US3419474A - Method of coking and classifying particulate matter by fluidization - Google Patents
Method of coking and classifying particulate matter by fluidization Download PDFInfo
- 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
Links
- 238000004939 coking Methods 0.000 title description 69
- 238000000034 method Methods 0.000 title description 22
- 238000005243 fluidization Methods 0.000 title 1
- 239000013618 particulate matter Substances 0.000 title 1
- 239000000571 coke Substances 0.000 description 58
- 239000003245 coal Substances 0.000 description 47
- 239000002245 particle Substances 0.000 description 43
- 239000007789 gas Substances 0.000 description 34
- 238000006243 chemical reaction Methods 0.000 description 13
- 239000000203 mixture Substances 0.000 description 13
- 239000000725 suspension Substances 0.000 description 11
- 239000000470 constituent Substances 0.000 description 10
- 238000005245 sintering Methods 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- 239000010849 combustible waste Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000007664 blowing Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000007872 degassing Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 240000000736 Amomum maximum Species 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
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.
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- 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)
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)
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)
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)
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 |
-
1963
- 1963-12-05 DE DE19631471554 patent/DE1471554A1/de active Pending
-
1964
- 1964-06-04 FR FR977032A patent/FR1397093A/fr not_active Expired
- 1964-06-05 BE BE648876D patent/BE648876A/xx unknown
- 1964-06-05 GB GB23?4/64D patent/GB1028460A/en not_active Expired
- 1964-07-09 US US381586A patent/US3419474A/en not_active Expired - Lifetime
Patent Citations (10)
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)
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 |
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