US3011953A - Method and apparatus for the carbonization of fluidized materials - Google Patents

Method and apparatus for the carbonization of fluidized materials Download PDF

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US3011953A
US3011953A US746266A US74626658A US3011953A US 3011953 A US3011953 A US 3011953A US 746266 A US746266 A US 746266A US 74626658 A US74626658 A US 74626658A US 3011953 A US3011953 A US 3011953A
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gases
product
chamber
bed
fluidised
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Foch Pierre
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Charbonnages de France CDF
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised 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
    • B01J8/26—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 two or more fluidised beds, e.g. reactor and regeneration installations
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S208/00—Mineral oils: processes and products
    • Y10S208/951—Solid feed treatment with a gas other than air, hydrogen or steam

Definitions

  • This invention relates to a method for the thermal treatment of coal using the fluidised bed technique. It also relates to an apparatus for carrying out this method in a continuous manner.
  • the invention concerns improvements in methods in which coal fines are subjected to the action of heat in a fluidised bed, in the presence of a fluidising gas, by a partial combustion of the mass. t applies, more generally, to carbonisation methods at high or low temperature wherein the main object to be achieved is the production of granulated or pulverulent coke or semi-coke.
  • the invention is characterised in that a part of the pyrolysis gases is burned and used to simultaneously preheat the fluidised product to be treated and crack the tars contained in the pyrolysis gases.
  • the invention is further characterised by the use, in a. closed circuit, of spent gases, hereinafter called fumes, in combination with an injection of Water in order to cool the fluidised solid product obtained.
  • the invention also concerns a new apparatus for carrying out the aforesaid method.
  • This apparatus consists of a three-stage vertical retort, these three superposed stages being respectively intended for the carbonisation of the fluidised coal, the partial combustion of the pyrolysis gases and the heating thereof, and the preheating of the coal fines by fluidising them with the gases coming from the preceding stage.
  • FIGURE 1 is a diagrammatic view of an installation for putting into practice the method according to the invention.
  • FIGURE 2 shows a specific embodiment of a new apparatus for carrying out the method according to the invention.
  • This installation and this apparatus are designed for the carbonisation of fluidised coal, at temperatures approximately ranging between 930 F. and 1,650 F., in order to obtain a granulated semi-coke, sm'd coal being preheated to about 570 F. to 750 F., and air being added, if necessary, at a temperature which should be advantageously as high as possible, but which, in accordance with simple and conventional methods, will be usually in the neighbourhood of 930 F.
  • the pyrolysis gas heated to a temperature of 1,830" F. by partial combustion, is used for preheating the product.
  • the installation shown in FIGURE 1 essentially comprises a carbonisation reactor 1 making use of the fluidisation technique, a combustion chamber 2, a drying and preheating chamber 3 also making use of the fluidisation technique and a cooling chamber 4.
  • the carbonisation treatment is effected in the reactor 1, supplied with hot crude, such as coal fines, from a conduit 5 end a feeder 6.
  • the fiuidising fluid (generally air) is supplied through a pipe 7 after having been heated in the combustion chamber 2.
  • the rate of fiow of the fluid and the rate of flow of coal fines are adjusted so as to maintain the fluidised mass contained in the retort 1 at a temperature suitable for the partial combustion thereof in the fluidised bed.
  • the reaction gases are discharged into the combustion chamber 2 through a pipe 8, after having been made dust-free in a cyclone separator 9.
  • the collected dust is recycled into the reactor through a pipe 1%.
  • the gases are partly burned by supplying preheated or non-preheated air through a pipe 11.
  • the combustion is only very partial so that the gas retains a high calorific power.
  • the combustion is so regulated as to obtain a temperature of about 1,650 F. or more, so that the condensable products are cracked.
  • the heated gases pass through a pipe 12 through which they are fed into the chamber 3 with a view to drying and heating the fluidised crude product.
  • the drying and preheating chamber 3 is fed with the crude product through a pipe 13 and a feeder 14, which is in turn fed from a hopper 15.
  • the heated and dried product is transferred to the reactor 1 through the feeder 6.
  • the ratio of heated gas to coal in the chamber 3 is so adjusted that the temperature is maintained therein at a predetermined level, generally comprised between 570 F. and 750 F.
  • the partly cooled fumes are made dustfree by means of a cyclone separator 16 and evacuated through 17.
  • Suificient quantities of neutral gases are introduced through a conduit 19 to compensate the losses occurring in a closed circuit 20 which is adapted to cool the fluidised final product in the cooling chamber 4, supplied With the treated product from the reactor 1 through a conduit 21 and a feeder 22.
  • the closedcircuit is cooled by a cooler 23.
  • the cooled product is extracted at 25 for further treatment.
  • the retort shown in FIGURE 2 comprises a carbonisation reactor 51 making use of the fluidisation technique, a combustion chamber 52 and a drying chamber 53 also making use of the fluidisation technique.
  • the carbonisation treatment is carried out in the retort 51, supplied with heated crude product through a pipe 54 and a feeder 55.
  • the fluid for the fiuidisation treatment is introduced through a pipe 56 leading from a heat exchanger 66.
  • the rate of flow of the fluid and the rate of flow of fines are so adjusted as to maintain the fluidised mass in the retort 51 at the processing temperature by a partial combustion within the bed.
  • the gases issuing from the reaction chamber are discharged into the combustion chamber 52 via channel 57.
  • the partial combustion of these gases is obtained by introducing preheated or non-preheated air through the pipe 58.
  • the very partial combustion is so adjusted as to obtain a temperature of about l,650 F. or more, thus causing the condensable products to crack.
  • a portion of the gases is transferred to the heat exchanger 69 through a pipe 59, and is then evacuated through a general conduit 68. But the greater proportion of the gases originating from the combustion chamber 52 is used for drying and heating the fluidised crude product.
  • a conduit 61 establishes a direct communication between thecombustion chamber 52 and the drying chamber 53.
  • This drying chamber having a fluidised bed, is supplied with the crude product through a pipe 62 and a feeder 63, which is in turn fed from a hopper 64.
  • the heated and dried product is transferred, as has already been stated, into the reactor 51 by way of the feeder 55.
  • the ratio of hot gases to coal in the chamber 53 is so adjusted that the temperature is maintained therein at a predetermined level, which will be generally comprised between 570 F. and 750 F.
  • the partly cooled gases are discharged through 65 and pass into a cyclone separator 66, firom which the dust is recycled into the drying chamber at 67.
  • the dust-free gases are evacuated through 68.
  • Neutral cold gases are introduced through pipe in function of the losses occurring in a closed circuit 71 which is provided for the cooling of the fluidised final product in a cooling chamber 72, supplied with the treated product from the reactor 5]. through a conpartial combustion to be efiected. This results in an improved yield of semi-coke and of gases.
  • the quality of I the semi-coke is improved through the decrease of its ash contents.
  • the calorific power of the gas is improved because of a lesser dilution by fumes (ntirogen and carbon dioxide).
  • this preheating step can be effected either in parallel with the preheating of the coal (FIGURE 2) or in series therewith (FIGURE 1).
  • An apparatus for the continuous carbonisation of 4 coal fines by the fiuidisation technique comprising a vertical retort including three chambers disposed in vertical alignment one above the other, and which starting from the bottom, consist of a reactor for fluidised treatment, a chamber for the post-combustion of the gases of pyrolysis and a chamber for preheating by V iluidisation; means within the confines of saidiretort directly connecting the reactor for fluidised treatment and the post-combustion chamber of pyrolysis gases and meansrwithin the confines of said retort directly connecting the post-combustion chamber and the chamber for preheating by iluidisation; means for adding air into the post-combustion chamber; and'means for transferring the product to be treated by gravity between the preheating and reaction chambers.
  • An apparatus according to claim Land means for preheating air added into the post-combustion chamber.
  • a method for the continuous carbonization of fluidized coal fines comprisin forming a bed of a heated product to be treated, introducing an oxydizing fluid into the bed toproduce turbulence in the bed and cause a stabilized reaction by partial combustion of the said product, mixing air with gases originating from said reaction, said gases having essentially the same constituents as when evolved, and causing a partial combustion thereof, the temperature of the resulting gases of which is'not less than about 900 C., to simultaneously cause a cracking of condensable products, and preheating said product to be treated in a fluidised state by a portion of said resulting gases originating from the last mentioned partial combustion of the gases.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Description

Dec. 5, 1961 P. FOCH 3,011,953
METHOD AND APPARATUS FOR THE CARBONIZATION 0F FLUIDIZED MATERIALS Filed July 2, 1958 2 Sheets-Sheet 1 7 milk wi cs Maw Dec. 5, 1961 c 3,011,953
METHOD AND APPARATUS FOR THE CARBONIZATION OF FLUIDIZED MATERIALS Filed July 2, 1958 2 Sheets-Sheet 2 7 fiflk (A), LocCS United States Patent 3,911,953 METHOD AND APPARATUS FOR THE CARBGNI- ZATION 0F FLUIDIZED MATERIALS Pierre Foch, Forbach, Moselle, France, assignor to Charbonnages de France, Paris, France, a public institution of the French Republic Filed July 2, 1958, Ser. No. 745,266
Claims. (Cl. 2G2--6) This invention relates to a method for the thermal treatment of coal using the fluidised bed technique. It also relates to an apparatus for carrying out this method in a continuous manner.
The invention concerns improvements in methods in which coal fines are subjected to the action of heat in a fluidised bed, in the presence of a fluidising gas, by a partial combustion of the mass. t applies, more generally, to carbonisation methods at high or low temperature wherein the main object to be achieved is the production of granulated or pulverulent coke or semi-coke.
The invention is characterised in that a part of the pyrolysis gases is burned and used to simultaneously preheat the fluidised product to be treated and crack the tars contained in the pyrolysis gases.
The invention is further characterised by the use, in a. closed circuit, of spent gases, hereinafter called fumes, in combination with an injection of Water in order to cool the fluidised solid product obtained.
The invention also concerns a new apparatus for carrying out the aforesaid method. This apparatus consists of a three-stage vertical retort, these three superposed stages being respectively intended for the carbonisation of the fluidised coal, the partial combustion of the pyrolysis gases and the heating thereof, and the preheating of the coal fines by fluidising them with the gases coming from the preceding stage.
Other features and advantages of the present invention will become clear on reading the following escription with reference to the accompanying drawings, in which:
FIGURE 1 is a diagrammatic view of an installation for putting into practice the method according to the invention, and
FIGURE 2 shows a specific embodiment of a new apparatus for carrying out the method according to the invention.
This installation and this apparatus are designed for the carbonisation of fluidised coal, at temperatures approximately ranging between 930 F. and 1,650 F., in order to obtain a granulated semi-coke, sm'd coal being preheated to about 570 F. to 750 F., and air being added, if necessary, at a temperature which should be advantageously as high as possible, but which, in accordance with simple and conventional methods, will be usually in the neighbourhood of 930 F. The pyrolysis gas, heated to a temperature of 1,830" F. by partial combustion, is used for preheating the product.
The installation shown in FIGURE 1 essentially comprises a carbonisation reactor 1 making use of the fluidisation technique, a combustion chamber 2, a drying and preheating chamber 3 also making use of the fluidisation technique and a cooling chamber 4.
The carbonisation treatment is effected in the reactor 1, supplied with hot crude, such as coal fines, from a conduit 5 end a feeder 6. The fiuidising fluid (generally air) is supplied through a pipe 7 after having been heated in the combustion chamber 2. The rate of fiow of the fluid and the rate of flow of coal fines are adjusted so as to maintain the fluidised mass contained in the retort 1 at a temperature suitable for the partial combustion thereof in the fluidised bed.
The reaction gases are discharged into the combustion chamber 2 through a pipe 8, after having been made dust-free in a cyclone separator 9. The collected dust is recycled into the reactor through a pipe 1%.
In the combustion chamber 2, the gases are partly burned by supplying preheated or non-preheated air through a pipe 11. The combustion is only very partial so that the gas retains a high calorific power. The combustion is so regulated as to obtain a temperature of about 1,650 F. or more, so that the condensable products are cracked. The heated gases pass through a pipe 12 through which they are fed into the chamber 3 with a view to drying and heating the fluidised crude product. The drying and preheating chamber 3 is fed with the crude product through a pipe 13 and a feeder 14, which is in turn fed from a hopper 15. The heated and dried product is transferred to the reactor 1 through the feeder 6. The ratio of heated gas to coal in the chamber 3 is so adjusted that the temperature is maintained therein at a predetermined level, generally comprised between 570 F. and 750 F. The partly cooled fumes are made dustfree by means of a cyclone separator 16 and evacuated through 17. Suificient quantities of neutral gases are introduced through a conduit 19 to compensate the losses occurring in a closed circuit 20 which is adapted to cool the fluidised final product in the cooling chamber 4, supplied With the treated product from the reactor 1 through a conduit 21 and a feeder 22. The closedcircuit is cooled by a cooler 23. The cooled product is extracted at 25 for further treatment.
The retort shown in FIGURE 2 comprises a carbonisation reactor 51 making use of the fluidisation technique, a combustion chamber 52 and a drying chamber 53 also making use of the fluidisation technique.
The carbonisation treatment is carried out in the retort 51, supplied with heated crude product through a pipe 54 and a feeder 55. The fluid for the fiuidisation treatment is introduced through a pipe 56 leading from a heat exchanger 66. The rate of flow of the fluid and the rate of flow of fines are so adjusted as to maintain the fluidised mass in the retort 51 at the processing temperature by a partial combustion within the bed.
The gases issuing from the reaction chamber are discharged into the combustion chamber 52 via channel 57. The partial combustion of these gases is obtained by introducing preheated or non-preheated air through the pipe 58. The very partial combustion is so adjusted as to obtain a temperature of about l,650 F. or more, thus causing the condensable products to crack. A portion of the gases is transferred to the heat exchanger 69 through a pipe 59, and is then evacuated through a general conduit 68. But the greater proportion of the gases originating from the combustion chamber 52 is used for drying and heating the fluidised crude product. For this purpose, a conduit 61 establishes a direct communication between thecombustion chamber 52 and the drying chamber 53. This drying chamber, having a fluidised bed, is supplied with the crude product through a pipe 62 and a feeder 63, which is in turn fed from a hopper 64. The heated and dried product is transferred, as has already been stated, into the reactor 51 by way of the feeder 55. The ratio of hot gases to coal in the chamber 53 is so adjusted that the temperature is maintained therein at a predetermined level, which will be generally comprised between 570 F. and 750 F. The partly cooled gases are discharged through 65 and pass into a cyclone separator 66, firom which the dust is recycled into the drying chamber at 67. The dust-free gases are evacuated through 68. Neutral cold gases are introduced through pipe in function of the losses occurring in a closed circuit 71 which is provided for the cooling of the fluidised final product in a cooling chamber 72, supplied with the treated product from the reactor 5]. through a conpartial combustion to be efiected. This results in an improved yield of semi-coke and of gases. The quality of I the semi-coke is improved through the decrease of its ash contents. The calorific power of the gas is improved because of a lesser dilution by fumes (ntirogen and carbon dioxide).
ltiwill be noted, that, as is the case in most methods of carbonisation by the fluidisation technique, it is advantageous to preheat the air or the processing gas. it will be noted that in the method according to the invention, this preheating step can be effected either in parallel with the preheating of the coal (FIGURE 2) or in series therewith (FIGURE 1).
The partial. combustion of the pyrolysis gases at a suflicient temperature within the combustion chamber 2 64 or 72, combined withfluidisation bymeans of the fumes introduced in 19 or 72, is valuable in case of carbonisation at low temperature, Where a very reactive solid product is involved, which has to be cooled'very rapidly in the absence of air, in order to avoid spontaneous re-ignitions. It is to be understood that this invention has just been described by way of explanation, without limitation of the same, and that various modificationscan be made therein without exceeding its scope, in particular by modifying the carbonisation conditions and change the gasification rates by making use of other fluids'than air, such as oxygen, steam, oXydizing gases, or any other fluid, commonlyused, or their mixtures.
I claim:
An apparatus for the continuous carbonisation of 4 coal fines by the fiuidisation technique, said apparatus comprising a vertical retort including three chambers disposed in vertical alignment one above the other, and which starting from the bottom, consist of a reactor for fluidised treatment, a chamber for the post-combustion of the gases of pyrolysis and a chamber for preheating by V iluidisation; means within the confines of saidiretort directly connecting the reactor for fluidised treatment and the post-combustion chamber of pyrolysis gases and meansrwithin the confines of said retort directly connecting the post-combustion chamber and the chamber for preheating by iluidisation; means for adding air into the post-combustion chamber; and'means for transferring the product to be treated by gravity between the preheating and reaction chambers.
2. An apparatus according to claim Land means for preheating air added into the post-combustion chamber.
3. 'An apparatus in accordance with claim 1, wherein the second-mentioned connecting means allows the passage of iluidisation gas into the preheatingchamber at substantially the lowest level thereof.
4. A method for the continuous carbonization of fluidized coal fines comprisin forming a bed of a heated product to be treated, introducing an oxydizing fluid into the bed toproduce turbulence in the bed and cause a stabilized reaction by partial combustion of the said product, mixing air with gases originating from said reaction, said gases having essentially the same constituents as when evolved, and causing a partial combustion thereof, the temperature of the resulting gases of which is'not less than about 900 C., to simultaneously cause a cracking of condensable products, and preheating said product to be treated in a fluidised state by a portion of said resulting gases originating from the last mentioned partial combustion of the gases.
5. The method of claim 4, further comprising preheating the mixingair.
References Cited in the file of this patent UNITED STATES PATENTS 1,551,956 Hubmann Sept. 1, 1925 2,131,702 Berry Sept. 27, 1938 2,480,670 Peck Aug. 30, 1949 2,626,234 Barr et a1. Jan. 20, 1953 2,689,787 Ogorzaly et a1. Sept. 21, 1954 2,899,365 Scott Aug. 11, 1959

Claims (1)

  1. 4. A METHOD FOR THE CONTINUOUS CARBONIZATION OF FLUIDIZED COAL FINES COMPRISING FORMING A BED OF A HEATED PRODUCT TO BE TREATED, INTRODUCING AN OXYDIZING FLUID INTO THE BED TO PRODUCE TURBULENCE IN THE BED AND CAUSE A STABILIZED REACTION BY PARTIAL COMBUSTION OF THE SAID PRODUCT, MIXING AIR WITH GASES ORIGINATING FROM SAID REACTION, SAID GASES HAVING ESSENTIALLY THE SAME CONSTITUENTS AS WHEN EVOLVED, AND CAUSING A PARTIAL COMBUSTION THEREOF, THE TEMPERATURE OF THE RESULTING GASES OF WHICH IS NOT LESS THAN ABOUT 900*C., TO SIMULTANEOUSLY CAUSE A CRACKING OF CONDENSABLE PRODUCTS, AND PREHEATING SAID PRODUCT TO BE TREATED IN A FLUIDISED STATE BY A PORTION OF SAID RESULTING GASES ORIGINATING FROM THE LAST MENTIONED PARTIAL COMBUSTION OF THE GASES.
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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3419474A (en) * 1963-06-06 1968-12-31 Peters Werner Method of coking and classifying particulate matter by fluidization
US3436314A (en) * 1964-07-23 1969-04-01 Manuel F Leonor Technique for converting bagasse and other moist plant substances into charcoal
US3595542A (en) * 1967-11-06 1971-07-27 Fawkham Dev Ltd Preheater using downwardly flowing, directly contacting, fluidizing vapors from calcining stage of calcerous material
FR2453888A1 (en) * 1979-04-12 1980-11-07 G Energet Pulverised solid fuel processing - absorbs heavy gums on solid particles by spray cooling
US4468314A (en) * 1982-09-01 1984-08-28 Exxon Research And Engineering Co. Hydropyrolysis of carbonaceous material

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1551956A (en) * 1924-05-22 1925-09-01 American Lurgi Corp Process of distilling wet combustible material
US2131702A (en) * 1936-10-24 1938-09-27 Nat Fuels Corp Coal processing
US2480670A (en) * 1942-05-02 1949-08-30 Standard Oil Dev Co Two-zone fluidized destructive distillation process
US2626234A (en) * 1949-06-11 1953-01-20 Standard Oil Dev Co Heat exchange of fluidized solids with gases and vapors
US2689787A (en) * 1948-12-18 1954-09-21 Standard Oil Dev Co Volatile fuel production and apparatus therefor
US2899365A (en) * 1959-08-11 scott

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2899365A (en) * 1959-08-11 scott
US1551956A (en) * 1924-05-22 1925-09-01 American Lurgi Corp Process of distilling wet combustible material
US2131702A (en) * 1936-10-24 1938-09-27 Nat Fuels Corp Coal processing
US2480670A (en) * 1942-05-02 1949-08-30 Standard Oil Dev Co Two-zone fluidized destructive distillation process
US2689787A (en) * 1948-12-18 1954-09-21 Standard Oil Dev Co Volatile fuel production and apparatus therefor
US2626234A (en) * 1949-06-11 1953-01-20 Standard Oil Dev Co Heat exchange of fluidized solids with gases and vapors

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3419474A (en) * 1963-06-06 1968-12-31 Peters Werner Method of coking and classifying particulate matter by fluidization
US3436314A (en) * 1964-07-23 1969-04-01 Manuel F Leonor Technique for converting bagasse and other moist plant substances into charcoal
US3595542A (en) * 1967-11-06 1971-07-27 Fawkham Dev Ltd Preheater using downwardly flowing, directly contacting, fluidizing vapors from calcining stage of calcerous material
FR2453888A1 (en) * 1979-04-12 1980-11-07 G Energet Pulverised solid fuel processing - absorbs heavy gums on solid particles by spray cooling
US4468314A (en) * 1982-09-01 1984-08-28 Exxon Research And Engineering Co. Hydropyrolysis of carbonaceous material

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