, or agglomerate. In this way, ash agglomerates are formed that are larger and denser than the particles of char in the bed. As their density and size increases, the fluidized bed is unable to support them. Gradually, the density of the ash agglomerates becomes high enough that they can no longer be supported in the fluidized bed, and the ash agglomerates defluidize. It is then necessary to remove these ash agglomerates from the vessel.
  • the ash withdrawal means of the prior art has taken several forms.
  • the first of these is one in which the ash settles at the bottom of the vessel and gradually. builds up to some physical level above the bottom.
  • a fixed outlet acts as an overflow discharge to withdraw the ash.
  • This is a satisfactory solution where the gasifier in use uses entrained limestone or some other type of material which is intended to remain within the bed as a relatively fixed inventory. It is unsatisfactory, however, where no residual ash is desired.
  • a second form of ash withdrawal means consists of a device which mechanically sifts the ash to separate the ash particles by size. This means is unsatisfactory because it does not take advantage of the difference in density between particles of char and particles of agglomerated ash. This may result in premature removal of char (which has residual carbon value) and a corresponding reduction in carbon conversion efficiency.
  • a third form of ash withdrawal means consists of a floor disposed at a very slight angle with respect to the horizontal, leading downwardly towards an ash removal plenum.
  • a fluidizing gas is discharged through nozzles in the floor to provide a fluidizing means for particles of agglomerated ash.
  • a disadvantage of this means is that ash removal may take place very slowly and as a result might not be effective for a large scale gasifier.
  • a further disadvantage is that large particles of ash which are too large or too dense to be fluidized by the floor nozzles may not be discharged, and could build up in the vessel. This can distort the gas distribution from the floor nozzles, further hindering solids removal.
  • Another form of ash removal means consists of an apparatus for removing ash agglomerates preferentially through a venturi throat using a high velocity jet of incoming gas made up of the process mediums, against which only the agglomerates having sufficient downward momentum may fall.
  • a high velocity jet of incoming gas made up of the process mediums, against which only the agglomerates having sufficient downward momentum may fall.
  • any withdrawal of ash through the venturi throat may cause a momentary blockage in the throat, and could result in a perturbation in the fluidized bed which is supported by the gas.
  • a fluidized bed gasifier for the gasification of carbonaceous material, comprising a vertically disposed elongated vessel defining an internal ash annulus region disposed within a lower section of said vessel said vessel having a sloping floor, disposed within said vessel in said ash annulus region, having a slope angle of between 80° and 45° upwards from a horizontal reference, said floor having orifices, extending therethrough, means for the injection of process mediums into said vessel, said injection means extending upwardly through said floor and into said ash annulus region, and means for discharging ash from said vessel, said discharge means penetrating said floor at the lower edge thereof, characterized in that gas injection means are provided in the area of said ash annulus region for the injection of a gas downwardly into said ash annulus region and said floor has a slope angle of between 80° and 45 0 upwards from a horizontal reference.
  • a fluidized bed gasifier 10 comprising a generally elongated vessel 12, the bottom of which is penetrated by a nozzle 14, which extends upwardly into the vessel 12. Penetrating the top of the vessel 12 is a product gas outlet 16.
  • the vessel 12 has three major horizontal regions: 1) the bed region 18 in the uppermost portion of the vessel 12 and extending downwardly to approximately the top of the combustion flame 15 formed at the top of the nozzle 14; 2) the combustor region 19 below the bed region 18 and above the top of the nozzle 14; and 3) the annulus region 22 extending from the top of the nozzle 14 downward.
  • the char particles flow pattern 20 and the agglomerated ash flow pattern 21 There is also shown the char particles flow pattern 20 and the agglomerated ash flow pattern 21.
  • Concentric to the nozzle 14 from a point below the top of the nozzle 14 and downwardly may be an inner booster 24.
  • An outer booster 26 may be embedded or attached to the vessel 12 at a position which is approximately at the same elevation as the top of the inner booster 24. Only one of the boosters 24, 26 is necessary, but preferably both are used.
  • the gas injected by the boosters 24, 26 may be any gas, but is preferably steam or clean recycled product gas.
  • a steeply- slanted floor 28, preferably symmetric on either side of the nozzle 14, is situated at the bottom of the annulus 22, the center of which floor 28 extends upwardly towards the top of the nozzle 14.
  • a gas, typically clean recycled product gas, is injected through inlet 30 into a floor gas plenum 31 beneath the floor 28. Beneath the floor gas plenum 31 is an ash plenum 32.
  • FIG. 3 there can be seen a more detailed view of the annulus 22 showing the nozzle 14 surrounded by the inner booster 24 and showing additional detail of the floor 28.
  • the floor 28 may be a single plate, or may be comprised of multiple plates such as 34, 36, 38 and 40. Also shown are holes 42 through which a gas, typically clean recycled product gas, is injected into the annulus region 22. Penetrating the floor 28 is one or more ash discharge openings 44.
  • FIG. 5 there can be seen a more detailed view of the vessel 12 showing the annulus region 22 inside of which is the nozzle 14 which is surrounded by the inner booster 24.
  • the outer booster 26 Attached to, or embedded in, the vessel 12 is the outer booster 26 which may be comprised of a singular coiled tube 46.
  • Penetrating the tube 46 may be outer booster discharge holes 48 situated in a manner to provide discharge of a process medium into the vessel 12.
  • Penetrating the inner booster 24 may be a series of inner booster discharge holes 50 to inject a process medium into the vessel 12.
  • both boosters 24, 26 are disposed uniformly around the ash annulus in such a manner that large bubbles rising from the floor 28 of the vessel 12 will be effected by the gas injected by the boosters 24, 26 and thereby broken up.
  • the extended time spent in the annulus region 22 defluidizing also provides the ash with the opportunity to cool from the temperature of the fluidized bed.
  • the recycled gas, typically injected at a temperature between 38°C and 370°C, and the steam, typically injected at a temperature between 100°C and 480°C cool the ash significantly, from above 870°C when it leaves the bed, to a range of 38°C to 427°C when it is discharged.
  • the ash passes through the floor 28 through ash discharge openings 44 (see Figure 4) and into the ash discharge plenum 32 where it can be further disposed of, such as through large diameter piping and lockhoppers.
  • the floor 28 has grid gas discharge penetrations 42 through which a gas such as recycled product gas passes from the floor gas plenum 31 into the annulus region 22 of the vessel 12.
  • these grid gas discharge penetrations 42 will be designed and sized such that the pressure drop across the penetrations 42 is greater than 30% of the bed pressure drop. It has been determined that this pressure drop will prevent flow imbalances through the penetrations 42 at different locations. Such flow imbalances could result in loss of fluidizing action on the ash agglomerates and char in the annulus region 22.
  • the bed pressure drop will depend upon several variables such as the vessel operating pressure and the vessel height. It is further desirable that the total flow from these grid gas discharge penetrations 42 will be approximately one-half of the total gas fed to the annulus region 22 including the boosters 24, 26. This will help to insure that the distribution of gas within the annulus region 22 is uniform.
  • the floor 28 may typically have an angle of between 80° and 45°, and.pref - erably, approximately 70°, upwards from the horizontal. This angle helps to assure the removal of large agglomerated ash particles formed in the bed.
  • the angle of internal friction is that angle of a surface for which a particle of a particular material will roll regardless of its shape. For coal that angle is 60°; for ash agglomerates 45°; and for char fines 65°. Because the angle of 70° is larger than the angle of internal friction for most coal- derived solid materials, no large particles of agglomerated ash are expected to accumulate even with the loss of fluidizing gas. Obviously, it would be acceptable to use an angle of between 70° and 45° if no coal or char fines were expected to find their way into the annulus region.
  • the floor 28 is penetrated by the nozzle 14 and the inner booster 24 and at least one ash discharge opening 44.
  • the penetration for the nozzle 14 and the inner booster 24 will be in the center and there will be two ash discharge openings 44 on opposite sides of the vessel 12 from each other and tangent to the wall of the vessel 12 at the lowest point of the floor 28.
  • the recycled gas discharged through the floor 28, through the floor gas discharges 42 will be at angles which will direct the ash towards the ash discharge openings 44 and away from the wall of the vessel 12.
  • these floor gas discharges 42 will discharge floor gas generally towards the ash discharge opening 44 and specifically at an angle 8 which is between 30° to 45° from a line that passes through the centers of both ash discharge openings 44.
  • the inner booster 24 may consist of a capped pipe concentric to the nozzle 14 with a series of holes 50 which penetrate the inner booster 24. These holes 50 may be made such that gas discharged from them will be discharged generally downward, and in the preferred embodiment, at an angle approximately 60° downward from the horizontal.
  • the outer booster 26 may generally consist of a coiled hollow pipe 46 with outer booster discharge penetrations 48 made such that the discharge of a gas would be generally downward, and in the preferred embodiment, at an angle approximately 60° downward from the horizontal.
  • These penetrations 48 and holes 50 may typically be of a diameter between 1.6 mm and 12.7 mm, but preferably about 6.35 mm in diameter.
  • the inner and outer boosters 24, 26 provide several functions. First, the boosters 24, 26 provide cooling of the agglomerated ash which is defluidizing inside the annulus 22. Second, the boosters 24 and 26 provide additional fluidizing gas in the annulus 22, particularly in that space above the boosters 24, 26 and below the top of the nozzle 14. Third, the boosters provide a mechanism generating bubbles uniformly across the annulus region 22 to facilitate particle separation.

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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)
  • Gasification And Melting Of Waste (AREA)
EP84107712A 1983-07-29 1984-07-03 Entaschungsapparat für Wirbelbettvergaser Withdrawn EP0139092A1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US51833883A 1983-07-29 1983-07-29
US518338 1983-07-29

Publications (1)

Publication Number Publication Date
EP0139092A1 true EP0139092A1 (de) 1985-05-02

Family

ID=24063507

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84107712A Withdrawn EP0139092A1 (de) 1983-07-29 1984-07-03 Entaschungsapparat für Wirbelbettvergaser

Country Status (5)

Country Link
EP (1) EP0139092A1 (de)
JP (1) JPS6053594A (de)
KR (1) KR850001399A (de)
AU (1) AU2774184A (de)
ZA (1) ZA844086B (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6787123B2 (en) 2001-04-28 2004-09-07 China Petroleum & Chemical Corporation Rare earth zeolite Y and the preparation process thereof
EP1974060A4 (de) * 2005-12-26 2010-05-26 Posco Vorrichtung zur herstellung von schmelzflüssigem eisen
WO2022157619A1 (de) * 2021-01-19 2022-07-28 Radmat Ag Vorrichtung zum verwerten von prozessgas unter umsetzung von altstoffen und bildung von synthesegas

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1526108A1 (de) * 1965-11-01 1970-02-12 Tashimaro Miike Vorrichtung zur fortlaufenden Muellverbrennung
EP0031098A1 (de) * 1979-12-13 1981-07-01 Combustion Engineering, Inc. Aschebeseitigungssystem mit Tauchkratzförderer
EP0041094A1 (de) * 1980-06-03 1981-12-09 Westinghouse Electric Corporation Teilchenentfernung aus Wirbelbettsystemen
US4372228A (en) * 1980-12-04 1983-02-08 York-Shipley, Inc. Fluidized bed reactor utilizing a conical-shaped support and method of operating the reactor

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1526108A1 (de) * 1965-11-01 1970-02-12 Tashimaro Miike Vorrichtung zur fortlaufenden Muellverbrennung
EP0031098A1 (de) * 1979-12-13 1981-07-01 Combustion Engineering, Inc. Aschebeseitigungssystem mit Tauchkratzförderer
EP0041094A1 (de) * 1980-06-03 1981-12-09 Westinghouse Electric Corporation Teilchenentfernung aus Wirbelbettsystemen
US4372228A (en) * 1980-12-04 1983-02-08 York-Shipley, Inc. Fluidized bed reactor utilizing a conical-shaped support and method of operating the reactor

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6787123B2 (en) 2001-04-28 2004-09-07 China Petroleum & Chemical Corporation Rare earth zeolite Y and the preparation process thereof
US6991774B2 (en) 2001-04-28 2006-01-31 China Petroleum & Chemical Corporation Rare earth zeolite Y and the preparation process thereof
EP1974060A4 (de) * 2005-12-26 2010-05-26 Posco Vorrichtung zur herstellung von schmelzflüssigem eisen
US8119059B2 (en) 2005-12-26 2012-02-21 Posco Apparatus for manufacturing molten irons
WO2022157619A1 (de) * 2021-01-19 2022-07-28 Radmat Ag Vorrichtung zum verwerten von prozessgas unter umsetzung von altstoffen und bildung von synthesegas

Also Published As

Publication number Publication date
JPS6053594A (ja) 1985-03-27
KR850001399A (ko) 1985-03-18
AU2774184A (en) 1985-01-31
ZA844086B (en) 1985-01-30

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