US3384557A - Method of curing of green briquettes by oxidation - Google Patents

Method of curing of green briquettes by oxidation Download PDF

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Publication number
US3384557A
US3384557A US384146A US38414664A US3384557A US 3384557 A US3384557 A US 3384557A US 384146 A US384146 A US 384146A US 38414664 A US38414664 A US 38414664A US 3384557 A US3384557 A US 3384557A
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briquettes
reaction zone
heat transfer
solids
curing
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US384146A
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Saller Erik
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FMC Corp
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FMC Corp
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Priority to US384146A priority Critical patent/US3384557A/en
Priority to GB29065/65A priority patent/GB1056467A/en
Priority to ES0315200A priority patent/ES315200A1/es
Priority to DE19651546640 priority patent/DE1546640B1/de
Priority to BE666910A priority patent/BE666910A/xx
Priority to NL656509227A priority patent/NL139768B/xx
Priority to FR25114A priority patent/FR1452705A/fr
Priority to YU1217/65A priority patent/YU31297B/xx
Priority to AT666165A priority patent/AT257536B/de
Priority to OA52136A priority patent/OA01785A/xx
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Publication of US3384557A publication Critical patent/US3384557A/en
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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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/08—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form in the form of briquettes, lumps and the like

Definitions

  • bituminous coal including non-coking coals, of a particle size less than 6 mesh and preferably less than 16 mesh with the average particle size in the range of 40 to 60 mesh, are heated in the presence of oxygen, which may be derived from the coal itself in the case of the so called high oxygen containing coals, i.e., coals having an excess of by weight of oxygen, to a temperature high enough to drive off substantially all moisture but below that at which substantial amounts of tar-forming vapors evolve.
  • oxygen which may be derived from the coal itself in the case of the so called high oxygen containing coals, i.e., coals having an excess of by weight of oxygen, to a temperature high enough to drive off substantially all moisture but below that at which substantial amounts of tar-forming vapors evolve.
  • coal particles from this heat treatment are heated to a higher temperature at which tar-forming vapors are evolved and for a time interval sutlicient to effect polymerization of the heated coal particles and evolution therefrom of substantially all of the tar-forming vapors to produce a char of markedly lower volatile combustible material content than the parent coal and substantially free of tar-forming vapors.
  • This char is heated to a still higher temperature to produce the calcined char particles for blending with the bituminous binder.
  • Typical conditions for producing such calcined char particles from a coking coal is to heat in the first stage to a temperature within the range of from 500 F. to 800 F., in an atmosphere containing from 8% to 20% by volume of oxygen; to further heat the hot coal particles from the first stage to a temperature not exceeding 1200" F. to drive off substantially all tar-forming vapors; and to heat in the third or calcining stage to a temperature within the range of from 1400 F. to 1800 F. for a time interval long enough to produce the desired reduction in the volatile combustible content of the calcined char particles, preferably to not exceeding about 5% by weight on a moisture and ash-free basis.
  • the conditions for the production of the calcined char are to heat the coal particles in the first stage to a temperature within the range of from 250 F. to 500 F. in an atmosphere containing from 1% to 3% by volume of oxygen where the coal treated is not a high oxygen-containing coal (in the treatment of such high oxygen-containing coals, oxygen from an extraneous source need not be introduced).
  • the hot coal particles from the first stage are heated to a temperature not exceeding 1200 F. for a time interval long enough to effect substantially complete removal of tar-forming vapors and the char thus produced heated to a still higher temperature within the range of from 1400 F. to ISO-0 F. to reduce the volatile 3,384,557 Patented May 21, 1968 content to the desired level, preferably to not exceeding about 3% by weight on a moisture and ash-free basis.
  • briquettes from the calcined char thus produced by blending the calcined char with the bituminous binder, desirably in the proportions of from to calcined char to 25% to 10% binder, properly curing the briquettes thus produced and coking the cured briquettes, results in uniform briquettes suitable for metallurgical purposes. These briquettes burn uniformly. When observed, even under relatively lower power of magnification, they are of uniform composition, i.e., as a general rule the carbon derived from the char and that derived from the bituminous binder are indistinguishable.
  • the curing treatment which effects copolymerization of the bituminous binder with the calcined char so that upon subsequent coking a uniform homogeneous briquette is obtained and in which as noted the carbon derived from the bituminous binder and that derived from the char are, for all practical purposes, indistinguishable, is a most important factor in the production of satisfactory briquettes.
  • This curing stage is also important because it imparts to the green (fresh) briquettes the necessary strength to withstand the subsequent coking treatment without excessive loss, i.e., without having an excessive number of the briquettes spall and crumble during the coking.
  • the cured briquettes when properly cured, can be used without subjecting them to a coking treatment before use.
  • cured briquettes of adequate strength are useful in cupola and blast furnaces.
  • the coking of the cured briquettes takes place within the furnace; the temperature conditions in cupola and blast furnaces are such as to effect the coking of the cured briquettes, which are then consumed in effecting the smelting and refining of the charge within the furnace.
  • curing of the green briquettes is effected by heating in an atmosphere containing 2% to 21% by volume of oxygen to a temperature within the range of from 400 F. to 550 F.
  • the presence of oxygen in the curing medium effects the removal of hydrogen from the carbon matrix derived from the calcined char and from the bituminous binder by dehydrogenation thereof.
  • the oxygen promotes copolymerization of the bituminous binder and the char so that upon subsequent coking a uniform briquette is obtained in which the carbon derived from the char and that derived from the binder, for all practical purposes, is indistinguishable.
  • the practice employed was to place the green briquettes in a relatively shallow bed (from about 12" to 18" high) on an .endless grate traveling through an oven maintained at a temperature of from 400 F. to 500 F. while maintaining in the oven an oxygen atmosphere containing about by volume of free oxygen.
  • This shallow grate procedure is objectionable not only because the equipment required is costly and wears out quickly, but also because ofthe limited capacity of a given size installation.
  • the curing time required with this shallow grate procedure are of the order of about 1 to 2 hours.
  • Another object of this invention is to provide such process which is continuous in character and hence of large capacity or throughput.
  • a bed of green briquettes is moved continuously in a downward direction, countercurrent to an upwardly flowing stream of finely divided solid particles having a size not exceeding about 6 mesh, preferably less than 16 mesh, with the average particle size in the range of 40to 60 mesh, which solid particles fiow through the interstices between the downwardly moving briquettes, the reaction zone of the bed is maintained at a temperature within the range of from 400 F. to 550 F., prefereably 450 F.
  • the upwardly flowing stream of finely divided solid particles is dispersed in a stream of air which thus supplies the oxygen for the curing and effects the heat transfer from the mass of briquettes subjected to oxidation to the finely divided solid particles so as to maintain the temperature conditions throughout the reaction zone where the oxidation of the briquettes is effected within a relatively narrow range not exceeding about 60 F. throughout the length of the reaction zone.
  • the rate of flow of the air stream and of the bed of briquettes through the reaction zone is controlled to insure the presence of at least 10% by volume, preferably at least by volume, of free oxygen in the solids free gas in the reaction zone where the briquettes enter this zone, or just above this zone.
  • the finely divided solid particles are withdrawn continuously, cooled and recirculated upwardly through the downwardly moving bed of green briquettes, thus acting to remove the heat of reaction and also to effect etficient heat exchange so as to maintain temperature conditions within the reaction zone within the aforesaid narrow range of not exceeding 60 F. as the briquettes move through this reaction zone.
  • the presence of oxygen during the curing of the green briquettes is essential. Also important is the presence of at least 10% by volume of free oxygen, on a solids free gas basis, where the briquettes enter the reaction zone. Unless at least 10% by volume of free oxygen, on a solids free gas basis, is present where the briquettes enter the reaction zone the oxidative curing of the briquettes does dot proceed rapidly enough to impart sufficient strength to the briquettes to prevent excessive disintegration of the briquettes in their fiow through the reaction zone.
  • the maintenance of the temperature conditions during the curing within the range of from 400 F. to 550 F. is also important. If the temperature is permitted to rise much above 550 F., ignition occurs and the reaction can no longer be controlled, with the result that instead of a curing reaction taking place, the carbon and hydrogen content of the briquette is consumed.
  • the air suspension of finely divided heat transfer material flows through the interstices of the column of briquettes flowing downwardly through the reaction zone giving good heat distribution and enabling control of the temperature within the bed within a relatively narrow range, not exceeding about 60 F.
  • This is effected by fiowing from 1 to 7 pounds, preferably 3 to 5 pounds, of solid heat transfer material per cubic foot of air up through the briquettes and with the flow of this solid heat transfer material at a superficial velocity of from 1 to 15 linear feet per second.
  • the superficial velocity of the solid heat transfer particles should be within the range of from 1 foot per second to 15 feet per second.
  • superficial velocity of the heat transfer solids is meant the velocity of the air stream in the curing column without any resistance therein to the flow of the heat transfer particles in the column, i.e., the bed of briquettes.
  • the velocity through the bed of briquettes with reasonable accurracy hence the definition of the velocity of the heat transfer particles in terms of superficial velocity. If the superficial velocity is below about one foot per second, the heat transfer solids tend to settle out of the air and collect on the briquettes,
  • the residence time of the green briquettes in the bed moving through the reaction zone is dependent on the temperature maintained in the reaction zone. Operating at about 500 F. the minimum residence time is about sixty minutes. At 450 F., somewhat longer residence times would be needed to obtain maximum strength. Longer residence times in excess of about three hours, however, 'add nothing to the quality of the final product. Since such longer residence times adversely affect the economics of the process, they are not recommended.
  • Preferred operation is a residence time of from about 60 to minutes at a temperature of from 450 F. to 500 F. within the reaction zone.
  • the briquettes can enter the curing zone at any desired temperature, preferably at the temperature at which they leave the briquetting operation, which is usually Within the range of from F. to 250 F. They soon reach reaction temperature as they move downwardly through the upper portion of the vessel, just before entering the reaction zone therein, due to the heat emanating from the reaction zone and the exothermic character of the curing reaction. The briquettes are maintained.
  • reaction temperature within the reaction temperature of from 400 F. to 550 F., preferably 450 F. to 500 F., as they pass downwardly through the reaction zone by circulating finely divided solids dispersed in the air stream introduced in the reaction zone and flowing upwardly between the interstices of the briquettes moving downwardly through this reaction zone, these finely divided solids being continuously withdrawn from the upper portion of the reaction zone, cooled and the cooled solids returned to the lower portion, thus removing the heat of reaction from the reaction zone and maintaining the latter within the temperature range of from 400 F. to 550 F. and within a temperature gradient of not exceeding about 60 F. from the inlet to the exit end of the reaction zone.
  • the briquettes are introduced into the reaction zone at a temperature near that at the exit end of the reaction zone where the curing is effected. This can be accomplished by flowing the briquettes through a mass of the finely divided heat transfer material 'after the latter leaves the reaction zone to effect partial cooling of the hot heat transfer particles and simultaneous heating of the briquettes.
  • Preferred heat transfer solids are the calcined char particles employed in producing the briquettes.
  • the advantages of using these char particles are that they prevent contamination of the briquette product, the char particles are readily available as part of the overall process, and char particles which are converted into fines and separated from the heat transfer particles can be utilized in the process by introducing same into the briquetting operation as part of the char feed, thus eventually contributing to the yield of coked briquettes from the process.
  • the invention is not limited to the use of calcined char particles as the heat transfer material. Instead of char, sand or minerals crushed to a particle size, as, for example, in a hammer-mill having screens passing inch particles, can be used.
  • the rate of flow of the briquettes downwardly countercurrent to the upwardly flowing heat transfer solid particles suspended in the air stream is dependent upon (1) the size of the vessel, and (2) the height of the reaction or curing zone chosen to give a selected residence time within the curing zone Within the range of from 60 to 180 minutes; this rate of flow must be such as to leave at least preferably at least by volume of free oxygen, on a solids free gas basis, in the gas stream at the point where the briquettes enter the curing zone.
  • the height and cross-section of the curing zone can be chosen to give any desired capacity within limits.
  • green briquettes as produced in the briquetting equipment are transported to the storage hopper 10. From this hopper 10 the green briquettes flow down through conduit 11 at a given and desired rate into the upper portion 12 of a fluidized bed of particulate heat transfer solids 13 reaching the interface 14 of the downwardly moving bed of briquettes 15.
  • Such feed of the briquettes from the storage hopper 10 through the conduit 11 can be effected by a vibratory feed mechanism (not shown) or other suitable mechanism for effecting the feed of the briquettes at a controlled rate.
  • the interface 14 between the particulate heat transfer solids 13 and the downwardly moving bed of briquettes 15 is controlled to be positioned at about the outlet 16 for the spent heat transfer solids 13. This outlet 16 forms the inlet or head of conduit 17 leading into the cooler vessel 41.
  • the green briquettes move down through the reaction zone 19, the extent of which is indicated by the arrows on the drawing. From the reaction zone 19 the cured briquettes continue downward by gravity past the distributing cone 21 into the exit section 22.
  • the latter comprises a lock hopper system 26 which consists of three slide valves 27, 28 and 29 operated in timed relation to permit flow of briquettes through the lock hopper system while maintaining the exit section 22 sealed.
  • the cured briquettes pass out of valve 29 onto a conveyor belt 31 where they are transported to a vibrating screen 32 for the purposes of the removal of pieces of briquettes and particles of heat transfer material, in the embodiment illustrated calcined char, which exit through valve 29.
  • the screenings are discharged from the vibrating screen 32 to chute 33 from which they are returned to the feed stock for the formation of the green briquettes.
  • the screened briquettes are discharged from the vibrating screen 32 onto a conveyor 34 which moves them to transport container 35 for transport to the locale of intended use or for further processing, e.g., feed to the coker.
  • the heat transfer material in the preferred embodiment calcined char, of the desired particle size, not exceeding about 6 mesh, preferably less than 16 mesh, is stored in hopper 36 and fed therefrom by means of a vibrating screen or other suitable feed mechanism into a conduit 37 leading into the disengaging space 38 of the reaction vessel shown in the drawing.
  • a vibrating screen or other suitable feed mechanism In the disengaging space 38 they mix with the gases which are heated by passage through the reaction zone and have been disengaged of most of the heat transfer solids. These gases are in a turbulent state in the disengaging space of chamber 38. Feed of the heat transfer material through these gases effects cooling of the gases with consequent heating of the incoming heat transfer solids fed into the disengaging chamber 38 from storage hopper 36.
  • the heat transfer material moves down in a dense phase by gravity through conduit 17 which is screened at its inlet 16 in order to prevent the flow of briquettes into conduit 17.
  • the heat transfer solids 13 exiting through the conduit 17 pass in a dense phase by gravity into the fluid bed 41 maintained in vessel 42.
  • the heat transfer solids are cooled by an incoming stream of cold air introduced through line 43 or by circulating a cooling medium through a jacket (not shown) surrounding vessel 42 to cool the contents of this vessel.
  • 44 is a meter for metering the air supplied through line 43.
  • the heat transfer material can be cooled by other procedures, for example, by direct water injection into the circulating stream of heat transfer material at a point in its circulation after leaving the reaction zone to remove enough of the heat of the curing reaction to maintain the reaction zone 19 within the range of 400 F. to 550 F.
  • the heat transfer solids are thus picked up by the air stream supplied through line 43 and conveyed through conduit 47 into the distribution chamber 48 where the suspension of heat transfer solids is dispersed in the annular conical chamber constituting the distribution chamber 48 and flow upward through the downwardly moving bed of briquettes into the disengaging chamber 38.
  • the heat transfer solids, dispersed in the air stream flowing upwardly and enveloping the downwardly moving bed of briquettes are cycled through the reaction zone 19 removing the heat of reaction, maintaining the briquettes within the reaction zone within a narrow temperature range not exceeding about 60 F., and maintaining a free oxygen concentration of at least 10% by volume, on a solids free basis Where the green briquettes enter the curing zone.
  • Cold air is introduced through line 54 provided with a meter 55.
  • the volume of air introduced through line 54 plus that introduced through line 43 controls the loading of the heat transfer solids in the air stream passing through the reaction zone 19, i.e., pounds of heat transfer solids per cubic foot of air passed through the reaction zone 19.
  • the volume of air introduced through line 43 controls the rate of recycle of heat transfer solids through the reaction zone 19, i.e., pounds of solids per minute passed through reaction zone 19.
  • the mixture of fluidizing gas including the reaction gases formed in the reaction zone and the heat transfer solids move upwardly through the bed of briquettes at a rate so designed that for each unit passage of briquettes through the reaction zone 19, about 10 passes of the heat transfer solids through the reaction zone 19 are effected.
  • the number of recycles of heat transfer solids per single pass of briquettes through the reaction zone 19 is of the order of 10 to 1.
  • the disengaging space 38 aids in effecting separation of the gases leaving the reaction zone 19 from the heat transfer solids by the cyclone separator 57.
  • the gases thus separated in the cyclone separator 57 enter the condenser 58 where condensables such as tars are condensed.
  • the condenser 58 can be in the form of the well known direct scrubber Where the gases are scrubbed by a suitable aqueous medium, e.g., water, to condense the condensables in the gas stream. Tars so condensed are removed through line 59. Liquor is decanted from the tars and removed through line 61. Clean gases exit through line 62 and flow through meter 63 from which they can be passed to storage for use, or otherwise disposed of, for example, by venting to the atmosphere.
  • the preheating of the air introduced through line 54 is discontinued and air at atmospheric temperature introduced at this point.
  • the curing reaction is maintained by the heat generated in the reaction zone 19. This heat is more than suflicient to heat the incoming air and the down-flowing bed of briquettes as well as the heat transfer solids flowing upwardly through the down-flowing bed of briquettes.
  • reaction zone 19 heat must be removed from the reaction zone 19 to maintain the temperature therein within the desired range of from 400 F. to 500 F, preferably 450 F. to 500 F. Also, once steady state operation is reached, the amount of heat transfer solids supplied to reaction zone 19 from hopper 36 is the amount required to replace the solids exiting through valve 29.
  • the cured briquettes produced in accordance with this invention have sufficient strength for use in cupola and blast furnaces. When so used coking of the briquettes takes place in the cnpola and blast furnaces; the cured and uncoked briquettes are sumeiently strong to provide adequate support for the burden and this without excessive crumbling so as to plug up the charge in the furnace.
  • the cured briquettes in the uncoked state can also be used as a smokeless fuel.
  • the example was carried out in equipment of the type shown in the drawing.
  • the briquettes were supplied to storage hopper 10 at a temperature of 80 F.
  • the green briquettes contained 81.9% calcined char and 18.1% bituminous binder, which was a tar binder obtained from the carbonization of the coal (Elkol coal) employed in forming the calcined char.
  • Elkol coal is a sub-bituminous grade B coal, mined at Kemmerer, Wyoming, having an approximate fixedcarbon weight percent on a dry basis of 53.2%; volatile matter content on a weight percent dry basis of about 42.7%; and an approximate elemental analysis on a weight percent dry basis as follows: carbon 70.8; hydrogen 5.2; oxygen 18.8; nitrogen 0.9; sulfur 0.8; and ash 3.4.
  • This example involved a run of approximately 38 hours duration during which 9100 pounds of green briquettes were passed through the reaction zone 19.
  • the briquettes introduced into the reaction vessel had a size of 1 /8 x x A.
  • the exiting briquettes, i.e., the cured briquettes, were dimensioned 1% x /3 x A, the same as the green briquettes introduced into the reaction vessel.
  • the calcined char employed as the heat transfer solids had the following mesh analysis:
  • Air was introduced just below the annular distributor 48 through lines 43 and 54. Total air flow was 60 s.c.f.m. and the superficial velocity in the reaction zone 19 was 1.76 feet per second.
  • the volumetric composition of the exit gas leaving the top of the unit was 15.6% 0 1.8% CO 0.5% CO and 82.1% N (by difference) on a dry and solid-free basis.
  • the calcined char particles were circulated upward through the reaction zone 19 at a rate of 1944 pounds per hour, equivalent to about 8.2 pounds of calcined char per pound of green briquettes.
  • the gas flowing through the reaction zone contained about 0.3 pounds of calcined char per cubic foot.
  • the temperature at the top of the reaction zone 19 during steady state operation was 430 F.; at the exit end just above the annular distributor 48 the temperature was 400 F.; and the temperature at the approximate middle of the reaction zone was 460 F.
  • the vessel 42 serves to remove the excess heat generated in the reaction zone and thereby provides a convenient way of controlling temperature in the reaction zone.
  • the cured briquettes thus produced were of excellent quality. Their resistance to crushing after coking was approximately 30% greater than coked briquettes produced from the same green briquettes but cured on an endless grate passing through an oven in which an atmosphere containing from 4% to 5% by volume of oxygen was maintained by the introduction of air and recycle of reaction gases through the grate.
  • the present invention provides an economically attractive process of curing green briquettes constituted of calcined char derived from coal and a bituminous binder in which air is employed as a medium for supplying the oxygen required for the curing and in which green briquettes are passed through the curing zone in a bed of any desired capacity, thus enabling the curing to be effected with large throughputs of the briquettes.
  • the residence time for the briquettes in the curing zone is relatively short and the process is continuous in character and hence the equipment required for the practice of the process can be tailored to meet the requirements of commercial installations where the capacity must be relatively large.
  • briquettes is used herein in a broad sense and includes compressed blends of char and binder in all forms including extrusions, pellets and other shapes.
  • the process of curing green briquettes consisting essentially of calcined char derived from coal and a bituminous binder, which process comprises continuously passing a bed of green briquettes downwardly through a reaction zone; continuously supplying green briquettes to the upper portion of said bed; continuously introducing a stream of air having heat transfer solid particles dispersed therein in the neighborhood of the exit end of said reaction zone and flowing the said stream of air and heat transfer particles upwardly through said reaction zone countercurrent to the down-flowing bed of briquettes with the stream of heat transfer solids enveloping the briquettes in the down-flowing bed, the rate of flow of the bed of briquettes downwardly and the rate of flow of 3 the stream of air having the heat transfer solids dispersed therein upwardly being controlled to provide in the portion of the reaction zone where the green briquettes enters at least 10% by volume of free oxygen, on a solids free basis; continuously withdrawing heat transfer solids from an upper portion of said reaction zone, cooling the solids thus

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Working-Up Tar And Pitch (AREA)
US384146A 1964-07-21 1964-07-21 Method of curing of green briquettes by oxidation Expired - Lifetime US3384557A (en)

Priority Applications (10)

Application Number Priority Date Filing Date Title
US384146A US3384557A (en) 1964-07-21 1964-07-21 Method of curing of green briquettes by oxidation
GB29065/65A GB1056467A (en) 1964-07-21 1965-07-08 Curing of green briquettes
ES0315200A ES315200A1 (es) 1964-07-21 1965-07-10 Un procedimiento para curar briquetas crudas de carbon calcinado y un aglutinante bituminoso.
BE666910A BE666910A (de) 1964-07-21 1965-07-14
DE19651546640 DE1546640B1 (de) 1964-07-21 1965-07-14 Verfahren zum Haerten von Briketts
NL656509227A NL139768B (nl) 1964-07-21 1965-07-16 Continue werkwijze voor het harden van groene briketten.
FR25114A FR1452705A (fr) 1964-07-21 1965-07-19 Précuisson de briquettes crues
YU1217/65A YU31297B (en) 1964-07-21 1965-07-19 Postupak za oplemenjivanje briketa uglja i vezivnog materijala
AT666165A AT257536B (de) 1964-07-21 1965-07-20 Verfahren zum Härten von grünen Briketts
OA52136A OA01785A (fr) 1964-07-21 1965-08-04 Précuisson de briquettes crues.

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US384146A US3384557A (en) 1964-07-21 1964-07-21 Method of curing of green briquettes by oxidation

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US3384557A true US3384557A (en) 1968-05-21

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US (1) US3384557A (de)
AT (1) AT257536B (de)
BE (1) BE666910A (de)
DE (1) DE1546640B1 (de)
ES (1) ES315200A1 (de)
GB (1) GB1056467A (de)
NL (1) NL139768B (de)
YU (1) YU31297B (de)

Cited By (8)

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US3462850A (en) * 1966-08-16 1969-08-26 Nat Gypsum Co Heat exchanger
US3499834A (en) * 1967-02-16 1970-03-10 Phillips Petroleum Co Retorting of hydrocarbonaceous solids
US3914876A (en) * 1973-02-22 1975-10-28 Broken Hill Pty Co Ltd Fluidized bed apparatus
US3918929A (en) * 1972-09-26 1975-11-11 Metallgesellschaft Ag Process for post-treating hot briquettes and the like
US4085707A (en) * 1975-02-14 1978-04-25 Exxon Research & Engineering Co. Combustion or part-combustion in fluidized beds
US4234387A (en) * 1978-04-28 1980-11-18 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Energy, Mines And Resources Coking poor coking coals and hydrocracked tar sand bitumen binder
US20100059205A1 (en) * 2002-04-29 2010-03-11 Kauppila Richard W Cooling arrangement for conveyors and other applications
US20150175891A1 (en) * 2012-07-20 2015-06-25 Nippon Steel & Sumitomo Metal Corporation Coal reforming method and coal reforming apparatus

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US2776935A (en) * 1955-06-29 1957-01-08 Exxon Research Engineering Co Heat treating fluid coke compactions
US3018226A (en) * 1960-10-07 1962-01-23 Consolidation Coal Co Method for preparing coked briquets from caking coals
US3051629A (en) * 1958-07-07 1962-08-28 Consolidation Coal Co Preparing metallurgical fuel briquets from non-caking coal by preshrinking char
US3117064A (en) * 1961-07-03 1964-01-07 Consolidation Coal Co Shock heater
US3117918A (en) * 1960-09-13 1964-01-14 Consolidation Coal Co Production of low sulfur formcoke
US3140242A (en) * 1960-08-03 1964-07-07 Fmc Corp Processes for producing carbonaceous materials from high oxygen coals
US3140985A (en) * 1959-09-26 1964-07-14 Metallgesellschaft Ag Method of oxidation hardening of briquettes
US3172823A (en) * 1965-03-09 Process for hardening carbonaceous briquettes

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FR649771A (fr) * 1927-01-31 1928-12-27 Procédé de traitement thermique des agglomérés
DE1105382B (de) * 1952-10-20 1961-04-27 Houilleres Bassin Du Nord Verfahren und Vorrichtung zur Rauchbeseitigung und Verfestigung von Briketts
US2871004A (en) * 1956-02-29 1959-01-27 Consolidation Coal Co Process for heat treating heat sensitive solid particles
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US8579014B2 (en) * 2002-04-29 2013-11-12 Richard W. Kauppila Cooling arrangement for conveyors and other applications
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US9309465B2 (en) * 2012-07-20 2016-04-12 Nippon Steel & Sumitomo Metal Corporation Coal reforming method and coal reforming apparatus

Also Published As

Publication number Publication date
NL139768B (nl) 1973-09-17
AT257536B (de) 1967-10-10
NL6509227A (de) 1966-01-24
YU31297B (en) 1973-04-30
BE666910A (de) 1966-01-14
GB1056467A (en) 1967-01-25
ES315200A1 (es) 1965-12-01
DE1546640B1 (de) 1970-12-03

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