US2131702A - Coal processing - Google Patents

Coal processing Download PDF

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Publication number
US2131702A
US2131702A US107336A US10733636A US2131702A US 2131702 A US2131702 A US 2131702A US 107336 A US107336 A US 107336A US 10733636 A US10733636 A US 10733636A US 2131702 A US2131702 A US 2131702A
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United States
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gas
coal
heating
temperature
zone
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US107336A
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English (en)
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George A Berry
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NAT FUELS CORP
NATIONAL FUELS Corp
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NAT FUELS CORP
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Priority to US107336A priority Critical patent/US2131702A/en
Priority to GB27619/37A priority patent/GB501374A/en
Priority to FR832966D priority patent/FR832966A/fr
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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
    • C10B1/00—Retorts
    • C10B1/02—Stationary retorts
    • C10B1/04—Vertical retorts

Definitions

  • the object of this invention is broadly to not limited to the treatment of the ⁇ material in transform bituminous coal into a carbonizing briquette form.
  • the degree of grinding whichis fuel resembling anthracite and to recover other necessary will vary with different coals, but valuable products. More particularly, the inshould be suiiicient to permitfoperation without vention is concerned with producing carbonizedswelling under the controlled heating conditions 5 briquetted fuelof high density. Y which will be-described below, so that the ilnal This invention is in part a continuation of my' product will have a high specic gravity.
  • briquettes are also such as will, in the 10
  • very valuable commodities formation of the untreated briquette permit thel 10 may be recovered from bituminous coal, and attainment of a high initial density' therein particularly from the so-called slack which is which favorably influences the ultimate density produced in large quantities in the mining and of the finished product and favors the productransportation of bituminous coal and which sells tion on the carbonized briquettes of a smooth, for considerably less than the price of prepared clean exteriorgfree. from 10056 particles that 15 sizes of bituminous coal.
  • the invention is not might rub'oil.
  • a ⁇ fire box of given volume such as semianthracita bituminous binderssuch 25 2.
  • the product ignites more readily than anas coal tar, pitch, etc. may be used.
  • 'Ihe coal briquettes are heated up to final car- 3.
  • the product sustains combustion at tembonizing temperaturesof 700 to 1000 C. and then peratures lower than anthracite andis smokecooled down or ⁇ quenched so that they can be less. It will burn uniformly throughout the re discharged into the-atmosphere without igni- 30 bed and does not tend to go out around cooled tion. This heating may be considered as disides as is the case with anthracite. vided into three stages or temperature ranges,
  • the ash content is low and the paragraphc although, of course, it is not necessary to physi value per unit weight is high. ically separate the stages. Heating and cooling The process of this invention is further chartake place in all stages by contact of the 35 acterized by a high yield of organic vapors conmaterial with a gaseous medium of suitable temdensable at ordinary temperatures and in priperature.
  • the gaseous medium is substantially mary condition; that is to say, substantially of nonreactive with the coal and with the products the same composition as they were when rst which it gives off.
  • the stages are as follows:
  • the second stage is the low temperature disi
  • These products may be produced from a wide tillation stage and extends'from the 300 to 350 variety of grades or characters of bituminous temperature at the end of the first stage up to coal, of which, for example, the coal fields of 500 to 600 C ⁇ . ⁇ It is during this stage that most eastern United States afford a practically unof the vapors, condensable at ordinary tempera- 56 limitedsupply. tures are likewise produced.
  • the process is carried out continuously, pref- 3.
  • the third stage is the final carbonization erably with a countercurrent flow of gases and and extends from theupper temperature limit solids. It is preferred to grind the vcoal and of the second stage up to 700 to 1000 C.
  • Fur- Y form it into briquettes, although the invention is ther amounts of tar vapors are evolved during 55 this stage, together with a permanent gas oi lower influenceic value, and the briquette shrinks more and more and acquires increased density and hardness.
  • the final temperature will depend on the reactivity and density desired in the final product. A lower final temperature will give a more easily ignitable less hard and dense product which is suitable for re place, brazier and similar methods of heating. On the other hand. a higher nal temperature will give a harder and denser product suitable for furnace firing.
  • the fully carbonized coal or briquettes are then cooled in a current oi nonreactive gas down to a sufficiently low temperature so that they can be discharged into the atmosphere without ignition and can be readily handled.
  • the heating may be very rapid, for example, heating increments per minute of 10 C., or even higher, do no harm and the same is true in the third stage. It is only necessary to control the ratel of heating accurately in the second stage and in this control it is not sufficient that the average rate of heating during the second stage be below the critical point.
  • the rate of heating will depend on the coal used and on,the binder used, and to some extent on the iineness of grinding of the'coal where briquettes are made. In general, it will vary from about 114 C. per minute for badly swelling or softening coal, up to nearly 10 C. per minute with certain coals such as Pocahontas and New River coal, which do not swell badly or soften unduly.
  • the coal or briquettes pass through the differenttemperature zones or regions, for example, by passing downwardly through a retort .countercurrent to the heating and cooling gas or gases for the various stages.
  • any other means which will move the coal or briquettes count-ercurrent to the gas stream may be employed an'd the present invention is not concerned with any particular structural details of retort design.
  • the average rate of heating through the critical zone will depend on the rate at which the briquettes pass through the zone, provided the ilow of heating gas and'its heat content are such as to supply the heat required to raise the briquettes to the nal temperature of the zone.
  • the maximum rate of heating occurring at any point in the zone will, however, also depend on other factors, notably, ratio between the weight of heating gas and briquettes.
  • FIG. 1 is a diagrammatic illustration of a plant for carrying out the present invention using a plurality of heating gas circuits
  • Fig. 2 to Fig. 6 are curves of gas and coal temperatures for various gas ratios and coal feeds.
  • the present invention is not concerned with the particular nature of the heating and cooling gas used so long as it is substantially nonreactive with thelcoal or with its distillation products, although in the preferred embodiment which will be described below in connection with Fig. 1 of the drawings, the evolved gases themselves are used as nonreactive gases and different gas circuits are used for the diierent stages in'order to recover the high caloric, permanent gas separate from the lower caloric gas produced'in the final carbonizing zone or stage. While this preferred lembodiment represents important practical advantages because of the higher price which can be obtained for undiluted, high caloric, permanent gases, the invention is broadly not limited to this procedure. If desired, a nonreactive gas stream may flow countercurrent to the coal throughout the whole length of the retort. -In more specic aspects, of course, the preferred embodiment constitutes a part of the present invention.
  • the heating gas performs two functions; First, it is a very uniform heating medium, contacting the surfaces of all of the lumps or briquettes, and secondly, the large volume of gas which is, of course, ⁇ necessary because of the low specific heat per unit volume, sweeps or scrubs off the vapors reaching the surface of the coal.
  • the partial pressure of the evolved vapors is therefore very low and they remain volatile at temperatures far below their boiling point at atmospheric pressure, and hence do not show any tendency to condense or precipitate on cooler coal which they encounter in passing countercurrent through the stage. y
  • Fig. 2v showsthe ideal and preferred operating conditions of the present invention. 7,lin this figure the weight of heating gas circulated per unit of time multiplied by its specific heat is exactly equal to the weight of coal or briquettes multiplied by their apparent specific heat.
  • apparent specific heat is used because the amount of heat absorbed by a unit weight of coal or briquettes in passing through the second stage' does not necessarily correspond exactly to the actual specific heat'of the material multiplied by the ltemperature rise. The reason for this is that there are other phenomena taking place.
  • Fig. 3 shows the conditions which obtain when the ratio of gas to solids is decreased. In order to introduce the same total quantity of heat to bring up all of the briquettes to the exit tem- ⁇ perature of the zone, it is, of course, necessary to introduce the gas at a higher temperature. It
  • Fig. 3 shows that it is possible to obtain the required rate of heating without balancing the heat capacity of the gas and solids accurately but this is obtained only at the sacrifice of output because in order to keep the maximum heating rate within the permissible limitation, the average. heating rate, which determines thev output of the must be greatly reduced.
  • the gas and solids temperature curves are no longer straight lines but instead of the rate of heating being lower than the average in the upper portion of the zone, and higher than the average in the lower portion of ther zone, it is higherl in the upper portion of the zone and lower in'the lower portion.
  • the conditions of; Fig. 2 represent the maximum permissible heating ⁇ rate
  • the maximum rate in the upper partof the"zone as shown in Fig. 5 will exceed this figure and therefore again the process will notfworkand the coal will swell.
  • Fig. 6 shows how it is possible to compensate Y'. for the unbalan'ce in Fig. 5 v and again the unbalance is compensated for by "decreasing the rate of flow of briquettes and gas in the same proportion and therefore decreasing the average rate of heating to a point sumciently low so that the maximum rate does not exceed the permissible figure.
  • the compensation is obtained at the expense vci? a longer time cycle "and greatly decreased output for a given piece of equipment. 1
  • the reason for avoiding any considerable deformation'of any Vsticking together of the briquettes lies in the necessity for subjecting the surface of the briquettes during the carbonization cycle to free and uniformcontact with the heating gases. If briquettes are not deformed excessively andv do not stick together, they roll suflicieritly in passing through the retortso that the points ⁇ of contact between the briquettes are constantly shifted.
  • FIG. 2 Another advantage of the preferred specic embodiment of the present invention represented by Fig. 2 is that the heat head between gas and solids is kept at a minimum.
  • Figs 3 and 5 show at one or other ends of the curves, a much larger heat head or heat difference between gas and solids. There is thus greater danger of cracking or carbonization of vapor evolved at the surface of the coal when encountering the much hotter gas at levels of the zone where the gas temperature and solids temperature curves diverge widely.
  • Heating by means of a gas stream also results in great uniformity and since the critical factor of rate of heating applies to each individual coal lump or briquette it is not sufficient that the rate of heating in the critical stage be low merely for the charge as a wholebecause it is not the average .condition throughout the charge which counts but the condition at the surface of each lump. Gas heating, therefore, gives a uniformity throughout the whole charge which is iinpossible with external heating.
  • bituminous coal or bituminous coal with anthracite, semianthracite,
  • semibituminous, lignite, semicoke and coke may be used. This is particularly important where fine noncoking refuse is available such as, for example, coke breeze, anthracite fines, for example anthracite nes obtained as the flotation concentrate from the flotation cleaning of anthracite slush culm. These ne materials command a very low price and can be effectively blended with bituminous coal by means of the lpresent invention to produce high grade briquettes having superior burning characteristics.
  • Fig. 1 of the drawings the reference character I indicates a vertically disposed, elongated
  • the retort I may be regarded as divided into four sections 4, 5, 6 and 1, acting as preheating, distilling, high temperature, and cooling or quenching sections, respectively.
  • the high temperature section 8 may be a retort of refractory material or metal and may be surrounded by a heating device 8.
  • a burner or burners 9 are provided for the heating device l.
  • An air inlet for ⁇ the burner ls shown at III andra lean gas inlet pipe Il is provided with a valve II' leading to this burner.
  • the products of combustion from the burner or burners pass into an Vannular combustionspace or flue I2 in the heating device 8.
  • Ports I3 lead from the combustion space I2 to the annular space ⁇ I4 from which a series of exits -or outlets ⁇ I5 for hot yproducts of combustion lead into the lower ⁇ portion of the high temperature section 8.
  • a pipe I6 provided with a valve I6' leads to a manifold I'l at the lower portion of the cooling section 1.
  • a series of openings I1' lead from the 4manifold II into the section' 1.
  • a pipe 25 lfor gases from which tar has been removed leads from the extractor 25 to the lean gas receiver 26.
  • a valved outlet or vent pipe 21 is provided on the receiver 26.
  • the valved pipes I I and Il4 also are connected to the lean gas receiver 26.
  • A'pipe 30 leads from the heated side of the heat exchanger 20 to a manifold 3
  • An outlet pipe 33 leads from the upper portion of the distilling section 5 to the condenser 34 which removes organic liquids that are condensible at ordinary temperatures.
  • a pipe 35 leads uncondensed gases of high caloriflc power from the condenser 34 to the suction pump or blower 36 from the outlet of which pipe leads to the tar extractor 31 of yanyof the well known types suitable for removing tar.
  • a pipe ⁇ 3'I' for rich gases from which tar has been removed leads from the extractor 31 to the-receiver 33 which is provided with a valved outlet .33 -for surplus rich gas.
  • a valved pipe 40 leads rich gases from the receiver 38 to the heat exchanger 20 where these gases are heated and. pass into the distilling section 5 through the pipe 30.
  • a valved by-pass 4I around the heat exchanger 2l leads from the pipe 40 to the pipe 50 to provide convenient regulation of the temperature of the rich gases that enter the distilling section 5 through the pipe 30.
  • An outlet pipe 44 leads from the upper portion of the preheating section 4 to the suction pump orv blower 45, from the outlet of which a valved pipe 46 leads to a condenser 41 Afrom which a pipe 41' leads uncondensed gases to the heater 48.
  • the gas heater may be heated by combustion of lean gases taken from the receiver 26 through the valved pipe 49 to a. burner 50, air for combustion purposes being admitted through the inlet 5I.
  • the hot products of combustion from the burner 50 after heating the gas heater 48 are lead by the pipe53 into the lower. portion of the preheating section 4.
  • a valved pipe 54 leads from the lean gas receiver 26 to the pipe 44 to supply any needed make up gases for the preheating section.
  • the volumes of the gases and the amount of the gas made in the several sections of the retort depend upon the type of coal being treated, although the difference between coals from the standpoint of gas volumes required for heat transfer purposes-from the gas to the coal is small. However, diie'rences in coals will affect to a considerable extent the amount of .gas produced in the several sections of the retort and the weight of the iinished product for a given weight of raw coal treated.
  • coal containing approximately 20% of volatile matter will produce amounts of gas and will require rates of gas circulation and temperatures as follows:
  • the gas entering the high temperature section 6 from the combustion flue I2 is taken from the lean gas receiver' 26, and is caused to undergo a sufcient amount of .combustion to bring the temperature of the mixture to slightly above '900 C., the volume being about 13,300 cubic feet.
  • the temperature of the gas leaving the upper portion of the hightemperature section 6. through the pipe II is about 100 higherthan the solid products at this point in the retort I.
  • the highv temperature section .6 may pass out throughv the pipe I3 to the heat exchanger 20, condenser 22, tar extractor 25 and into the receiver 26.
  • About one-111th or 9,700 cubic feet of the gases passing -through the high temperature section 6 may pass into the lower portion of the distilling section 5 at a temperature of about 600 C. and be joinedb'y heated rich .gas entering this section throughy the pipe 30.
  • the vent 21 on the lean gas receiver 26 the amount of gas that passes from the high temperature section-6 to the distilling Section5 can be regulated,
  • the rich gas of high B. t. u. value is drawn off through the pipe 33 and is passed through the (or part of it through the by-pass 4I) back to the lower portion of the distilling section 5..
  • the moisture and other condensable products are condensed out of the gas leaving through the pipe 44 before it enters the heater 48.
  • the rich gasl that is produced byctheocoa'l in the distilling section 5 is of very high caloric value. It has been found to be ⁇ from 800 to 1000 or more B. t. u. per cubic foot, depending upon the sort of coal that is treated. 'I'his gas is largely methane and higher hydrocarbonslusually called illuminants and a relatively small amount of hydrogen.
  • the rate of heating in the distilling section is 2 to 4 C. per minute for the coals specied.
  • the invention has been described specically in conjunction with a plurality of gas circuits which permit the separate removal of high Acaloriilc gas. It will be apparent that the carbonization, that is to say, theproduction of ⁇ the solid product of the invention is not concerned with the characteristics of heating gas so long'as the heating gas is nonreactive with the material. Where it isl not desired to obtain high calorlflc permanent gas separately, a cheaper operation from the standpoint of equipment and operating costs can be effected by permitting the gas stream to flow through the Whole length o f the retort.
  • Compromises may also be eiIected, that is to say, distilling section 5 may be partly heated by gases flowing up from the section 8 and partly by gases coming from the heat exchanger 20'.
  • the condenserv 22, tar extractor 25, and receiver 26 is reduced in si ⁇ z ⁇ e by corresponding reduction in the heat losses and in th were and other operating expenses.
  • The/Wfaken off through the pipe 39 will, of course, be of a mentionic value intermediate between that obtainable with a full dual circuit operation and that corresponding to a complete single circuit.
  • the skilled I engineer will choose a compromise which represents the best economic value for a particular plant using a particulargraw material in a given location. It is an advantage of the present invention that gases of different calorific power can g be produced so as to adapt the process for the different conditions obtaining in different geographic locations.
  • a continuous process of destructively distilling coal whichcomprises passing the coal capable of coking in succession through a series of zones, the rst being a preheatlng zone to a temperature at which evolution o! volatile material begins, the second zone being the lfirst dlstilling zone and extending from the softening point of the coal up to a temperature of about 500 to 600 C. in which zone the major portion of the condensable hydrocarbon volatiles are evolved and a third zone extending up to about '700 to 1000 C.
  • the heating for at least the second zone being by contact with hot gases which are substantially nonreactive with the coal at the existing temperatures in the zones, the volume of heating gas and its speciilc heat in the second zonebeing suilicient so that when introduced at substantially the exit temperature of the coal leaving the zone i t contains suilicient heat to bring the coal passing through the zone up to exit temperature while Abeing itself cooled down to substantially the temperature of the coal at the inlet of the second zone, the rate of heating in the second zone being sufficiently low so that the particular coal will not swell sufficiently. to produce a product having a density as light as high-temperature coke produced from the same coal in a standard by-product coke oven.
  • a continuous process of vdestructively distilling coal capable of coking which comprises grinding the coal, incorporating a binder with ⁇ the ground coal forming it into briquettes having suilicient strength to permit handling and I passing the coal in succession through a series of zones, the rst being a preheating zone to a temperature at which evolution 'of volatile material begins, the second zone being the ilrst vdistill-- ing zone and extending from the softening point of the coal up to a temperature of about 500 to 600 C. in which zone the major portion of the' condensable hydrocarbon volatiles are evolved and ⁇ a third zone extending up to about 700 to 1000 C.
  • the heating for at least the second zone being by contact. ⁇ with hot gases which are substantially nonreac- 'tive with the coal at the existing temperatures in the zones, the volume of heating gas and its specic heat in the second zone being suillcient so that when introduced at substantially the exit temperature oi' the coal leaving the zone it contains suilicient heat to bringthe coal and binder passing through the zone up to exit temperature while being itself cooled down 4to substantially the temperature of the coal at the inlet to the second zone, the rate of heating in the second zone being sunlciently low so that the particular coal will not swell sufficiently' to produce a.
  • a continuous process for destructively distilling coal capable of coking which comprises passing the coal in succession through a series of zones, the rst being a preheating vzone to a temperature at which evolution o'f volatile material begins, the second zonebeing the ilrst distilling zone and extending from the softening point of the coal up to a temperature of about 500 to 600? C. .in which zone the major portion of the .condensable hydrocarbon volatiles are evolved and a third zone extending up to about '700 to 1000 C. in which zone the desired degree of distillation and carbonization is reached, the
  • the volume ⁇ of heating gas and its specic heat in the second zone being sufficient softhat when introduced at substantially the exit temperature of the coal leaving the zone it contains suiilcient heat to bring the coal and binder passing through the zoneup to exit temperature while being itself cooleddown to substantially the temperature of the coal at the inlet to the zone, the rate of heating in the second zone beinggsuillciently low so that the particular coal will not swell suillciently to produce a lproduct having a density as light as high-temperature coke produced from the .same coal in a standard by-product coke oven.
  • A'process according to claim 1 in which the heating in the third zone is eilected by a gas v stream oi' relatively low caloric value which has been partially burned' and the heatingv in the second zone is effected by the circulation of a gas stream of high caloric value whereby dilution ofthe volatile material evolved in the second zone with gases of low calorinc value is avoided.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
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US107336A 1936-10-24 1936-10-24 Coal processing Expired - Lifetime US2131702A (en)

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Application Number Priority Date Filing Date Title
US107336A US2131702A (en) 1936-10-24 1936-10-24 Coal processing
GB27619/37A GB501374A (en) 1936-10-24 1937-10-11 Improved process for the destructive distillation of coal
FR832966D FR832966A (fr) 1936-10-24 1937-10-18 Procédé continu pour la distillation du charbon en vase clos

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Cited By (61)

* Cited by examiner, † Cited by third party
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US2536783A (en) * 1948-03-04 1951-01-02 Colorado Fuel & Iron Corp Apparatus for producing activated carbon
US2560767A (en) * 1946-03-22 1951-07-17 Universal Oil Prod Co Distillation of carbonaceous solids
US2637683A (en) * 1948-12-24 1953-05-05 Universal Oil Prod Co Distillation of solid carbonaceous materials
US2658862A (en) * 1950-06-09 1953-11-10 Reilly Tar & Chem Corp Process for the defluidization and fixed-bed coking of a preheated fluidized coal
US2675307A (en) * 1949-08-04 1954-04-13 Monsanto Chemicals Process for coking-calcining complete smelting charge aggregates
US2694038A (en) * 1950-07-10 1954-11-09 Phillips Petroleum Co Method for manufacturing coke
US2698283A (en) * 1950-06-29 1954-12-28 Svenska Maskinverken Ab Method and apparatus for the destructive distillation of oil shale
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US2709153A (en) * 1949-12-27 1955-05-24 Rummel Roman Carbonization and gasification of bituminous material
US2732332A (en) * 1956-01-24 Geller
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US2794774A (en) * 1952-08-12 1957-06-04 Mora Fernando Mario Retort arrangement
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US2899365A (en) * 1959-08-11 scott
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US2966446A (en) * 1956-06-04 1960-12-27 Union Oil Co Shale retorting process
US2966400A (en) * 1954-09-27 1960-12-27 Frances H Lykken Lignite processing method
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US3011953A (en) * 1958-07-02 1961-12-05 Charbonnages De France Method and apparatus for the carbonization of fluidized materials
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US3140985A (en) * 1959-09-26 1964-07-14 Metallgesellschaft Ag Method of oxidation hardening of briquettes
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US3167487A (en) * 1961-08-28 1965-01-26 Mansfield Vaughn Method for producing coke and gas from carbonizable material
US3177128A (en) * 1961-10-30 1965-04-06 Bart V Vartanian Apparatus for producing carbon by direct heating with recycled volatile by-products
US3185635A (en) * 1961-05-10 1965-05-25 Us Smelting Refining And Minin Method for producing metallurgical coke and metal-coke from both coking and non-coking coals
DE1216836B (de) * 1961-07-21 1966-05-18 Metallgesellschaft Ag Verfahren zur Haertung bindemittelhaltiger Briketts durch oxydierende Behandlung mit sauerstoffhaltigen Gasen
US3316155A (en) * 1963-01-25 1967-04-25 Inland Steel Co Coking process
US3331754A (en) * 1963-06-07 1967-07-18 Mansfield Vaughn Coke quenching system and method
US3444048A (en) * 1966-01-20 1969-05-13 Bergwerksverband Gmbh Continuous coking apparatus
US3464892A (en) * 1967-05-23 1969-09-02 Sun Oil Co Tunnel oven with a series of moving barges and separate compartments
US3464913A (en) * 1965-11-24 1969-09-02 Pan American Petroleum Corp Oil shale retorting method
US3475319A (en) * 1966-12-22 1969-10-28 Exxon Research Engineering Co Retorting of oil shale
US3539027A (en) * 1968-09-20 1970-11-10 Eaton Yale & Towne Integrating conveyorized weighing system
DE1421258B1 (de) * 1959-06-18 1972-09-21 Fmc Corp Verfahren zur Herstellung von Formkoks aus Kohlen beliebiger Art
DE2141876A1 (de) * 1971-08-20 1973-03-01 Metallgesellschaft Ag Verfahren zur verkokung stueckiger brennstoffe mit spuelgasen
US3933618A (en) * 1974-03-11 1976-01-20 Blue Ember Flame Corporation Gas generation apparatuses and processes
US4002534A (en) * 1971-08-20 1977-01-11 Metallgesellschaft Aktiengesellschaft Continuous coking process
US4056443A (en) * 1975-02-19 1977-11-01 Centro Sperimentale Metallurgico S.P.A. Coke production
US4099933A (en) * 1973-06-01 1978-07-11 Hydrocarbon Research, Inc. Process for the multiple zone gasification of coal
US4102750A (en) * 1975-08-18 1978-07-25 Nippon Steel Corporation Process for producing formed coke for metallurgical use
US4108731A (en) * 1973-11-29 1978-08-22 Centro Sperimentale Metallurgico S.P.A. Coke production
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US4056443A (en) * 1975-02-19 1977-11-01 Centro Sperimentale Metallurgico S.P.A. Coke production
US4115202A (en) * 1975-02-22 1978-09-19 Firma Carl Still Apparatus for producing non-abrasive coke forms from brown-coal briquets
US4102750A (en) * 1975-08-18 1978-07-25 Nippon Steel Corporation Process for producing formed coke for metallurgical use
US4134794A (en) * 1976-02-23 1979-01-16 Firma Carl Still Method for producing non-abrasive coke forms from brown-coal briquets
US4165216A (en) * 1977-03-23 1979-08-21 Enerco, Inc. Continuous drying and/or heating apparatus
US4284477A (en) * 1978-06-26 1981-08-18 Mansfield Carbon Products, Inc. Coking apparatus for producing coke
US4661123A (en) * 1983-04-21 1987-04-28 Duchene Paul R Kiln for treating bituminous schists
US7037410B2 (en) 1994-11-28 2006-05-02 Gentech, Inc. Process and apparatus for destructive distillation of rubber
US20020077516A1 (en) * 1994-11-28 2002-06-20 Gentech, Inc. Process and apparatus for destructive distillation of rubber
US5783046A (en) * 1994-11-28 1998-07-21 Gentech, Inc. Process and apparatus for the destructive distillation of rubber
US6372948B1 (en) 1994-11-28 2002-04-16 Gentech, Inc. Process and apparatus for the destructive distillation of rubber
US9464245B2 (en) * 2010-11-01 2016-10-11 Institute Of Process Engineering, Chinese Academy Of Sciences Apparatus and method for multistage hierarchical pyrolysis and gasification of solid fuels
US20130239479A1 (en) * 2010-11-01 2013-09-19 Shiqiu Gao Apparatus and Method for Multistage Hierachical Pyrolysis and Gasification of Solid Fuels
US20130062186A1 (en) * 2011-09-13 2013-03-14 Franklin G. Rinker Process for treating coal using multiple dual zone steps
US9074138B2 (en) * 2011-09-13 2015-07-07 C2O Technologies, Llc Process for treating coal using multiple dual zone steps
US20170114279A1 (en) * 2015-10-22 2017-04-27 Enventix, Inc. Pyrolysis Reactor
US10752841B2 (en) * 2015-10-22 2020-08-25 Enventix, Inc. Pyrolysis reactor
EP3491052A4 (fr) * 2016-07-26 2020-03-18 PRTI Global Management LLC Appareil et procédé de défabrication thermique de pneus et d'autres déchets
US10703876B2 (en) 2016-07-26 2020-07-07 Prti Global Management Llc. Apparatus and method for thermally demanufacturing tires and other waste products
US20220275166A1 (en) * 2021-03-01 2022-09-01 PRTI Global Management, LLC Apparatus and method for thermally demanufacturing tires and other waste products
US11479723B2 (en) * 2021-03-01 2022-10-25 PRTI Global Management, LLC Apparatus and method for thermally demanufacturing tires and other waste products

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FR832966A (fr) 1938-10-07

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