US3912465A - Continuous carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier - Google Patents

Continuous carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier Download PDF

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US3912465A
US3912465A US493647A US49364774A US3912465A US 3912465 A US3912465 A US 3912465A US 493647 A US493647 A US 493647A US 49364774 A US49364774 A US 49364774A US 3912465 A US3912465 A US 3912465A
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particulate
bed
heat carrier
column
carbonization
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Daizo Kunii
Taiseki Kunugi
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    • 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
    • B01J8/32—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 with introduction into the fluidised bed of more than one kind of moving particles
    • 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
    • C10J3/54—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
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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

Definitions

  • ABSTRACT An apparatus and continuous process for the carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier is disclosed wherein the carbonization and gasification are separately carried out.
  • the process comprises the steps of fluidizing particulate heat carrier with steam to form a first fluidized bed, passing the particulate heat carrier through said first bed in a densely fluidized state from the bottom upwardly to the top of said first bed, and introducing particulate coal into the first bed thereby contacting said coal with said heat carrier to effect carbonization of the coal.
  • the resultant gas and oil vapor are withdrawn from the first bed, and a mixture of the particulate heat carrier and particulate coke produced by the carbonization of the coal is passed from the top of the first bed to the bottom of a second fluidized bed, and the particulate mixture is combined at the bottom of the second fluidized bed with particulate heat carrier coming from a third fluidized bed at a higher temperature.
  • the combined particulate materials are passed through the second fluidized bed in a densely fluidized state from the bottom upwardly to the top of the second bed to effect gasification of the particulate coke.
  • the gasified product is withdrawn from the second bed and a portion of the particulate heat carrier is passed from the top of the second bed to the bottom of a third fluidized bed.
  • the particulate heat carrier together with the accompanying ungasified particulate coke is passed through the third fluidized bed in a densely fluidized state from the bottom upwardly to the top of the third bed, and a hot combustion gas containing air or oxygen is introduced into the third bed thereby burning the ungasified particulate coke and heating said particulate heat carrier.
  • the heated particulate heat carrier is passed from the top of the third bed to the bottom of the second bed for use in the gasification of coke, and another portion of the particulate heat carrier is passed from the top of said second bed to the bottom of said first bed for use in the carbonization of coal.
  • the invention relates to a continuous process for the carbonization and gasiflcation of powdery or particulate coal (they are referred to particulate coal" hereafter.) with double recirculation of fluidized powdery or particulate (they are referred to particulate hereafter.) heat carrier, and to an apparatus therefore.
  • solid particulate heat carrier having a relatively large particle size, for example, an average particle size of 0.1 to 5 mm
  • carbonization column particulate coal having an average particle size 0.1 to 5 mm is contacted with the particulate heat carrier which is kept in a densely fluidized state, thereby to effect carbonization of the coal at a temperature which may vary within a wide range of 500 to 800C
  • particulate coke which has been formed in the carbonization step is gasified with steam in the presence of the particulate heat carrier kept in a densely fluidized state, whereby a gasified product predominantly comprised of hydrogen and carbon monoxide is produced.
  • the gasified product obtained by the process we previously proposed comprises a mixture of various gases, including hydrogen, carbon monoxide, various hydrocarbons, and nitrogen or sulfur-containing compounds. For some purposes it is desirable to separately obtain a fraction which is rich in hydrogen and carbon monoxide and another fraction which is rich in methane and otherhydrocarbons.
  • a primary object of the invention is to provide a continuous process for the gasification of coal which enables to produce a gaseous mixture which is rich in hydrogen and carbon monoxide and another gaseous mixture which is rich in methane and other hydrocarbons, separately.
  • Another object of the invention is to provide a continuous process for the gasification of coal wherein heat carrier particles having a relatively large size may be used.
  • Still another object of the invention is to provide a continuous process for the gasification of coal wherein carbonization of coal at a temperature of 500 to 800C and gasification of coke with steam at a temperature of 800 to 1,000C may separately and efficiently be carried out.
  • a further object of the invention is to provide a novel apparatus for the gasification of particulate coal with fluidized bed of particulate heat carrier, which comprises a carbonization column for carbonizing particulate coal, a gasification column for gasifying particulate coke from the carbonization column with steam and a combustion-heating column for heating the spent heat carrier for re-use.
  • a still further object of the invention is to provide a novel system, adapted for use in the novel process and apparatus of the invention, for recirculating the particulate heat carrier through the carbonization, gasification and combustion-heating columns.
  • a continuous process for the carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier wherein the carbonization and gasification are separately carried out comprises the steps of fluidizing particulate heat carrier having an average size of 0.1 to 5 mm with steam to form a first fluidized bed, passing said particulate heat carrier through said first bed in a densely fluidized state from the bottom upwardly to the top of said first bed, introducing particulate coal having an average size of 0.1 to 5 mm into said first bed thereby contacting said coal with said heat carrier to effect carbonization of the coal while maintaining said first bed at a temperature of 500 to 800C, as measured at the top of said first bed, withdrawing the resultant gas and oil vapor from said first bed, passing a mixture of the particulate heat carrier and particulate coke produced by the carbonization of the coal from the top of said first bed to the bottom of a second fluidized bed, said mixture being at a temperature of 500 to 800C,
  • Usable heat carrier is particulate inorganic substance, such as cement clinker, coal ash, sand, refractories, porous alumina, iron ores and the like, having an average particle size of 0.1 to 5 mm.
  • particulate ash produced by processing the starting particulate coal may conveniently be used.
  • coal solid fossil fuel, including, for example, peat, grass peat, lignite, brown coal, bituminous coal and the like.
  • an apparatus for the carbonization and gasiflcation of particulate coal with double recirculation of fluidized particulate heat carrier comprising an upright, generally cylindrical carbonization column in which a first fluidized bed of particulate heat carrier kept at a temperature of 500 to 800C, as measured at the top of said first bed, is formed for carbonizing particulate coal, said carbonization column having a height of at least three times as large as the maximum diameter, inlets provided at the bottom and lower portions of the side wall of said carbonization column for introducing steam into said carbonization column, at least one inlet provided at the side wall of said carbonization column above the positions where said inlets for steam are provided for introducing particulate coal into said carbonization column, an outlet provided at the top of said carbonization column for withdrawing a gas and oil vapor resulting from the carbonization of coal from said carbonization column, an upright, generally cylindrical gasification column in which a second fluidized bed of particulate heat carrier kept at a temperature of 800 to l,
  • FIG. 1 is a schematic vertical cross-sectional view of an apparatus in accordance with the invention
  • FIG. 2 is a schematic vertical cross-sectional view showing the upper part of another combustion and heating column which may be used in the practice of the invention
  • FIG. 3 is a schematic vertical cross-sectional view showing the bottom part of another carbonization column which may be used in the practice of the inven tion;
  • FIG. 4 is a schematic vertical cross-sectional view showing another gasification column which may be used in the practice of the invention.
  • FIG. 5 is a schematic vertical cross-sectional view showing still another combustion and heating column which may be used in the practice of the invention.
  • the illustrated apparatus comprises an upright generally cylindrical carbonization column A, an upright generally cylindrical gasification column B and an upright generally cylindrical combustion-heating column C, each having a height of at least three times as large as the maximum diameter of the column.
  • a densely fluidized bed of solid particulate heat carrier is formed in each column.
  • Each bed has a height of at least two times as large as the maximum diameter of the column.
  • the combustion-heating column C has upwardly increasing diameters.
  • the top of the fluidized bed formed in the carbonization column A and the top of the fluidized bed formed in the gasification column B are communicated through respective ducts 9 and 2 with the bottom of the gasification column B and the bottom of the carbonization column A, respectively.
  • top of the fluidized bed formed in the gasification column B and the top of the fluidized bed formed in the combustion and heating column C are communicated through respective ducts l7 aand 10 with the bottom the combustion-heating column C and the bottom of the gasification column B, respectively.
  • Heat carrier which has been passed from the top of the fluidized bed 14 in the gasification column B downwardly through a duct 2 predominantly by gravity to the bottom of the carbonization column A and is at a temperature of 800 to 1,000C, is fluidized with steam, which is introduced through an inlet 3 into the carbonization column A at the bottom thereof, to form a fluidized bed 1, and is passed upwardly through the carbonization column A while being kept in a densely fluidized state with steam, which is introduced through inlets 4,4 and 5,5 into the carbonization column A at lower portions thereof.
  • Particulate coal to be processed having an average size of 0.1 to 5 mm, is blown into the fluidized bed 1 through an inlet 6 provided in the side wall of the carbonization column A, contacted with the hot heat carrier and carbonized.
  • the gas and oil vapor so produced together with the steam leaving the fluidized bed 1 are passed through a space 7 above the fluidized bed 1 in the carbonization column A, discharged from an outlet 8 of the column A and passed to subsequent processing steps.
  • the number of the inlets 4,4' or 5,5 at each level, the number of such levels as well as the location and type of the inlets, and the type, number and location of the inlet 6 for feeding particulate coal are not limited to those as shown in FIG. 1 and may suitably be selected in accordance with a design known per se for the maintenance of the desired conditions in the carboniztion column A.
  • the fluidized bed 1 is maintained at a temperature of 500 to 800C, when measured at the top of the bed.
  • the particulate heat carrier and the particulate coke which has been produced by the carbonization of the particulate coal, both being at a temperature of 500 to 800C, are then passed from the top of the fluidized bed 1 in the carbonization column A downwardly through a duct 9 predominantly by gravity to the bottom of the gasification column B, where they are admixed with the heat carrier which has been passed from the top of the fluidized bed 22 in the combustionheating column C downwardly through a duct 10 predominantly by gravity to the bottom of the gasification column B and is at a temperature of 850 to l,l0OC and, the combined particulate material is fluidized with steam, which is introduced through an inlet 11 into the gasification column at the bottom thereof to form the fluidized bed 14, and is passed upwardly through the gasification column B while being kept in a densely fluidized state with steam, which is introduced through inlets 12,12 and 13,13 into the gasification column B at lower portions thereof.
  • the steam reacts with and gasifies the particulate coke.
  • the gas so produced predominantly comprised of hydrogen and carbon monoxide together with unreacted steam leaving the fluidized bed 14 is passed through a space 15 above the fluidized bed 14 in the gasification column B, discharged from an outlet 16 of the column B and passed to subsequent processing steps.
  • the number of inlets 12,12 or 13,13 at each level, the number of such levels as well as the location and type of the inlets are not limited to those as shown in FIG. 1 and may suitably be selected in accordance with a design known per se for the maintenance of the desired conditions in the gasification column B.
  • the fluidized bed 14 is maintained at a temperature of 800 to 1,000C, when measured at the top of the bed.
  • a hot combustion gas containing air or oxygen is introduced into the densely fluidized bed 22 through an inlet 21 provided in the side wall of the combustion-heating column C thereby to substantially completely burn the ungasified particulate coke accompanied by the heat carrier from the gasification column B and to heat the particulate heat carrier to a temperature of 850 to l,100C.
  • the resultant combustion gas leaves the fluidized bed 22 and is passed through a space 23 above the fluidized bed 22 in the column C and withdrawn through an outlet 24 from the system for subsequent treatments.
  • the type, location and type of the inlets 19,19 20,20 and 21 are not limited to those as illustrated in FIG. 1.
  • a part of particulate ash produced by the combustion the particulate coke is acompanied by the combustion gas and discharged from the system through the outlet 24.
  • the ash may be withdrawn from the combustion and heating column C through an outlet 25 provided in the side wall of the column C in the proximity of the top of the fluidized bed 22.
  • a part of the particulate heat carrier is accompanied by the withdrawn ash, it may be separated from the ash outside the system and may be fed back to the system through an inlet 26. While the illustrated apparatus has such an inlet 26 located at an upper portion of the combustion-heating column C, it should be appreciated that such an inlet 26 may be provided in any one of the columns.
  • the particulate heat carrier which has been heated in the combustion-heating col umn C to a temperature of 850 to 1,100C, travel from the top of the fluidized bed 22 in the column C downwardly through the duct 10 predominantly by gravity to the bottom of the gasification column B, where it is admixed with a mixture of the particulate heat carrier and particulate coke which mixture has come from the top of the fluidized bed 1 in the carbonization column A through the duct 9 and is at a temperature of 500 to 800C.
  • the combined particulate material is fluidized with steam supplied through the inlet 11 to form the fluidized bed 14 and passed upwardly trough the gasification column B while being kept in a densely fluidized state with steam introduced through the inlets 12,12 and 13,13 into the column B.
  • the particulate coke in the fluidized bed 14 is gasified with the steam and, the fluidized bed 14 is maintained at a temperature of 800 to l,00OC, as measured at the top of said bed.
  • the combustion gas withdrawn from the combustionheating column C is accompanied by an amount of the particulate heat carrier.
  • any accompanying heat carrier may be collected in a suitable collector, such as cyclone 27 (see FIG. 2), provided just below the outlet 24 in the space 23 above the bed 22, and may be fed back to the bed 22. The same is applicable with respect to the columns A and B.
  • a collector 27 may be located just outside the outlet 24, 16 or 8.
  • column A or B which may be used is not limited to that shown in FIG. 1.
  • carbonization column A may has a construction as shown in FIG. 3, with respect to the connection of the duct 2 to the bottom of the column A.
  • Further gasification column B may have a substantially uniform cross-section, as shown in FIG. 4.
  • the column C should preferably has upwardly increasing crosssectional areas.
  • Column C may be of the shape as shown in FIG. 5.
  • Columns A, B and C may have different diameters.
  • the carbonization and gasification of particulate coal having an average particle size of 0.1 to 5 mm are separately carried out and, thus, a mixture of normally liquid hydrocarbons and normally gaseous hydrocarbons is obtained on one hand from the carbonization column A, and a gas rich in hydrogen and carbon monoxide is separately obtained from the gasification column B on the other hand. Since the former mixture may readily be separated into the normally liquid hydrocarbons and the normally gaseous hydrocarbons by a method known per se, the normally liquid hydrocarbons, the normally gaseous hydrocarbons as well as the gaseous mixture predominantly comprised of hydrogen and carbon monoxide may effectively be produced from coal without excessive decomposition of the valuble components of coal.
  • recirculation of particulate heat carrier may be performed very stably and, controlling of the rate of recirculation and of tempertures of carbonization, gasification and combustionheating columns are readily carried out.
  • the process of the invention is advantageous in that the particle size of the usable particulate heat carrier may vary within the specified wide range; that loss due to abrasion of the particulate heat carrier and parts of the apparatus may be minimized since in the practice of the invention there is no chance for particulate material to impinge against the wall of the apparatus at high velocities; and that the apparatus used can be low in height.
  • a continuous process for the carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier wherein the carbonization and gasification are separately carried out comprises the steps of fluidizing particulate heat carrier having an average particle size of 0.1 to 5 mm with steam to form a first fluidized bed, passing said particulate heat carrier through said first bed in a densely fluidized state from the bottom upwardly to the top of said first bed, introducing particulate coal having an average particle size of 0.1 to 5 mm into said first bed thereby contacting said coal with said heat carrier to effect carbonization of the coal while maintaining said first bed at a temperature of 500 to 800C, as measured at the top of said firstbed, withdrawing the resultant gas and oil vapor from said first bed, passing a mixture of the particulate heat carrier and particulate coke produced by the carbonization of the coal from the top of said first bed to the bottom of a second fluidized bed, said mixture being at a temperature of 500 to 800C, combining at the bottom of said
  • each of said first, second and third fluidized bed has an upright, generally cylindrical configuration.
  • An apparatus for the carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier comprising an upright, generally cylindrical carbonization column in which a first fluidized bed of particulate heat carrier kept at a temperature of 500 to 800C, as measured at the top of said first bed, is formed for carbonizing particulate coal, said carbonization column having a height of at least three times as large as the maximum diameter, inlets provided at the bottom and lower portions of the side wall of said carbonization column for introducing steam into said carbonization column, at least one inlet provided at the side wall of said carbonization column above the positions where said inlets for steam are provided for introducing particulate coal into said carbonization column, an inlet provided at the top of said carbonization column for withdrawing a gas and oil vapor resulting from the carbonization of coal from said carbonization column, an upright, generally cylindrical gasification column in which a second fluidized bed of particulate heat carrier kept at a temperature of 800 to 1,000C, as measured at the top of said second bed, is formed
  • each column is provided with means for separating solid particulate material from the gas leaving

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  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US493647A 1973-08-18 1974-07-30 Continuous carbonization and gasification of particulate coal with double recirculation of fluidized particulate heat carrier Expired - Lifetime US3912465A (en)

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JP (1) JPS55439B2 (enrdf_load_stackoverflow)
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IN (1) IN143271B (enrdf_load_stackoverflow)
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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4007092A (en) * 1975-03-18 1977-02-08 Exxon Research And Engineering Company Process for producing low sulfur coke
US4118201A (en) * 1976-07-14 1978-10-03 Mobil Oil Corporation Production of low sulfur fuels from coal
US4280893A (en) * 1977-12-06 1981-07-28 Leas Arnold M Integrated coal conversion process
US4311670A (en) * 1976-09-22 1982-01-19 A. Ahlstrom Osakeyhtio Fluidized bed reactor system
WO1985000119A1 (en) * 1983-06-20 1985-01-17 Battelle Development Corporation High-velocity multisolid fluidized bed process
GB2182344A (en) * 1985-11-04 1987-05-13 British Gas Corp Gasification of solid carbonaceous material
US4704138A (en) * 1982-12-06 1987-11-03 Atlantic Richfield Company Spouted bed heating of solids for coal gasification
US4738207A (en) * 1986-01-11 1988-04-19 Gerald Moss Non-polluting method of burning fuel for heat and CO2
US5290327A (en) * 1988-08-23 1994-03-01 Gottfried Rossle Device and allothermic process for producing a burnable gas from refuse or from refuse together with coal
US5346515A (en) * 1986-10-16 1994-09-13 Bergwerksverband Gmbh Fluidized bed gas generator for allothermic gasification of coal
US6276441B1 (en) * 1992-10-02 2001-08-21 Neste Oy Method and regenerator for regenerative heat transfer
RU2220187C2 (ru) * 1997-12-18 2003-12-27 Ибара Корпорейшн Система газификации топлива
EP1449907A1 (fr) * 2003-02-24 2004-08-25 Institut Francais Du Petrole Installation et procédé de gazéification multi-étapes d'une charge comprenant de la matière organique
US20080134581A1 (en) * 2005-02-01 2008-06-12 Johannes Christoffel Van Dyk Method Of Operating A Fixed Bed Dry Bottom Gasifier
CN101955801A (zh) * 2010-10-15 2011-01-26 山东联合能源技术有限公司 L型卧式回转波浪床煤气化生产工艺及系统
DE102017106347A1 (de) 2017-03-24 2018-09-27 Universität Stuttgart Verfahren und Vorrichtung zur allothermen Herstellung von Brenngasen
US20230357641A1 (en) * 2020-09-14 2023-11-09 University Of Pretoria Fluidised bed pyrolysis apparatus and method

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US4331529A (en) * 1980-11-05 1982-05-25 Exxon Research & Engineering Co. Fluid coking and gasification process
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JP5261931B2 (ja) * 2006-12-26 2013-08-14 株式会社Ｉｈｉ 流動層ガス化方法及び装置

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US4007092A (en) * 1975-03-18 1977-02-08 Exxon Research And Engineering Company Process for producing low sulfur coke
US4118201A (en) * 1976-07-14 1978-10-03 Mobil Oil Corporation Production of low sulfur fuels from coal
US4311670A (en) * 1976-09-22 1982-01-19 A. Ahlstrom Osakeyhtio Fluidized bed reactor system
US4280893A (en) * 1977-12-06 1981-07-28 Leas Arnold M Integrated coal conversion process
US4704138A (en) * 1982-12-06 1987-11-03 Atlantic Richfield Company Spouted bed heating of solids for coal gasification
WO1985000119A1 (en) * 1983-06-20 1985-01-17 Battelle Development Corporation High-velocity multisolid fluidized bed process
GB2182344A (en) * 1985-11-04 1987-05-13 British Gas Corp Gasification of solid carbonaceous material
US4738207A (en) * 1986-01-11 1988-04-19 Gerald Moss Non-polluting method of burning fuel for heat and CO2
US5346515A (en) * 1986-10-16 1994-09-13 Bergwerksverband Gmbh Fluidized bed gas generator for allothermic gasification of coal
US5290327A (en) * 1988-08-23 1994-03-01 Gottfried Rossle Device and allothermic process for producing a burnable gas from refuse or from refuse together with coal
US6276441B1 (en) * 1992-10-02 2001-08-21 Neste Oy Method and regenerator for regenerative heat transfer
US7618469B2 (en) 1997-12-18 2009-11-17 Ebara Corporation Fuel gasification system
US20050144844A1 (en) * 1997-12-18 2005-07-07 Norihisa Miyoshi Fuel gasification system
US7390337B2 (en) * 1997-12-18 2008-06-24 Ebara Corporation Fuel gasification system
US20080263952A1 (en) * 1997-12-18 2008-10-30 Norihisa Miyoshi Fuel gasification system
RU2220187C2 (ru) * 1997-12-18 2003-12-27 Ибара Корпорейшн Система газификации топлива
US7811340B2 (en) 2003-02-24 2010-10-12 Institute Francais Du Petrole Multi-stage facility and method for gasifying a feedstock including organic matter
FR2851570A1 (fr) * 2003-02-24 2004-08-27 Inst Francais Du Petrole Installation et procede de gazeification multi-etapes d'une charge comprenant de la matiere organique
EP1449907A1 (fr) * 2003-02-24 2004-08-25 Institut Francais Du Petrole Installation et procédé de gazéification multi-étapes d'une charge comprenant de la matière organique
US20080134581A1 (en) * 2005-02-01 2008-06-12 Johannes Christoffel Van Dyk Method Of Operating A Fixed Bed Dry Bottom Gasifier
US8252074B2 (en) * 2005-02-01 2012-08-28 Sasol-Lurgi Technology Company (Proprietary) Limited Method of operating a fixed bed dry bottom gasifier
CN101955801A (zh) * 2010-10-15 2011-01-26 山东联合能源技术有限公司 L型卧式回转波浪床煤气化生产工艺及系统
CN101955801B (zh) * 2010-10-15 2013-08-14 山东联合能源技术有限公司 L型卧式回转波浪床煤气化生产工艺及系统
DE102017106347A1 (de) 2017-03-24 2018-09-27 Universität Stuttgart Verfahren und Vorrichtung zur allothermen Herstellung von Brenngasen
US20230357641A1 (en) * 2020-09-14 2023-11-09 University Of Pretoria Fluidised bed pyrolysis apparatus and method

Also Published As

Publication number Publication date
IN143271B (enrdf_load_stackoverflow) 1977-10-29
JPS5041903A (enrdf_load_stackoverflow) 1975-04-16
JPS55439B2 (enrdf_load_stackoverflow) 1980-01-08
ZA745181B (en) 1975-08-27
CA1035144A (en) 1978-07-25
AU7235574A (en) 1976-02-19

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