US3401089A - Process for agglomerating carbonaceous materials - Google Patents

Process for agglomerating carbonaceous materials Download PDF

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Publication number
US3401089A
US3401089A US436864A US43686465A US3401089A US 3401089 A US3401089 A US 3401089A US 436864 A US436864 A US 436864A US 43686465 A US43686465 A US 43686465A US 3401089 A US3401089 A US 3401089A
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agglomerates
finely divided
fraction
particles
coal
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US436864A
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Robert J Friedrich
Gorin Everett
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Consolidation Coal Co
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Consolidation Coal Co
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Priority to US436864A priority Critical patent/US3401089A/en
Priority to GB8406/66A priority patent/GB1131433A/en
Priority to DE1571643A priority patent/DE1571643B2/de
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
    • B01J2/12—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic in rotating drums
    • 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
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin

Definitions

  • This invention relates to a process [for agglomerating discrete carbonaceous particles in a tumbling zone of a rotating retort and more particularly to a process for recycling a portion of the agglomerate product to the tumbling zone of the retort for agglomeration with other discrete carbonaceous particles.
  • United States Patent 3,073,751 entitled, A Method of Making Formcoke, and assigned to the assignee of this invention, discloses a process for making formcoke from a cak-ing coal.
  • particulate bituminous coal and finely divided char (the solid carbonaceous residue of coal which has been distilled between 800 and 1400" F.) are introduced into a tumbling zone of a rotating retort.
  • Pitch may also be added to the tumbling zone of the rotating retort with the coal and char to serve as an additonal binder and to increase the yield of the formcoke.
  • Suitable relative proportions of the constituents introduced into the retort are: 30-60 parts by weight caking coal, 40-65 parts by weight char, and -20 parts by weight pitch.
  • the temperature within the retort is maintained in the range of between 750 and 825 F.
  • the desired temperature of the mixture in the retort is maintained under essentially adiabatic conditons, that is, the raw materials are preheated before they are introduced into the tumbling zone of the rotating retort to supply as sensible heat substantial-1y all the heat required to achieve the desired temperature in the tumbling zone.
  • the retort is rotated to effect tumbling and intimate mixing of the solids.
  • the residence time of the carbonaceous solids in the retort is generally about -40 minutes.
  • the hot green agglomerates are recovered from the retort and thereafter calcined at an elevated temperature, e.g. between 1400-1900 F. with a preferred range of between 1550-1800 F.
  • the calcined agglomerate is the product formcoke that has the density, strength and abrasion resistance of conventional blast furnace coke and, in fact, the strength is generally superior to that of conventional coke.
  • the formcoke For use as a metallurgical coke in conventional blast furnaces, it is desirable that the formcoke have a size no greater than 3" and preferably between A" and 2". The narrowest possible range of sizes is preferred but a size range between and 2 is satisfactory.
  • the raw or green agglomeates recovered from the retort have a spectrum of sizes and the agglomerates of desirable size are separated from the undersize and oversize agglomerates and calcined at an elevated temperature to provide a product f-ormcoke having the desired size range. economiesally, it is highly desirable to recycle the undersize and oversize green agglomerates to the tumbling zone of the retort as a portion of the feed material.
  • agglomerates are formed in the tumbling zone of a rotary retort in the following manner.
  • the particulate constituents are intimately mixed in the tumbling zone by the rotation of the rotary retort during the initial stage of agglomerate formation and form a loosely coherent plastic mass that breaks up into relatively fine plastic particles.
  • the plastic particles during continued tumbling unite to form larger particles or seed particles by a snowball-ing type of mechanism. As the seed particles roll down the inclined top surface of the bed formed in the retort, the fine plastic particles adhere to the seed particles and cause a continued growth of the seed particles.
  • the growth process continues until the coal carbonizes sufliciently to eliminate adhesion and the binder loses its plasticity as a result of temperature and residence time.
  • the agglomerates then rigidity and no further agglomerate growth takes place.
  • the agglomerate product recovered from the retort is a homogeneous carbonized admixture of the constituents fed to the retort.
  • the coal and pitch portion of the feed material is subjected to carbonizing temperatures during the tumbling process so that the agglomerate product is similar in many respects to the discrete particulate char formed by low temperture carbonization.
  • the agglomerate product recycled to the tumbling zone of the rotary retort was comminuted to substantially the same size as the other constituents fed to the rotary retort as for example to a size capable of passing through a screen having 4" openings, the recycled agglomerate product would participate in the agglomeration process and the recycled agglomerate product would assimilate with the other constituents and grow or agglomerate to form the desired homogeneous agglomerate.
  • the principal object of this invention is to provide a process for treating the offsize agglomerate product so that it will participate with other discrete carbonaceous particles in the tumbling zone of a rotating retort to form homogeneous agglomerates suitable for calcining into formcoke of desired strength and density.
  • Another object of this invention is to provide a process for agglomerating discrete carbonaceous particles that also includes as a constituent particles of the agglomerate product previously formed in the tumbling zone of a rotating retort.
  • Another object of this invention is to provide a method for making agglomerates from discrete carbonaceous particles which includes comminuting the offsize agglomerate product to substantially the same size as the other particulate carbonaceous constituents, and introducing the comminuted agglomerate product into the tumbling zone of the rotating retort for assimilation with the other particulate carbonaceous constituents.
  • finely divided caking bituminous coal is introduced into a comminuting device where it is reduced to a size consisting of, for example, 14 mesh x 0 Tyler standard screen.
  • the comminuted coal particles are fed through a conduit 12 to a coal drier or preheater 14 where the coal particles are subjected to a temperature of about 600 F. by means of a hot gas supplied through conduit 16.
  • the vapors are withdrawn from the coal drier 14 through outlet 18.
  • a stream of preheated coal is withdrawn from the coal drier or preheater 14 through the conduit 20.
  • a portion of the preheated coal is conveyed through branch conduit 22 to a low temperature carbonizer 24.
  • the remaining preheated coal is supplied through conduit to the tumbling zone of a rotating retort 26.
  • the raw coal can be comminuted to a size capable of passing through a screen having A openings, hereinafter defined as a A" x 0 size, and conveyed to the coal drier 14.
  • the coal particles can be separated into two different sized fractions; the larger sized fraction is retained on a 14 mesh Tyler standard screen and has a spectrum of sizes between A" and 14 mesh, and the smaller sized fraction, i.e. the fraction passing through the 14 mesh Tyler standard screen (14 mesh x 0) is conveyed through conduit 22 to the carbonizer 24.
  • the coal particles in carbonizer 24 are heated to a temperature of about 900 F., preferably in a dense phase fluidized bed.
  • the operation of such carbonization zone is well known and does not form an essential part of this invention except to the extent that the char so produced in a fluidized bed has particularly desirable properties as a constituent of formcoke.
  • the tar vapors evolved in the carbonizer 24 are conducted through a conduit 28 to a condenser 30.
  • Other tar vapors evolved in other portions of the process may also be conducted through conduit 28 to condenser 30 where the noncondensable gases are recovered through conduit 32 and the tar condensate is recovered through conduit 34.
  • the tar is fractioned in a fractionator 36 and a distillate fraction is recovered through conduit 38 and a pitch fraction is recovered through conduit 40.
  • the pitch fraction is conveyed through conduit 40 to the rotating retort 26, as later described.
  • Air is supplied to the carbonizer 24 through conduits 42 and 44 and the hot char is withdrawn from the carbonizer 24 through conduit 46 and introduced into a preheater 48 where the char is heated to a temperature of about 1100 F. by any suitable means. Heat may be supplied by partial combustion of the char within the preheater vessel 48. The particulate carbonaceous material, heated to about 1100 F. is then conveyed through conduit 50 to the rotating retort 26 and admixed in the tumbling zone of the rotating retort 26 with the preheated coal particles supplied through conduit 20 and the pitch supplied through conduit 40. Means may also be provided to preheat the pitch to a temperature of about 700 F.
  • the preheat temperatures for the coal, char and pitch 4 a are suitably adjusted in accordance with the relativ proportions of the three ingredients to yield the desired average temperature of the admixture which may be between about 725" F. and 825 F. depending on the characteristics of the feed material.
  • the atmosphere in the retort should be nonoxidizing and any air employed in the preheater should be completely consumed.
  • the retort 26 has an enclosure 52 surrounding the discharge end thereof so that the agglomeration within the retort 26 is accomplished under substantially nonoxidative conditions.
  • the agglomerate product withdrawn from the retort 26 is classified or screened into three fractions, namely an oversize fraction wherein all agglomerates have a size larger than 2%", an undersize fraction wherein all agglomerates have a size smaller than /8", and an intermediate desired size fraction wherein all agglomerates have a size smaller than 2%" and larger than 78'.
  • the agglomerates are classified into the three fractions by discharging the agglomerate product from the retort 26 onto a first screen 54 which has 2%" openings.
  • the oversized fraction i.e. +2 4 remains on screen 54.
  • the desired fraction i.e. 2 /4" x /8" and the undersized fraction, i.e. 'Vs"
  • the screen 56 has /s" openings and the desired fraction, i.e. 2% x Vs", remains on screen 56 and the undersized fraction, i.e. 'Ve, passes through the openings in screen 56.
  • the desired fraction (2% x is conveyed from screen 56 by a suitable conveying device schematically illustrated at 60 to a lock hopper 62.
  • the agglomerates are conveyed from the lock hopper 62 to a calciner 64 that is adapted to operate under a pressure of between 0 and 300 p.s.i. and at a temperature of between 1400 and 1900 F.
  • a hot gas preferably a reducing gas, is introduced into the calciner 64 through a conduit 66 and passes upwardly therethrough in countercurrent heat exchange relation to the downwardly moving stream of agglomerates.
  • the rate of heating is regulated to produce strong formcoke.
  • the operation of the calciner is well known in the art and does not form an essential part of this invention.
  • the agglomerates experience about a 12 /2 linear shrinkage in the calciner 64 and the calcined formcoke i.e. the product formcoke, withdrawn from calciner 64 through conduit 68 has a spectrum of sizes between 2" and
  • the oversized agglomerate fraction (+2 A) remaining on screen 54 and the undersized agglomerate fraction passing through screen 56 are both discharged onto the conveyor belt 58 and conveyed to a crusher or comminuting device 70 where both fractions are com minuted to a size capable of passing through a screen having A" openings.
  • the comminuted offsized agglomerates have a size spectrum consisting of particles having a size smaller than 4" (MW x 0).
  • the comminuted agglomerate product having a size of A" X 0 is conveyed from the crusher 70 through conduit 72 to the char preheater 48 where the comminuted agglomerate product is admixed with the char from the carbonizer 24 and heated to a temperature of about 1100 F.
  • the offsized agglomerates are ground to a size spectrum consisting of particles having a size smaller than 8 mesh (8 m. X 0) so that the offsized agglomerates and the char from carbonizer 24 will both fluidize in the preheater 48.
  • the admixture of char and comminuted agglomerate product is conveyed through conduit 50 to the retort 26.
  • the oversized and undersized agglomerate product comprised between 2040% of the product recovered from the retort 26.
  • Table I illustrates the product size of three typical runs where a caking bituminous coal from the Pittsburgh seam and a char obtained by the distillation of a caking bituminous coal, likewise from the Pittsburgh seam, were used.
  • the total weight percent of the desired size X 2" in Run #1 was 61.2 weight percent of the total formcoke product.
  • Run #3 78.2 Weight percent of the formcoke product had the desired size spectrum.
  • the oversize fraction of Run #1 consisted of 16 weight percent and 22.8 Weight percent of the formcoke product was the undersized f-raction.
  • the oxersize fraction consisted of 3 weight percent of the total formcoke prodof the rotary retort. It is further apparent, from Table II, as illustrated in Run #5, that a substantial portion of the agglomerates having a size between A and /2" does not participate in the agglomeration.
  • Table III illustrates the product formcoke size of three typical runs where bituminous coal, char obtained by the distillation of a caking bituminous coal and recycled agglomerate product were agglomerated in the tumbling zone of a rotary retort under substantially the same conditions as Runs #4, #5 and #6 of Table II and thereafter calcined.
  • a formcoke product may be produced having the desired size consist from constituents including recycled agglomerate product.
  • a bituminous coal was neutron irradiated at the Brookhaven laboratories and had a radioactivity of .2 millicurie/gram.
  • a char having a radioactivity of .2 millicurie/ gram was formed from the irradiated coal particles and admixed with other bituminous coal in a tumbling zone of a rotary retort to form an agglomerate product.
  • the undersized fraction of the irradiated agglomerates was furtherseparated into three fractionsflfit x /s", /2" x /4", and x /2".
  • Three runs, indicated as Runs #4, #5 and #6 in Table II, were made in a manner substantially the same as the process described.
  • Run #7 The desirable size fraction of Run #7 consisted of 69.9 weight percent of the formcoke product.
  • the oversize fraction was 25.2 weight percent and the undersize fraction was 2.8 weight percent.
  • Runs #8 and #9 the 40 desired fraction consisted of 82 weight percent and 72.1
  • Runs #7, #8 and #9 illustrate that suitable percentages of the formc-oke product having the desired size fraction may be obtained if the size of the recycled agglomerate product is controlled.
  • the herein described process may also be used in making a formcoke product from a noncaking or weakly caking coal.
  • a sufficient amount of binder such as tar or the like must be used so that the discrete carbonaceous particles will agglomerate in the retort.
  • the agglomerate product produced in the rotary retort is similar in many respects to the char product obtained by the low temperature carbonization of coal. Where it is desirable to obtain a formcoke product that has a narrow size spectrum, the char formed by the low temperature carbonization of coal can be eliminated as a constituent.
  • the agglomerate product, comminuted as described in the above process can be substituted for the .low temperature char. In this process the agglomerate product is screened to relatively narrow size fractions so that about 60% of the agglomerate product is considered offsize product and comminuted to substantially the same size spectrum as the coal particles and then recycled to the rotary retort.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Materials Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
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US436864A 1965-03-03 1965-03-03 Process for agglomerating carbonaceous materials Expired - Lifetime US3401089A (en)

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Application Number Priority Date Filing Date Title
US436864A US3401089A (en) 1965-03-03 1965-03-03 Process for agglomerating carbonaceous materials
GB8406/66A GB1131433A (en) 1965-03-03 1966-02-25 Process for agglomerating carbonaceous materials
DE1571643A DE1571643B2 (de) 1965-03-03 1966-03-02 Verfahren und Vorrichtung zur Herstellung von Formkoks

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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3946098A (en) * 1972-12-11 1976-03-23 Metallurgical Processes Ltd. Preparation of feed material for a blast furnace
US4030982A (en) * 1975-07-10 1977-06-21 Consolidation Coal Company Process of making formcoke from non-caking or weakly caking coals
US4104129A (en) * 1973-10-26 1978-08-01 United States Steel Corporation Low temperature carbonization and desulfurization of coal under elevated pressures
US4148692A (en) * 1977-08-26 1979-04-10 Bethlehem Steel Corporation Process for producing low reactivity calcined coke agglomerates
US4159905A (en) * 1970-12-08 1979-07-03 Bergwerksverband Gmbh Method of manufacturing green hot briquettes from fine coal for use in shaft furnaces
US4221570A (en) * 1979-04-16 1980-09-09 Continental Oil Company Method and apparatus for producing hardened carbonaceous agglomerates
US4278447A (en) * 1979-11-16 1981-07-14 Conoco, Inc. Methods for producing feedstock for a fixed bed gasifier from finely-divided coal
US4314900A (en) * 1980-05-07 1982-02-09 Conoco Inc. Method for producing distillable hydrocarbonaceous fuels and carbonaceous agglomerates from a heavy crude oil
US4388152A (en) * 1980-08-04 1983-06-14 Conoco Inc. Process for producing blast furnace grade coke, a distillable product and fuel gases from a heavy, high sulfur, crude oil
US4410472A (en) * 1982-01-15 1983-10-18 Aluminum Company Of America Method for making spherical binderless pellets
US4473464A (en) * 1980-05-07 1984-09-25 Conoco Inc. Method for producing distillable hydrocarbonaceous fuels and carbonaceous agglomerates from a heavy crude oil
US4631156A (en) * 1984-07-27 1986-12-23 Bofors Nobel, Inc. System and method of particulating 4,4' methylenebis (2-chloroaniline)
US5071515A (en) * 1987-03-09 1991-12-10 Conoco Inc. Method for improving the density and crush resistance of coke
WO1998027186A1 (en) * 1996-12-18 1998-06-25 Minpro Australia N.L. Coal processing method
US20080149471A1 (en) * 2006-12-26 2008-06-26 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US9045693B2 (en) 2006-12-26 2015-06-02 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US9446975B2 (en) 2011-10-21 2016-09-20 Therma-Flite, Inc. Gasifying system and method

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2511901A (en) * 1950-06-20 Agglomeration of carbon black
US2699381A (en) * 1953-08-28 1955-01-11 Phillips Petroleum Co Oil pelleting of carbon black
US2872300A (en) * 1954-10-18 1959-02-03 Phillips Petroleum Co Process and apparatus for simultaneously pelleting powdered materials and classifying same
US2892689A (en) * 1954-06-14 1959-06-30 Phillips Petroleum Co Process and apparatus for classifying particulate material
US3073751A (en) * 1960-08-01 1963-01-15 Consolidation Coal Co Method of making formcoke
US3347638A (en) * 1963-12-23 1967-10-17 Phillips Petroleum Co Process for production of carbon black pellets

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2511901A (en) * 1950-06-20 Agglomeration of carbon black
US2699381A (en) * 1953-08-28 1955-01-11 Phillips Petroleum Co Oil pelleting of carbon black
US2892689A (en) * 1954-06-14 1959-06-30 Phillips Petroleum Co Process and apparatus for classifying particulate material
US2872300A (en) * 1954-10-18 1959-02-03 Phillips Petroleum Co Process and apparatus for simultaneously pelleting powdered materials and classifying same
US3073751A (en) * 1960-08-01 1963-01-15 Consolidation Coal Co Method of making formcoke
US3347638A (en) * 1963-12-23 1967-10-17 Phillips Petroleum Co Process for production of carbon black pellets

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4159905A (en) * 1970-12-08 1979-07-03 Bergwerksverband Gmbh Method of manufacturing green hot briquettes from fine coal for use in shaft furnaces
US3946098A (en) * 1972-12-11 1976-03-23 Metallurgical Processes Ltd. Preparation of feed material for a blast furnace
US4104129A (en) * 1973-10-26 1978-08-01 United States Steel Corporation Low temperature carbonization and desulfurization of coal under elevated pressures
US4030982A (en) * 1975-07-10 1977-06-21 Consolidation Coal Company Process of making formcoke from non-caking or weakly caking coals
US4148692A (en) * 1977-08-26 1979-04-10 Bethlehem Steel Corporation Process for producing low reactivity calcined coke agglomerates
US4221570A (en) * 1979-04-16 1980-09-09 Continental Oil Company Method and apparatus for producing hardened carbonaceous agglomerates
US4278447A (en) * 1979-11-16 1981-07-14 Conoco, Inc. Methods for producing feedstock for a fixed bed gasifier from finely-divided coal
US4473464A (en) * 1980-05-07 1984-09-25 Conoco Inc. Method for producing distillable hydrocarbonaceous fuels and carbonaceous agglomerates from a heavy crude oil
US4314900A (en) * 1980-05-07 1982-02-09 Conoco Inc. Method for producing distillable hydrocarbonaceous fuels and carbonaceous agglomerates from a heavy crude oil
US4388152A (en) * 1980-08-04 1983-06-14 Conoco Inc. Process for producing blast furnace grade coke, a distillable product and fuel gases from a heavy, high sulfur, crude oil
US4410472A (en) * 1982-01-15 1983-10-18 Aluminum Company Of America Method for making spherical binderless pellets
US4631156A (en) * 1984-07-27 1986-12-23 Bofors Nobel, Inc. System and method of particulating 4,4' methylenebis (2-chloroaniline)
EP0169626A3 (en) * 1984-07-27 1987-06-03 Lomac, Inc. System and method of particulating 4,4' methylenebis (2-chloroaniline)
US5071515A (en) * 1987-03-09 1991-12-10 Conoco Inc. Method for improving the density and crush resistance of coke
WO1998027186A1 (en) * 1996-12-18 1998-06-25 Minpro Australia N.L. Coal processing method
US20080149471A1 (en) * 2006-12-26 2008-06-26 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US8444828B2 (en) 2006-12-26 2013-05-21 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US9045693B2 (en) 2006-12-26 2015-06-02 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US9446975B2 (en) 2011-10-21 2016-09-20 Therma-Flite, Inc. Gasifying system and method

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GB1131433A (en) 1968-10-23
DE1571643C3 (enrdf_load_stackoverflow) 1975-03-20
DE1571643B2 (de) 1974-07-25
DE1571643A1 (de) 1971-01-07

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