US3419474A - Method of coking and classifying particulate matter by fluidization - Google Patents

Method of coking and classifying particulate matter by fluidization Download PDF

Info

Publication number
US3419474A
US3419474A US381586A US38158664A US3419474A US 3419474 A US3419474 A US 3419474A US 381586 A US381586 A US 381586A US 38158664 A US38158664 A US 38158664A US 3419474 A US3419474 A US 3419474A
Authority
US
United States
Prior art keywords
coking
coke
coal
dross
tube
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US381586A
Other languages
English (en)
Inventor
Peters Werner
Traenckner Kurt-Christian
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.)
KURT CHRISTIAN TRAENCKNER
Original Assignee
Individual
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
Priority claimed from DEB72189A external-priority patent/DE1168455B/de
Priority claimed from DEB73630A external-priority patent/DE1238440B/de
Application filed by Individual filed Critical Individual
Application granted granted Critical
Publication of US3419474A publication Critical patent/US3419474A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
    • 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
    • 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
    • C10B49/16—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 moving solid heat-carriers in divided form
    • C10B49/20—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 moving solid heat-carriers in divided form in dispersed form
    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/06—Methods of shaping, e.g. pelletizing or briquetting
    • C10L5/08—Methods of shaping, e.g. pelletizing or briquetting without the aid of extraneous binders
    • 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

Definitions

  • PETERS ET AL 3,419,474 METHOD oF COKIN@ AND CLASSIFYING PARTICULATE Dec. 31, 196s MATTER BY FLUIDIZATION Flled July 9 1964 INVENTORS /Q me l" /DRJB ATTORNEY United States Patent O 3,419,474 METHOD F COKING AND CLASSIFYING PAR- TICULATE MATTER BY FLUIDIZATION Werner Peters, Langacker 5, Wattenscheid-Hontrop, Germany, and Kurt-Christian Traenckuer, Grosser Schirnkamp 15, Essen-Steele, Germany Filed July 9, 1964, Ser. No. 381,586 Claims priority, application Germany, Sept. 24, 1963, B 73,630; Dec.
  • ABSTRACT 0F THE DISCLOSURE A coking method, comprising the steps of introducing into the lower portion of an elongated upright tubular reaction vessel a suspension in a hot gas of coal particles adapted to be coked, the hot gas serving as substantially the sole source of heat for coking the -coal particles, so as to form inthe reaction vessel a stream consisting of the particles dispersed in hot gas and upwardly passing throughout substantially the entire length of the tubular reaction vessel in such a manner as to cause during the upward passage of the stream through the tubular reaction vessel coking of the coal particles and formation of a hot combustible gas thus converting the upwardly owing stream during passage of the latter through the tubular reaction vessel into a suspension of coked particles in combustible gas, withdrawing the suspension from the upper portion of the tubular reaction vessel, and Separately recovering from the withdrawn suspension the coke and the combustible gas thereof.
  • the present invention relates to a coking method and device and, more particularly, the present invention is concerned with producing coke dross, i.e. coke having a particle size of up to about mm.
  • Coke dross is obtained as a by-product of the conventional coke production due to the abrasive action of the larger coke particles.
  • the commercial demand for coke dross has increased to such an extent that additional coke dross is now produced by grinding of larger coke particles. This process, however, is highly uneconomical.
  • the present invention contemplates a coking method comprising the steps of forming an upwardly flowing stream of a mass of particulate coal adapted to be coked, having a particle size up to about l0 mm. and dispersed in gas having a temperature of at least 200 C. so as to cause during such upward flow of the stream coking of the particulate coal under formation of hot combustible gas, and separately recovering the combustible gas and the thus formed coke.
  • the present invention also includes a coking arrangement comprising, in combination, an elongated upright coking tube, introduction means associated with the lower end of the coking tube for introducing particulate coal into the same, blowing means Iassociated with the lower end of the coking tube for blowing hot air into the same 3,419,474 Patented Dec. 3l, 1968 ice so as to form in the coking tube an upwardly flowing suspension of coal particles in hot air thereby causing in the coking tube coking of the coal particles and formation of combustible gas, withdrawal means associated with the upper end of the coking tube for withdrawing the suspension of coke and combustible gas therefrom, and separating means operatively connected to the withdrawal means for separating the suspension into coke particles and combustible gas.
  • coke dross is produced in Ia simple and economical manner by blowing coal which is adapted to be coked and which has a particle size of up to about 10 mm., by means of preheated air and at the speed of at least about 3 meters per second, in upward direction, through an upwardly, preferably vertically, extending coking tube having a length of at least 3 to 5 meters.
  • a maximum temperature will be reached within the coking tube which will be at least equal to about 750 C.
  • Coke dross and hot combustible gases will be formed in the tube and will leave through the upper end thereof. The thus produced coke dross is then separated from the combustible gases and the latter may be utilized for various purposes.
  • the present invention it is possible to cause degasication of coal up to a particle size of about 10 mm. in a very quick manner and so that a coke dross is formed having approximately the same particle size as the initially introduced coal.
  • the combustible gases formed during the coking process will have, depending on the quality of the starting material, a caloric value of up to about 3,000 kcal. per standard cubic meter.
  • the coal is conveyed through the upright coking tube by means of air blown in to the lower end of the coking tube and preheated to at least 200 C.
  • air it is also possible to replace the air with other gases and particularly to introduce in combination with air or other gases a relatively small proportion of combustible gases into the lower portion of the coking tube.
  • the passage of the coalgas suspension through the coking tube, during which passage the suspension is changed into a suspension of coke in combustible gas, is facilitated by having the interior of the coking tube completely unobstructed.
  • the speed of flow of the gases through the upright coking tube will be adjusted to the particle size of the coal which is to be coked.
  • Relatively small sized coal having a particle size of up to 3 mm. preferably will be blown through the coking tube in a gas stream having a speed of at least about 5 meters per second.
  • Larger size coke particles up to a particle size of about 10 mm. require a correspondingly higher speed of flow of the gas, up to about 30 meters per second.
  • the particulate coal is introduced into the coking tube from below, preferably pneumatically in a manner known per se.
  • the :inner diameter of the coking tube will be preferably between 0.5 meters and 3 meters, most preferably between 0.80 meters and 1.80 meters. It is possible to coke between 20 and 40 metric tons of ⁇ coal per hour in a coking tube having a length of l0 meters and an inner diameter of 1.50 meters.
  • the air-coal ratio should be so chosen that at least 500 standard cubic meters of air are blown into the tube for each metric ton of coal and at most about 1000 standard cubic meters of air should be introduced for each metric ton of coal. Generally, the optimum ratio will be about 700 stand-ard cubic meters of air per metric ton of coal.
  • the temperature within the coking tube may rise -up to about l350 C., whereby either a completely or a partially degaszsed coke dross is produced.
  • any coal may be used which contains at least about 14% of volatile constituents.
  • the coke dross which leaves the coking tube at the upper end thereof can be easily separated not only from the hot stream of combustible gas, but also into several fractions of coke dross diiiering by size.
  • the coke dross leaving the upper end of the coking tube may .be separated into a fraction containing smaller particles of a size, for instance, of up to 5 and into a fraction containing larger particles having a size of between about 5 and 10 mm.
  • the same may be passed through various types of cooling, i.e., heat exchange devices such as fluidized bed coolers, drop coolers or tube coolers.
  • coke dross produced according to the present invention may be used, either hot or after cooling, for mixing with strongly baking or fat coal so as to form a somewhat leaner mixture which is better suitable for subsequent coking.
  • the combustible gas as it emanates from the coking tube and without purification for operating a drying installation for the drying or preheating of the usually moist coking coal.
  • the freshly produced coke dross may be advantageously used as the sintering fuel for the sintering of ore and the like. In this case it is also advisable to charge the sintered belt with the coke dross without prior cooling of the latter in order to utilize the sensible heat of the coke dross.
  • the coke dross produced according to the present invention is used as fuel for the sintering of Ore or the like, it is furthermore advantageous to utilize the lhot combustible gases emanating from the coking tube for the igniting of the coke dross-ore or the like sintering mixture.
  • the separated combustible gases may be used as heating gas, for instance for producing steam.
  • preheated air may be introduced through conduit 2 into heat-insulated coking tube 1, while the finely particulate coal having a particle size of up to l mm. is pneumatically blown into the lower end of coking tube 1 through conduit 3.
  • a mixture of coke dross and of a tar and water-containing combustible waste gas will leave the coking tube.
  • the larger coke dross particles are separated in separator 5 and the smaller coke dross particles in separator while the combustible gas which thus has been freed of coke dross is withdrawn through conduit 4.
  • the larger coke dross particles are cooled while passing through cooler 7, by means of water sprinklers 6 so that coke dross having a temperature of about 150 C. collects in hopper 8 provided with a suitable gate at its lower end from which the coke may be dropped into hopper car 9.
  • the liner coke dross particles will pass from cyclone separator 10 through sluice gate 11 into Water cooler 12 and from there to hopper 13 and eventually into hopper car 14.
  • the heat balance of the method of the present invention is highly favorable.
  • By coking a highly volatile coal about 65% of the calories of the initial coal are retained in the coke dross and 30% can be found in the combustible waste gas, so that the entire caloric loss of the degasification amounts only to about 5%
  • a coking tube of 10 meter length and an inner diameter of 1.5 meters has a capacity such that -generally about 30 tons per hour of gasilame coal, i.e. a fat coal containing between about 32 and 36% of volatile constituents can be degasitied therein.
  • the yield per unit of cross sectional area of the coking tube of the present process is at least about 5 times greater than that obtainable in the conventional iiuidized bed coking process.
  • EXAMPLE l 30 tons of a fat coal containing 38% of volatile constituents and having a particle size of between 0 and 6 mm. are passed together with 23,000 ⁇ standard cubic meters of air preheated to 450 C., at a speed of 15 meters per second through a coking tube having a length of 16 meters and a diameter of 1.40 meters. Thereby, a maximum temperature of between 1000 and 1100 C. will be reached in the coking tube. 14.4 metric tons of coarse coke dross and 4.2 metric tons of iine coke dross are recovered as well as 29,000 standard cubic metersof waste gas having a caloric value of 2,500 kcal. per standard cubic meter. The waste gas passing through conduit 4, without ybeing subjected to purification, is introduced into a heating device, for instance a steam boiler.
  • a heating device for instance a steam boiler.
  • the air which is introduced through conduit 2 has been preheated to 450 C.
  • the air will -be preheated to between 200 and 500 C.
  • EXAMPLE 2 1000 kg. of fat coal containing 25% volatile constituents and having a particle size of between 0 and 3 mm., dispersed in 700 standard cubic meters of air which have been preheated to 350 C. are passed at a speed of iiow of 12 meters per second through a coking tube having a length of 12 meters and a diameter of 1 meter. The temperature in the coking tube reaches between 900 and 1200 C. 720 kg. of coke dross containing 12% volatile constituents and having a temperature of 600 C. are obtained and are mixed while still hot with 600 parts by weight of a briquetting coal having a water content of 15%. The temperature of the thus obtained mixture will be about C. and the water content thereof will be practically nil. The thus formed mixture is excellently suitable to be briquetted in conventional mauner.
  • EXAMPLE 3 1000 kg. of a slightly baking coal containing 18% of volatile constituents and having a particle size of from 0 to 2 mm., are passed together with 550 standard cubic meters of air preheated to 400 C., at a speed of 12 meters per second through a coking tube having a height of 6 meters and a diameter of 80 cm.
  • the maximum degassing temperature reached in the coking tube is about 850 C.
  • EXAMPLE 4 By passing 1000 kg. of a coal containing 45% of volatile constituents and having a particle size of from -8 mm. together with 900 standard cubic meters of air preheated to 400 C. through a coking tube having a diameter of 2.50 meters and a length of 22 meters, 600 kg. of coke dross are obtained.
  • the thus obtained coke dross contains l0% volatile constituents and is mixed with 15 times its own ⁇ weight of a fine iron ore and the thus formed mixture is placed on a sintering belt.
  • the combustible waste gas formed in the coking tube and separated from the coke dross serves in part for operating the ignition stove of the sintering device. Excess waste gas is used for heating purposes, for instance in a steam boiler. In this manner, with a relatively small amount of coke dross, a high quality sintered product is obtained.
  • a coking method comprising the steps of introducing into the lower portion of an elongated upright tubular reaction vessel having a diameter of between about 0.5 and 3 meter a suspension in hot air of coal particles adapted to be coked, said hot air having a temperature of at least 200 C.
  • said upright tubular reaction vessel is an elongated substantially vertical reaction tube having a length ofiat least 3 meters, said coal particles have a size of up to 10 mm., said hot air having a temperature of between about 200 C. and 500 C., and said stream passing through said vertical reaction tube at a speed of at least 3 meters per second.
  • reaction tube has a length of between about 3 and l0 meters, said stream passes therethrough at a speed of between 3 and 30 meters per second, and said preheated air has a temperature of between about 200 and 500 C.
  • a mass consisting of larger and smaller coal particles is pneumatically introduced into the lower portion of said upright tubular reaction vessel together with said hot air so as to form said upwardly passing stream in said tubular reaction vessel 8.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Dispersion Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US381586A 1963-06-06 1964-07-09 Method of coking and classifying particulate matter by fluidization Expired - Lifetime US3419474A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DEB72189A DE1168455B (de) 1963-06-06 1963-06-06 Verfahren zum Betrieb von Sinteranlagen
DEB73630A DE1238440B (de) 1963-06-06 1963-09-24 Verfahren zur Herstellung einer Brikettierkohlenmischung
DEB0074544 1963-12-05

Publications (1)

Publication Number Publication Date
US3419474A true US3419474A (en) 1968-12-31

Family

ID=27209225

Family Applications (1)

Application Number Title Priority Date Filing Date
US381586A Expired - Lifetime US3419474A (en) 1963-06-06 1964-07-09 Method of coking and classifying particulate matter by fluidization

Country Status (5)

Country Link
US (1) US3419474A (de)
BE (1) BE648876A (de)
DE (1) DE1471554A1 (de)
FR (1) FR1397093A (de)
GB (1) GB1028460A (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5123183A (en) * 1989-04-07 1992-06-23 Salomon S.A. Rear-entry ski boot

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2716907B2 (de) * 1977-04-16 1979-08-09 L. & C. Steinmueller Gmbh, 5270 Gummersbach Verwendung von Koksstaub oder Koksgrieß als Aktivkoks
CN109022006B (zh) * 2018-07-19 2022-10-18 山东大学 煤粉粒径分级利用的粉状焦炭/兰炭的生产系统及工艺

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US288550A (en) * 1883-11-13 Ore-separator
US393411A (en) * 1888-11-27 Grain-separator
US1475502A (en) * 1922-06-16 1923-11-27 Manning Refining Equipment Cor Method of revivifying finely-divided fuller's earth, bone char, and the like
US1888372A (en) * 1929-08-06 1932-11-22 Birtley Iron Company Ltd Separation of dry materials
US2339932A (en) * 1941-04-10 1944-01-25 Standard Oil Dev Co Chemical process
US3011953A (en) * 1958-07-02 1961-12-05 Charbonnages De France Method and apparatus for the carbonization of fluidized materials
US3053648A (en) * 1959-10-08 1962-09-11 Battelle Memorial Institute Reduction of iron ore
US3117918A (en) * 1960-09-13 1964-01-14 Consolidation Coal Co Production of low sulfur formcoke
US3140240A (en) * 1960-07-21 1964-07-07 Consolidation Coal Co Process for carbonizing coal
US3150958A (en) * 1958-11-27 1964-09-29 Elektrokemisk As Process for the reduction of metals from oxide

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US288550A (en) * 1883-11-13 Ore-separator
US393411A (en) * 1888-11-27 Grain-separator
US1475502A (en) * 1922-06-16 1923-11-27 Manning Refining Equipment Cor Method of revivifying finely-divided fuller's earth, bone char, and the like
US1888372A (en) * 1929-08-06 1932-11-22 Birtley Iron Company Ltd Separation of dry materials
US2339932A (en) * 1941-04-10 1944-01-25 Standard Oil Dev Co Chemical process
US3011953A (en) * 1958-07-02 1961-12-05 Charbonnages De France Method and apparatus for the carbonization of fluidized materials
US3150958A (en) * 1958-11-27 1964-09-29 Elektrokemisk As Process for the reduction of metals from oxide
US3053648A (en) * 1959-10-08 1962-09-11 Battelle Memorial Institute Reduction of iron ore
US3140240A (en) * 1960-07-21 1964-07-07 Consolidation Coal Co Process for carbonizing coal
US3117918A (en) * 1960-09-13 1964-01-14 Consolidation Coal Co Production of low sulfur formcoke

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5123183A (en) * 1989-04-07 1992-06-23 Salomon S.A. Rear-entry ski boot

Also Published As

Publication number Publication date
BE648876A (de) 1964-12-07
DE1471554A1 (de) 1968-12-12
GB1028460A (en) 1966-05-04
FR1397093A (fr) 1965-04-23

Similar Documents

Publication Publication Date Title
US3047473A (en) Drying, preheating, transferring and carbonizing coal
US3010882A (en) Process of extruding anthracite coal to form a metallurgical coke-like material
US3692505A (en) Fixed bed coal gasification
US3051629A (en) Preparing metallurgical fuel briquets from non-caking coal by preshrinking char
US3206299A (en) Dense-bed, rotary, kiln process and apparatus for pretreatment of a metallurgical charge
US3444048A (en) Continuous coking apparatus
US2772954A (en) Gasification method
US3705086A (en) Coal carbonizing in trickling streams
US4050990A (en) Method and apparatus for producing form coke
US2743217A (en) Distillation process
US2560357A (en) Production of solid fuel agglomerates
US2983653A (en) Apparatus for degasifying finely divided fuels
US2311140A (en) Manufacture of producer gas
US3419474A (en) Method of coking and classifying particulate matter by fluidization
US2701758A (en) Thermal processes
US3184293A (en) Carbonaceous shapes
US2187872A (en) Gas producer for gasifying granular fuels
US3455789A (en) Process for continuous carbonization of coal
US2684897A (en) Smelting of ore, particularly iron ore
US4309197A (en) Method for processing pulverized solid fuel
US3384557A (en) Method of curing of green briquettes by oxidation
US4352720A (en) Process and apparatus for the production of molded metallurgical coke from coal briquettes
US3823073A (en) Calcining coke in vertical kiln
US2815316A (en) Process of treating coal
US2922752A (en) Continuous carbonization process and apparatus