US2906608A - Apparatus for dense-phase fluidisation - Google Patents

Apparatus for dense-phase fluidisation Download PDF

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US2906608A
US2906608A US634234A US63423457A US2906608A US 2906608 A US2906608 A US 2906608A US 634234 A US634234 A US 634234A US 63423457 A US63423457 A US 63423457A US 2906608 A US2906608 A US 2906608A
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grate
duct
chamber
gas
gasification
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US634234A
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Jequier Leon Jean Roland
Gerard Henri Aime Richar Putte
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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/245—Spouted-bed technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/44—Fluidisation grids
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/36—Fixed grates
    • 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
    • C10J3/72—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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00761—Discharging
    • 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
    • C10J2300/0969—Carbon dioxide
    • 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

Definitions

  • the gasification zone is in the gasification agents being introduced at that apex.
  • the device described above permits a very good dense-phase fluidization, that is to say a uniform distribution and a regular agitation of the fine particles during the course of gasification.
  • the gas isthus better divided by the fine particles, the reducing action of which is therefore better distributed in the flow of gas.
  • abetter reduction of the gasification agents is obtained and in consequence a gas of superior quality and a higher efficiency is formed.
  • the advantages of the conical zone for the evacuation of the ash are obtained.
  • Fig. 1 is a diagrammatic view in vertical cross-section of an embodiment of an apparatus for gasifying solid fuels, in accordance with the invention.
  • Fig. 2 is a partial cross-section on a larger scale of the annular grate which surrounds the central conical zone.
  • Fig. 3 is a plan view of this grate on a smaller scale.
  • Fig. 4 shows a vertical cross-section of a device for re-eycling dust.
  • the gas-producer shown in Fig. 1 comprises a gasification zone surrounded by a refractory wall 1.
  • the fine particles of solid fuel are brought into this zone, either from the exterior, or from heating stages which are not shown, by any suitable devices.
  • a portion of the gaseous gasification agents, which may or may not be pre-heated, is introduced through the pipe 2 into the central conical portion 3 of the grate.
  • This conical portion 3 has a fairly accentuated conicity (an apex angle comprised for example between 10 and 50) and is made of a full wall coupled to a venturi 4 which ensures a uniform speed of the gasification agents in the lowest section of the cone,
  • the convergent portion of the venturi serves to increase the speed of the gas at from falling, whereas on the upstream side of this con vergent portion, the speed of the gas is reduced so as not to hinder the descent of the. large particles which have passed; through the neck. of the venturi..
  • The. divergent portion of the venturi may be formed by the cone. 3 or maybe, coupled to this cone if the latter has, a conicity greater than that of the divergent portion'of the venturi at optimum. efficiency. It is desirable that the gasification agents. should have a.
  • the length of the conduit 2a betweenthe tube 2. and the venturi 4 should be sufiicient: to damp out any movement of this kind, or that this conduit shouldbe fitted with fins parallel to the axis and'fixed to the walls of, the said conduit, leaving between them aclear way having a diameter at least as great as that of the neck of. the venturi.
  • the remaining part of the gasification agents is introduced through the. piping system 5 underthe annular. peripheral grate-6. The latter is formed .by radial, orconcentric members provided with overlapping portions.
  • Figs. 2 and- 3 show the constitution of the grate 6 by metal rings 6a which, are concentrically mounted on radial supports 6b which are. attached. at their extremities to the wall of the chamber 7 and to that of the cone 3'. These rings form between. each other small passages. 60 of zigzag shape, which are permeable to the gases coming from the chamber 7 but not to the solid particles. These passages are maintained at their correct width by means of spacers 6d with which the rings. 6a are provided. Any other arrangement may be employed, for example that of radial elements with overlapping portions. The parts.
  • the gasification chamber 8 a. zone of dense. and uniform fluidization.
  • the reaction of the carbon of the fine particles. with the oxygen of the gasification agents is. extremely rapid and violent, converting all the oxygen to carbon dioxide with a very; considerable production of heat.
  • the carbon dioxide thus. formed, that introduced with the gasification agents, and the steam. of these agents are immediately brought: up to. the high temperature of the gasification. As these gases are also kept in intimate contact with the fine.
  • the dust, thus separated from the fiow of gas does not contain av greater proportion of ashv than the initial fine particles. It is thus possible to re-cycle them andthus to convert them to useful gas.
  • the best method. of. doing this. is to re-introduce them into the apparatus by means of a small quantity of the gasifying agents.
  • the re-introduction if preferably carried out below the venturi 4,, as shown in. Fig. 4.
  • the separation of the dust is effected in a cyclone separator 50 which could furthermore be re.- placed by another similar. apparatus of, any kind.
  • the gas to be free from dust enters through piping system 21 and'the clean gas passes out through the Piping 22.v
  • the dustcollected, at the base of the cyclone falls down, in a tube 23 provided with a gas-intake 2.4, which gas is, intended to maintain the dust in the column constantly in a slightly fluidized state in order to avoid any obstruction.
  • This gas may be an inert gas or gas manufactured in the apparatus and extracted by the compressor 25. after cooling.
  • a valve 26 of a suitable type, or a rotary distributor At the base of the descent tube 23 for the dust, is provided a valve 26 of a suitable type, or a rotary distributor.
  • the dust falls into a chamber 27 or into any suitable device which enables it to, be taken up again by a branch flow of gasifying agents arriving through the tube 28'.
  • the suspension of dust in this flow is. sent through the pipe 29 into the vertical tube 2a which brings the air to the venturi 4. of Fig. 1.
  • This intake tube 29 is. preferably arranged obliquely inside the vertical tube and discharges close to the wall of this latter so that the jet of dust is broken up against this wall and there is thus no agglomeration of dust to be feared.
  • the intake of the tube 29 is. efiected of course. above the intake of the. tube 2. of Fig, 1
  • the section .of the vertical tube 2a is so chosen that the speed at that point is sufficient to cause the fine particles introduced to rise towards the gasification zone, without however impeding the descent of the large particles of ash which have passed through the venturi.
  • reaction zone is at high temperature and the gasifying agents are immediately brought up to that temperature, the specific surface area of the fine particles present in this zone is considerable, and their agitation with respect to the flow of gas is very great, thereby assisting the reactions of reduction;
  • the uniform conical surface may be replaced by any other type of flared surface or by that of a pyramid.
  • the invention is adapted to applications other than the gasification of fuels.
  • Swiss Patent No. 292,859 describes a continuous method of manufacture of iron or steel by treatment and reduction of oxide, of hydrate or of metallic salt, the said substances being used in the form of powder and all or part of the various stages of the treatment and the reduction being effected by means of currents of reducing gas that maintain this powder in a state of dense-phase fluidization.
  • a fluidization zone arranged in accordance with the invention, especially in the stage of reduction of the FeO in order to extract the particles of agglomerated iron, especially in the case of ores which require a fairly high reduction temperature giving rise to agglomeration by sintering of the particles of iron as and when they are reduced.
  • Swiss Patent No. 292,727 also describes the application of fluidization to the manufacture of cement.
  • a zone of dense-phase fluidization constructed in accordance with the invention will be used with advantage in the part of the apparatus in which the clinkers form, the latter being evacuated, when they are of a sufiicient size, through the central cone and the venturi.
  • French Patent No. 1,050,572 describes the manufacture of zinc by reduction of ore by means of coal in a dense-phase fluidization apparatus which could be preferably constructed in accordance with the present invention, the elimination of the agglomerates formed by the coal ash and the matrix of ore being carried out through the central cone and the venturi.
  • An apparatus for the treatment of substances in a dense-phase fluidized mass comprising, in combination, means defining a fluidizing chamber, said chamber having a side wall, a substantially vertical conduit disposed below said chamber and having an upper extension, an upwardly divergent duct connected to said upper extension of said conduit and having an upward divergence comprised between 10 and 50, said duct being bounded by a substantially continuous wall and having an upper end opening into said chamber at a radial distance from said side wall, means for delivering a gaseous fluidizing agent to said conduit to create and ascending gaseous flow through said divergent duct, an upwardly divergent grate gradually sloping outwardly and upwardly from said upper end of said duct to said side wall and having a divergence substantially greater than that of said duct with said grate extending substantially closer to the horizontal than to the vertical, and means externally of said duct for supplying a gas to said chamber through said grate, whereby said gases enter said fluidizing chamber both from said duct and through said grat
  • said grate comprises overlapping elements in staggered formation to define a plurality of passages for the gas issuing from said gas supply means, said passages opening into the fluidizing chamber in a substantially verical direction.
  • said extension is a Venturi smoothly connecting said conduit with said divergent duct, the delivery point of the fluidizing agent delivering means being positioned below said Venturi, whereby said Venturi is traversed by an ascending gaseous flow.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US634234A 1956-01-19 1957-01-15 Apparatus for dense-phase fluidisation Expired - Lifetime US2906608A (en)

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BE (1) BE554203A (zh)
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Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3152005A (en) * 1962-03-29 1964-10-06 Dow Chemical Co Process for the preparation of pelletized solids
US3298792A (en) * 1961-09-28 1967-01-17 Montedison Spa Apparatus for improved fluidized beds and reactors containing same
US3329506A (en) * 1966-01-24 1967-07-04 Hupp Corp Method for roasting coffee and similar particulate solids
US3370938A (en) * 1965-07-30 1968-02-27 Allied Chem Method and apparatus for controlling particle size of fluidized beds
US3527575A (en) * 1966-03-31 1970-09-08 Gas Council Distributors of fluidizing media for fluidized beds
US3867110A (en) * 1973-12-17 1975-02-18 Inst Gas Technology Method of coal pretreatment
US3884649A (en) * 1973-10-29 1975-05-20 Inst Gas Technology Coal pretreater and ash agglomerating coal gasifier
US3935825A (en) * 1975-02-24 1976-02-03 Institute Of Gas Technology Coal ash agglomeration device
US4023280A (en) * 1976-05-12 1977-05-17 Institute Of Gas Technology Valve for ash agglomeration device
DE2654662A1 (de) * 1975-12-04 1977-06-08 Shell Int Research Verfahren und vorrichtung zur teilverbrennung von kohlestaub
US4076509A (en) * 1975-06-02 1978-02-28 Ab Bahco Ventilation Apparatus for processing dust-carrying gas and bulk goods
US4191539A (en) * 1976-06-07 1980-03-04 Institute Of Gas Technology Method for feeding caking coal particles to a gasifier
US4229289A (en) * 1979-03-12 1980-10-21 Institute Of Gas Technology Fluidized bed apparatus and process
EP0027280A1 (en) * 1979-10-15 1981-04-22 Institute of Gas Technology Process and apparatus for the conversion of agglomerating hydrocarbonaceous solid material to a more valuable gaseous product
EP0031856A1 (en) * 1979-12-28 1981-07-15 Institute of Gas Technology Device and process for converting coal particles to a fuel gas
FR2507203A1 (fr) * 1981-06-09 1982-12-10 Westinghouse Electric Corp Appareil et procede pour une gazeification de matieres carbonees en lits fluidises
US4369045A (en) * 1981-07-29 1983-01-18 Institute Of Gas Technology Fluidized bed gasification process with agglomerated solids removal
FR2555710A1 (fr) * 1983-11-28 1985-05-31 Fives Cail Babcock Procede pour la combustion ou la gazeification en lit fluidise de combustibles solides et dispositif pour la mise en oeuvre de ce procede
EP0246191A2 (en) * 1986-05-12 1987-11-19 Institute of Gas Technology Teatment of solids in a fluidized bed burner
US4854249A (en) * 1987-08-03 1989-08-08 Institute Of Gas Technology Two stage combustion
US4867756A (en) * 1986-05-20 1989-09-19 Institute Of Gas Technology Removal of sulfur compounds in fluidized bed carbonaceous solids gasification
US5006062A (en) * 1986-05-12 1991-04-09 Institute Of Gas Technology Treatment of solids in fluidized bed burner
US5014632A (en) * 1988-08-16 1991-05-14 A. Ahlstrom Corporation Distributor plate in a fluidized bed reactor
US5082634A (en) * 1985-05-13 1992-01-21 Bp Chemicals Limited Gas distribution plate for fluidization
WO2014152070A1 (en) * 2013-03-14 2014-09-25 Synthesis Energy Systems, Inc. Method and apparatus for recycling ash fines
CN105132039A (zh) * 2015-08-14 2015-12-09 新奥科技发展有限公司 流化床飞灰返炉气化设备及方法
CN107754733A (zh) * 2016-08-18 2018-03-06 北京华石联合能源科技发展有限公司 一种具有液相自循环功能的悬浮床反应器

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1199176B (de) * 1961-05-27 1965-08-19 Veit Dennert K G Baustoffbetie Intermittierendes Verfahren zum Herstellen von Blaehton
FI75504C (fi) * 1984-08-28 1988-07-11 Ahlstroem Oy Anordning i virvelbaeddsreaktor.
AT519392B1 (de) * 2016-11-09 2019-10-15 Beilschmidt Alfred Wirbelschichtreaktor

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1802960A (en) * 1929-03-22 1931-04-28 Fillmore Hyde A Hearth
US2409707A (en) * 1943-01-29 1946-10-22 Standard Oil Dev Co Cement manufacture
US2429721A (en) * 1944-01-28 1947-10-28 Standard Oil Dev Co Contacting gases and solids in fluidized systems
US2625463A (en) * 1946-04-27 1953-01-13 Babcock & Wilcox Co Method for producing hydrogen cyanide
US2657917A (en) * 1948-05-25 1953-11-03 Robert E Stanton Method of high-temperature treatment of compounds
US2700592A (en) * 1950-03-13 1955-01-25 Dorr Co Method of carrying out endothermic reactions under fluidizing conditions

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Publication number Priority date Publication date Assignee Title
FR953869A (fr) * 1946-10-09 1949-12-14 Standard Oil Dev Co Mise en contact de solides fluidifiés avec des gaz
FR1079088A (fr) * 1953-03-06 1954-11-25 Appareils de fluidisation en phase dense

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1802960A (en) * 1929-03-22 1931-04-28 Fillmore Hyde A Hearth
US2409707A (en) * 1943-01-29 1946-10-22 Standard Oil Dev Co Cement manufacture
US2429721A (en) * 1944-01-28 1947-10-28 Standard Oil Dev Co Contacting gases and solids in fluidized systems
US2625463A (en) * 1946-04-27 1953-01-13 Babcock & Wilcox Co Method for producing hydrogen cyanide
US2657917A (en) * 1948-05-25 1953-11-03 Robert E Stanton Method of high-temperature treatment of compounds
US2700592A (en) * 1950-03-13 1955-01-25 Dorr Co Method of carrying out endothermic reactions under fluidizing conditions

Cited By (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3298792A (en) * 1961-09-28 1967-01-17 Montedison Spa Apparatus for improved fluidized beds and reactors containing same
US3152005A (en) * 1962-03-29 1964-10-06 Dow Chemical Co Process for the preparation of pelletized solids
US3370938A (en) * 1965-07-30 1968-02-27 Allied Chem Method and apparatus for controlling particle size of fluidized beds
US3329506A (en) * 1966-01-24 1967-07-04 Hupp Corp Method for roasting coffee and similar particulate solids
US3527575A (en) * 1966-03-31 1970-09-08 Gas Council Distributors of fluidizing media for fluidized beds
US3884649A (en) * 1973-10-29 1975-05-20 Inst Gas Technology Coal pretreater and ash agglomerating coal gasifier
US3867110A (en) * 1973-12-17 1975-02-18 Inst Gas Technology Method of coal pretreatment
US3935825A (en) * 1975-02-24 1976-02-03 Institute Of Gas Technology Coal ash agglomeration device
US4076509A (en) * 1975-06-02 1978-02-28 Ab Bahco Ventilation Apparatus for processing dust-carrying gas and bulk goods
DE2654662A1 (de) * 1975-12-04 1977-06-08 Shell Int Research Verfahren und vorrichtung zur teilverbrennung von kohlestaub
US4023280A (en) * 1976-05-12 1977-05-17 Institute Of Gas Technology Valve for ash agglomeration device
US4191539A (en) * 1976-06-07 1980-03-04 Institute Of Gas Technology Method for feeding caking coal particles to a gasifier
US4229289A (en) * 1979-03-12 1980-10-21 Institute Of Gas Technology Fluidized bed apparatus and process
US4315758A (en) * 1979-10-15 1982-02-16 Institute Of Gas Technology Process for the production of fuel gas from coal
JPH0143799B2 (zh) * 1979-10-15 1989-09-22 Insuchi* Obu Gasu Tekunorojii
EP0027280A1 (en) * 1979-10-15 1981-04-22 Institute of Gas Technology Process and apparatus for the conversion of agglomerating hydrocarbonaceous solid material to a more valuable gaseous product
JPS5661486A (en) * 1979-10-15 1981-05-26 Inst Gas Technology Method and apparatus for converting hydrocarbon solid matter to gas product
EP0031856A1 (en) * 1979-12-28 1981-07-15 Institute of Gas Technology Device and process for converting coal particles to a fuel gas
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CN105189712B (zh) * 2013-03-14 2017-10-24 综合能源有限公司 用于再循环细灰的方法和装置
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CN105132039B (zh) * 2015-08-14 2018-01-12 新奥科技发展有限公司 流化床飞灰返炉气化设备及方法
CN107754733A (zh) * 2016-08-18 2018-03-06 北京华石联合能源科技发展有限公司 一种具有液相自循环功能的悬浮床反应器

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FR1141539A (fr) 1957-09-03
DE1045986B (de) 1958-12-11

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