EP0022018B1 - Verfahren und Vorrichtung zur Herstellung von Koks oder Halbkoks - Google Patents

Verfahren und Vorrichtung zur Herstellung von Koks oder Halbkoks Download PDF

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Publication number
EP0022018B1
EP0022018B1 EP80400943A EP80400943A EP0022018B1 EP 0022018 B1 EP0022018 B1 EP 0022018B1 EP 80400943 A EP80400943 A EP 80400943A EP 80400943 A EP80400943 A EP 80400943A EP 0022018 B1 EP0022018 B1 EP 0022018B1
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EP
European Patent Office
Prior art keywords
coke
oven
semi
fines
rotary
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP80400943A
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English (en)
French (fr)
Other versions
EP0022018A1 (de
Inventor
Gustave Leyendecker
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Houilleres du Bassin de Lorraine
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Houilleres du Bassin de Lorraine
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Priority to AT80400943T priority Critical patent/ATE2439T1/de
Publication of EP0022018A1 publication Critical patent/EP0022018A1/de
Application granted granted Critical
Publication of EP0022018B1 publication Critical patent/EP0022018B1/de
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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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • 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
    • C10B1/10—Rotary retorts

Definitions

  • the subject of the invention is a process for the continuous production of coke or semi-coke by means of a rotary kiln.
  • This process is effective for obtaining more or less reactive cokes with a low volatile matter content, but does not allow, without significant modifications, to obtain cokes or semi-cokes baked at relatively low temperature, for example below 600 °. C and still having a fairly high content of volatile matter, for example up to 20%.
  • Such cokes or semi-cokes can have many direct or indirect applications. They can be recovered as they are for electrometallurgy, electrochemistry, gasification. They can be used as an adjunct in the manufacture of molded coke or in carbonized coke pastes with charging processes using preheating and / or compacting.
  • the object of the invention is to propose a new process and a new installation making it possible to obtain, with good adjustment flexibility, a wide range of cokes differentiated by their volatile matter contents, for example in the game from 1 to 20% volatile matter.
  • Another object is to avoid the combustion of by-products in situ, in order to recover a maximum amount of tar and gas.
  • the hot gas generator may for example be a burner installed at the end of the rotary kiln, as is known per se.
  • the heat output of the hot gas generator is controlled by the difference between the temperature of the coke or semi-coke at the end of the oven and a set cooking temperature. In this way, carbonization is obtained at the set temperature, which, indirectly, makes it possible to obtain the desired content of volatile matter. Controlling the carbonization temperature is essential according to the invention.
  • the overpressure in the oven enclosure can be adjusted by action on a valve located upstream of the production gas dewatering fan.
  • a finer adjustment can be obtained in addition by injecting an auxiliary ballast fluid, such as steam and / or combustion fumes of the lean gas from the recycled carbonization and / or nitrogen, directly in the rotating oven.
  • the coke or semi-coke is quenched by introduction into an inclined rotating tube fitted with water sprayers and the coke or semi-coke is quenched immediately after its extraction from the rotary kiln.
  • the process leading, depending on the settings, to highly flammable semi-cokes, the immediate extinction of these semi-cokes constitutes an important means.
  • the coke or semi-coke extinguishing device comprises means for spraying water.
  • the extinguishing device is an inclined rotating tube and that said rotating tube is open at its discharge end.
  • An installation according to the invention for the implementation of the method according to the invention comprises a tubular rotary oven 1, sealed and inclined by 2 ° on the horizontal downwards from right to left in the figure.
  • the rotary kiln communicates by rotary joints 2 and 3 with baffles respectively with a feed cover 4 and a heating cover 5.
  • a feed hopper 6 makes it possible to bring the coal upstream of the oven by a inclined chute 7 by means of a honeycomb distributor 8.
  • the hot gases of the rotary kiln are extracted from the feed cover 4, the walls of which are rinsed with water to avoid any fouling, by a pipe 9 to be brought to a first washer 10, then to a second washer 11, in which are arranged batteries of water sprayers 12.
  • the gases are sucked in by a dewatering fan 13 and sent to a pipe 14 provided with a register 15 allowing these gases to be wholly or partially sent to a storage capacity and / or to a pipe recycling 16.
  • the gas washing waters are sent to a decanter 17 communicating with an overflow tank 18, from where a pump 19 recycles them to the sprayers 12.
  • the heating cover 5 opens onto a chute 20 opening directly into the cover 21 of a rotating extinguishing tube 22 inclined 2 ° down from left to right, in the figure.
  • This tube 22 is provided with a ramp 23 of water sprayers.
  • the tube 22 is open at its lower or downstream end and the quenched coke in the tube can fall on a screen 24 whose passers-by falls on a conveyor belt 25.
  • the heating of the rotary kiln 1 is provided by a burner 26 supplied by a line 27 of liquid or gaseous fuel and an air line 28.
  • a regulator 29 provides a stoichiometric adjustment of the proportion of fuel and air or, at will , a depleted air setting.
  • the fuel flow rate is also regulated by the regulator 29 controlled, by a circuit 30, at a set temperature to be observed in the mass of incandescent coke or semi-coke, the true temperature there being measured by a thermometric probe 31 placed in the oven in the vicinity of the cover 5. It is also possible to introduce water vapor into the oven through a cane 32 opening into the cover 5.
  • the water vapor flow rate can be adjusted by a controlled pressure switch 33, by a circuit 34 , at a set pressure to be observed in the actual enclosure of the oven, the true pressure being measured by a pressure sensor 35 placed in the oven at an upstream point, for example.
  • the hot gases recycled through the line 16 can be reintroduced into the burner 26, either directly or by mixing with the fuel supplied by the line 27 if this fuel is gaseous.
  • the oven is sealed by. injections of water vapor by means of the injectors 36 in the rotary joints 2 and 3.
  • the pressure sensor 35 is used to regulate by a logic circuit 37 the vacuum created by the dewatering fan 13, this logic circuit also being able to open or close a bypass valve 38 and / or to regulate a draft register 39.
  • the coal is brought into the carbonization furnace via the hopper 6 provided with a protective screen and the anti-pinch cellular distributor 8.
  • This device makes it possible to supply the installation independently of the rotation speed and the slope of the revolving oven 1.
  • the coal by traversing the rotary furnace 1 of carbonization, loses its volatile matters thanks to the contribution of calories supplied by the burner 26 operating in stoichiometry.
  • the rotary carbonization oven 1 operates at slight overpressure (- 10 Pa), this in order to avoid parasitic air inlets liable to degrade the quality of the gas produced by dilution or combustion of volatile materials.
  • the baffle seals 2 and 3 and steam injection 36 fitted to the heating and supply hoods of the oven thus prevent the discharge of tarry gases towards the outside. Steam injection ducts allow eventual artificially increase the pressure.
  • the coke flows freely between tubes 1 and 2, the pressure difference between carbonization tube 1 and extinguishing tube 22 is less than 10 Pa.
  • a hot coke guard also makes it possible to limit ironing.
  • the incandescent coke flows, via the chute 20 which is broadly dimensioned and sufficiently sloping to avoid any accidental blockage by agglomerates, in the quenching tube 22 where the coke is quenched by water spraying.
  • the extinction is favored by a sweeping with natural air of the extinction tube by effect of air call of the sprayers. It is known, in fact, that to obtain a good extinction of a semi-coke, it is advisable that during its cooling it fixes a sufficient quantity of oxygen.
  • the production gas passes, as has been said, in the supply hood 4, the walls of which, to avoid any fouling, are rinsed with water, then in a series of washers 10, 11, where it undergoes watering. . Almost all of the tars are thus trapped and recovered at the base in the decanter 17.
  • the residence time of volatile materials in the oven should be controlled in order to avoid their thermal dissociation. This is achieved by the steam serving as the ballast gas in the oven and by the appropriate washing system for the production gases to prevent fouling. It is also obtained by recycling the fumes that make ballast.
  • the means of the invention therefore make it possible to control the carbonization temperature, which is essential, due to the risks of runaway well known in the manufacture of semi-coke or reactive coke.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Coke Industry (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Chemical Or Physical Treatment Of Fibers (AREA)
  • Fertilizers (AREA)
  • Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
  • Medicines Containing Plant Substances (AREA)
  • Furnace Details (AREA)
  • Control And Other Processes For Unpacking Of Materials (AREA)
  • Cookers (AREA)
  • Traffic Control Systems (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Industrial Gases (AREA)
  • General Preparation And Processing Of Foods (AREA)

Claims (11)

1. Verfahren zur kontinuierlichen Erzeugung von Koks oder Schwelkoks mit einem Gehalt an flüchtigen Stoffen zwischen 1 % und 20% ausgehend von Feinkohle und/oder Graupe oder Feinkohle mit mehr als 15% flüchtigen Stoffen und einem Schwellungsindex von unter 8, wobei die Feinkohle und/oder Graupe am Einlauf eines schwach geneigten, rohrförmigen Drehofens aufgegeben wird, in dem das Gut während seiner Behandlung vom Aufgabeende zum Abgabeende läuft, der von einem Heißgaserzeuger mit Wärme versorgt wird und aus dem der erzeugte Koks oder Schwelkoks abgeführt wird, wobei die Versorgung des Heißgaserzeugers so geregelt wird, daß er neutrale oder reduzierend wirkende Heißgase erzeugt, dadurch gekennzeichnet, daß das Innere des Ofens durch geregeltes Einblasen eines Hilfs-Ballastfluids auf einem leichten Gas-Überdruck gegenüber der Umgebungsluft gehalten wird.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Hilfs-Ballastfluid Wasserdampf umfaßt.
3. Verfahren nach Anspruch 1, wobei die Verkokungs-Solltemperatur zwischen 450°C und 1100°C liegt, dadurch gekennzeichnet, daß die Wärmeabgabe des Heißgaserzeugers geregelt wird aufgrund der Differenz zwischen der Temperatur des Koks oder Schwelkoks am Abgabeende des Ofens und einer Verkokungs-Solltemperatur.
4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß zur Förderung der Aufrechterhaltung der Dichtigkeit des Ofens ein neutrales, gashaltiges Fluid, beispielsweise Wasserdampf, in die Dichtungsanordnungen des Drehofens eingeblasen wird.
5. Verfahren nach Anspruch 1, wobei der Koks oder Schwelkoks durch Eingabe in ein sich drehendes, geneigtes Rohr gelöscht wird, dadurch gekennzeichnet, daß das geneigte Rohr mit Wasserverneblem versehen wird unddaß der Koks oder Schwelkoks darin unmittelbar nach seiner Abführung aus dem Ofen gelöscht wird.
6. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Feinkohle und/oder Graupe dem Drehofen unter Beigabe des zurückgeführten Feinstanteils des erzeugten Koks oder Schwelkoks aufgegeben wird.
7. Einrichtung zur Durchführung des Verfahrens nach einem der Ansprüche 1 bis 6, umfassend
- einen schwach geneigten, rohrförmigen Drehofen, der an seiner höchsten Stelle im wesentlichen abgedichtete Aufgabemittel für Graupe und/oder Feinkohle sowie an seiner tiefsten Stelle Mittel zur Einführung oder Erzeugung von Heißgasen und im wesentlichen abgedichtete Abführungsmittel für Koks oder Schwelkoks aufweist, und
- eine Löschvorrichtung für den Koks oder Schwelkoks, deren Einlauf mit den Abführungsmitteln für Koks oder Schwelkoks des Drehofens verbunden ist,

dadurch gekennzeichnet, daß der rohrförmige Drehofen (1) abgedichtet ist und Dampfzuführungsmittel (32) und Dampfzufuhr-Stellmittel (33) umfaßt, die von einem Meßwandler (35) für den Gasdruck im Ofen (1) gesteuert sind.
8. Einrichtung nach Anspruch 7, dadurch gekennzeichnet, daß die Löschvorrichtung (22) für den Koks oder Schwelkoks Mittel (23) zum Einspritzen von Wasser umfaßt.
9. Einrichtung nach Anspruch 8, wobei die Löschvorrichtung ein sich drehendes, geneigtes Rohr ist, dadurch gekennzeichnet, daß das genannte, sich drehende Rohr (22) an seinem Abgabeende offen ist.
10. Einrichtung nach Anspruch 7, dadurch gekennzeichnet, daß sie hinsichtlich des Durchsatzes verstellbare Abführungsmittel (13) für Gas aus dem Ofen umfaßt, die durch Meßmittel (35) für den Überdruck im Ofen (1) gesteuert sind.
11. Einrichtung nach Anspruch 7, dadurch gekennzeichnet, daß sie Einblasmittel (36) zum Einblasen eines neutralen, gashaltigen Fluids, beispielsweise Wasserdampf, in die Dichtungsanordnungen (2, 3) des Drehofens (1) aufweist.
EP80400943A 1979-06-25 1980-06-24 Verfahren und Vorrichtung zur Herstellung von Koks oder Halbkoks Expired EP0022018B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT80400943T ATE2439T1 (de) 1979-06-25 1980-06-24 Verfahren und vorrichtung zur herstellung von koks oder halbkoks.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR7916233A FR2459824A1 (fr) 1979-06-25 1979-06-25 Procede et installation de fabrication de coke ou semi-coke
FR7916233 1979-06-25

Publications (2)

Publication Number Publication Date
EP0022018A1 EP0022018A1 (de) 1981-01-07
EP0022018B1 true EP0022018B1 (de) 1983-02-09

Family

ID=9227039

Family Applications (1)

Application Number Title Priority Date Filing Date
EP80400943A Expired EP0022018B1 (de) 1979-06-25 1980-06-24 Verfahren und Vorrichtung zur Herstellung von Koks oder Halbkoks

Country Status (10)

Country Link
US (1) US4366026A (de)
EP (1) EP0022018B1 (de)
JP (1) JPS5645980A (de)
AT (1) ATE2439T1 (de)
BR (1) BR8003929A (de)
DE (1) DE3061892D1 (de)
DK (1) DK160366C (de)
FR (1) FR2459824A1 (de)
NO (1) NO150723C (de)
YU (1) YU41719B (de)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE8801377D0 (sv) * 1988-04-14 1988-04-14 Productcontrol Ltd Foredling av organiskt material
FR2656326B1 (fr) * 1989-12-22 1992-05-07 Pillard Chauffage Procedes, dispositifs et fours tournants pour fabriquer en continu du charbon de bois riche en carbone.
US5707592A (en) * 1991-07-18 1998-01-13 Someus; Edward Method and apparatus for treatment of waste materials including nuclear contaminated materials
DE4321676C2 (de) * 1992-07-14 1995-11-16 Bergwerksverband Gmbh Verfahren und Vorrichtung zur Regelung des Gasdruckes einer Koksofenkammer
US7247368B1 (en) * 2001-10-12 2007-07-24 Touchstone Research Laboratory, Ltd. Stealth foam and production method
US9045693B2 (en) 2006-12-26 2015-06-02 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
AU2007340053B2 (en) * 2006-12-26 2012-03-08 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US9604192B2 (en) 2007-03-14 2017-03-28 Richard D. TUCKER Pyrolysis and gasification systems, methods, and resultants derived therefrom
WO2008112306A1 (en) * 2007-03-14 2008-09-18 Tucker Richard D Pyrolysis systems, methods, and resultants derived therefrom
RU2481386C2 (ru) * 2008-10-08 2013-05-10 Сергей Петрович Хмеленко Способ непрерывной термохимической переработки различных видов углеродсодержащего сырья
CN101734657B (zh) * 2009-12-15 2012-05-02 北京大学 一种连续制备活性半焦的方法及其专用装置
CN104946272B (zh) * 2014-03-28 2017-09-26 宝山钢铁股份有限公司 一种焦炉荒煤气用余热回收装置及组合式二级取热方法
CN106318418B (zh) * 2016-09-23 2019-03-15 河南博顿生物科技有限公司 一种玉米秸秆低温炭化制备生物质炭燃料的方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE417688C (de) * 1921-01-21 1925-08-14 Eugen Weiss Verfahren zum Verschwelen von festen Brennstoffen im Drehrohrofen
US1830884A (en) * 1926-12-04 1931-11-10 Nielsen Harald Distillation of carbonaceous materials
FR1201247A (fr) * 1957-08-13 1959-12-29 Ruhrgas Ag Procédé de fabrication de coke de grande résistance
FR2284662A1 (fr) * 1974-06-27 1976-04-09 Lorraine Houilleres Procede de fabrication de coke pulverulent et de coke reactif en grains
US3940239A (en) * 1974-12-16 1976-02-24 Allis-Chalmers Corporation Rotary reducing kiln seal
US4064018A (en) * 1976-06-25 1977-12-20 Occidental Petroleum Corporation Internally circulating fast fluidized bed flash pyrolysis reactor

Also Published As

Publication number Publication date
EP0022018A1 (de) 1981-01-07
NO150723B (no) 1984-08-27
NO801873L (no) 1980-12-29
DK269780A (da) 1980-12-26
JPH0113514B2 (de) 1989-03-07
YU164580A (en) 1983-02-28
FR2459824A1 (fr) 1981-01-16
YU41719B (en) 1987-12-31
JPS5645980A (en) 1981-04-25
ATE2439T1 (de) 1983-03-15
DK160366C (da) 1991-08-19
DK160366B (da) 1991-03-04
US4366026A (en) 1982-12-28
FR2459824B1 (de) 1982-07-16
BR8003929A (pt) 1981-01-13
DE3061892D1 (en) 1983-03-17
NO150723C (no) 1984-12-05

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