EP0047509B1 - Procédé de séchage, respectivement préchauffage de charbon en utilisant des charbons maigre ou peu gras - Google Patents

Procédé de séchage, respectivement préchauffage de charbon en utilisant des charbons maigre ou peu gras Download PDF

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Publication number
EP0047509B1
EP0047509B1 EP81106956A EP81106956A EP0047509B1 EP 0047509 B1 EP0047509 B1 EP 0047509B1 EP 81106956 A EP81106956 A EP 81106956A EP 81106956 A EP81106956 A EP 81106956A EP 0047509 B1 EP0047509 B1 EP 0047509B1
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EP
European Patent Office
Prior art keywords
coal
binder
drying
preheating
steam
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
EP81106956A
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German (de)
English (en)
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EP0047509A2 (fr
EP0047509A3 (en
Inventor
Jürgen Dr. Ing. Echterhoff
Harald Dipl.-Ing. Frick
August Schaper
Heinrich Mohmeyer
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.)
Cessione amman Ima GmbH
Original Assignee
Alfelder Eisenwerke Carl Heise Kom-Ges Vorm Otto Wesselmann & Cie
Kokereigesellschaft SAAR mbH
Alfelder Eisenwerke Carl Heise KG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Alfelder Eisenwerke Carl Heise Kom-Ges Vorm Otto Wesselmann & Cie, Kokereigesellschaft SAAR mbH, Alfelder Eisenwerke Carl Heise KG filed Critical Alfelder Eisenwerke Carl Heise Kom-Ges Vorm Otto Wesselmann & Cie
Priority to AT81106956T priority Critical patent/ATE11303T1/de
Publication of EP0047509A2 publication Critical patent/EP0047509A2/fr
Publication of EP0047509A3 publication Critical patent/EP0047509A3/de
Application granted granted Critical
Publication of EP0047509B1 publication Critical patent/EP0047509B1/fr
Expired legal-status Critical Current

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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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying

Definitions

  • drying and preheating For the pretreatment of hard coal using non-baking or weakly baking coal by grinding, drying and preheating, the drying and preheating being carried out inertly with water vapor originating from the coal to be dried and then the coal particles being mixed with a binder in the presence of water vapor before they are mixed be used for pounding and coking.
  • the method can also be applied using or using coking coal.
  • a method of the type mentioned is known from DE-A 2810694, which involves the production of high-quality coke from coal which is unsuitable for coke production.
  • the fine-grained hard coal is dried in a drying device by means of a low-oxygen cycle gas, which essentially consists of water vapor. In a dedusting system, the steam from the coal dust particles is swept away.
  • the dried fine-grained hard coal is mixed with a bituminous binder in a mixing device, which is also operated under the protection of the low-oxygen cycle gas.
  • the coal pretreated in this way reaches the coal tower via encapsulated conveying devices and is used from there as insert coal for coking after the pounding operation.
  • DE-B 2555431 shows a process for producing blast furnace coke, which however works in bulk operation.
  • the coal is first crushed to such an extent that 85-95% of the coal particles are up to 3 mm fine and the rest is not more than 10 mm coarse.
  • the coal is then dried and preheated at 110-250 ° C., mixed with binders in an amount of 3 to 8% by weight and then pre-compressed, the pre-compressed fine coal to form briquettes of low strength with a density of 1.0-1.
  • briquettes of low strength are produced with the aid of the binder, it being necessary for a certain proportion of the briquettes to break up again when pouring them into the coke oven, and in this way the desired higher bulk density is achieved. So that the proportion of the voids between the poured briquettes in the coke oven is not too large and so that the desired higher bulk density is not adversely affected, the fraction of the briquettes must be kept within relatively narrow limits.
  • an entrained-flow dryer is used, which is operated with an inert gas of nitrogen, carbon dioxide and their mixtures with and without water vapor.
  • Such inert gas is freshly generated, for example, by burning coal, oil or gas. A return of a large part of the inert gas is also provided. Since water is carried in through the moist coal which is converted into water vapor during drying, this water vapor is discharged with excess inert gas. The inert gas only comes into brief contact with the coal grain during drying and preheating, so that a considerable temperature difference has to be used, which means that there is a risk of overheating and damage to the coal grain. In addition to the inherent disadvantages of entrained-flow dryers, these require very high investment and operating costs. The known method is also not harmless from a safety point of view, because the simultaneous presence of oxygen, CO and coal creates the risk of deflagration.
  • the dried and preheated coal after separation and removal from the circuit of the entrained-flow dryer comes under the influence of atmospheric air with a corresponding proportion of oxygen, so that here, in particular in the area of the pre-compression devices of the briquetting press, oxidation phenomena can occur on the surface of the coal particles, which are of the quality of the coke produced in this way is detrimental.
  • the weakly baking feed mixtures concerned whose already low coke formation capacity can easily be attacked or destroyed by the presence or the entry of oxygen at the prevailing temperatures.
  • the invention has for its object to develop a method of the type described in such a way that the access of oxygen, that is to say the oxidation of the carbon particles even after drying and preheating during subsequent handling until use in the coke oven, is prevented, so that also Using non-baking or only weakly baking coal a high-quality blast furnace coke can be produced.
  • this is achieved in that the mixing time of the coal with the binder is fixed, the coating of the coal particles by the binder occurs and the binder takes over the protective function against atmospheric oxygen on the way to coking.
  • the pretreated carbon particles are not only mixed or mixed with the binder, but intensively coated before they are led out of the inert gas atmosphere.
  • the binder acts as a protective jacket for the hot coal grain and prevents the entry of atmospheric oxygen in a free atmosphere.
  • the coating Although coal itself is a poor heat conductor, the coating also contributes to the fact that the temperature of the heated coal only drops very slowly, so that the coal in no way has to be fed to the ramming operation and the subsequent coking. It is entirely possible to temporarily store the preheated coal coated with the binder for several days and / or to transport it over long distances.
  • the binder not only fulfills the protective function of the coal grain during handling in an open atmosphere, but at the same time represents the compacting agent during the stamping process, that is, it replaces the water of the otherwise known damp-stamped coal. In conjunction with the pounding operation, the binder allows the production of a sufficiently stable coal cake that can be easily inserted into the coke oven.
  • the use of the mineral oil or coal-based binder instead of water as a compacting agent during stamping has the further advantage that the coal is inserted into the coal furnace practically free of water and yet stamped, so that no water has to be evaporated there.
  • the density should not fall below 1.0 kg / dm 3 , based on the anhydrous substance, especially if a high proportion of non-baking or only weakly baking hard coal is used. It has also been shown that an anhydrous, bound coal mixture can be compressed higher than moist coal with the same pounding energy.
  • the high tamped weight is not only advantageous for handling the cake, but also for improving the properties of the coke produced or for the fact that a relatively higher proportion of non-or only weakly baking hard coal can be used to produce high-quality blast furnace coke.
  • the high specific tamped weight improves the characteristics of the coke that describe the abrasion and the piece strength. It was even surprisingly found that when coal mixtures with relatively poor coking capacity were used, this was improved relatively more than when using higher-quality coking coal. Decreasing baking capacity can be compensated for by increased compaction. Pounding and preheating the coal improve the coke quality compared to bulk operation with moist coal.
  • the combination of the features leads to such an improvement in the properties of the coke that the person skilled in the art could not have expected based on the individual features.
  • the furnace throughputs are 30 to 50% cheaper compared to bulk operation with moist coal. This is probably due to the fact that the evaporation of the water takes place outside the coke oven, that the bulk density of dry coal is already higher than that of moist coal, and that because of the higher uniformity in terms of bulk density distribution and due to the lack of different water contents, the coke can be pressed earlier overall .
  • the binder also binds the dust and thus counteracts dust discharge in the template. Another advantage is the easier filling of the coke oven.
  • the new process is therefore environmentally friendly.
  • the use of non-baking or only weakly baking hard coal is very important to an extent that was previously not considered possible.
  • the use of water vapor as a heat transfer medium ultimately enables a higher energy density compared to an exhaust gas.
  • the drying and preheating of the fine-grained hard coal can not only be carried out in a safe manner, but is also inexpensive and gentle on the coal.
  • the drying, preheating and coating of the ground coal with the binder is carried out in the presence of water vapor with an oxygen content of less than 2%.
  • the intergas essentially consists of the water vapor that comes from the coal to be dried itself.
  • water vapor as an inert gas or drying medium, deflagrations and oxidation phenomena during drying and preheating are reliably avoided.
  • the coal is heated very intensively, but gently, because the condensing water vapor first raises the temperature of the coal relatively quickly and then the water is evaporated again by the coal.
  • the inert gas circuit can be heated indirectly by any fuel or exhaust gas at a high temperature level, but preferably by the hot circuit gases of a coke dry cooling system.
  • the circuit of the water vapor can therefore be expediently conducted in cocurrent over the coal to be dried and preheated in order to achieve a gentle treatment of the coal.
  • the binder is added to coat the coal particles in two to 8% by weight, preferably 5% by weight, of the preheated coal. Depending on the proportion, the mixing time required for the coating is determined.
  • the device for drying or preheating coal or coal mixtures and subsequent coking has a material silo 1 with a metering device for the ground moist coal.
  • the moist coal can be drawn off via a material conveyor 2.
  • the moist coal is dried and then preheated via a cellular wheel sluice 3 in the area of the inlet funnel of a drying drum 4, which is rotatably supported and driven about its longitudinal axis.
  • the coal is always in a cascade-shaped movement when passing through the drying drum 4 due to the trickle internals provided in it.
  • the system also has a pre-separator and cooler 5 and, downstream of this, a dedusting device 6, which is expediently designed as a cloth filter dedusting.
  • a fan 7 is provided downstream for circulating the heat transfer medium or the inert gas circuit and the partial circuit.
  • a heat exchanger 8 is used for indirect heating of the inert gas circuit.
  • the heat exchanger 8, on the other hand, is connected to a heating circuit 9, which ultimately leads to the exhaust stack 10 and has an exhaust gas recirculation 11.
  • a mixed gas fan 12 and a controllable shut-off element 13 are arranged in this exhaust gas recirculation 11.
  • a burner 14 is heated with gas or another medium which is drawn off via a line or a storage tank 15.
  • the combustion air for the burner 14 is brought in via an air fan 16 and a shut-off device 51.
  • the exhaust gases can be returned via the return line 11 after passing through the heat exchanger 8 and mixed in a mixing chamber 17 with the combustion exhaust gases.
  • the inert gas circuit leads with a line 18 from the heat exchanger 8 to the entrance into the drying drum 4.
  • the line sections 19, 20, 21, 22 and 23 complete the inert gas circuit.
  • the line piece 19 is connected between the outlet of the drying drum 4 and the inlet of the pre-separator and cooler 5, which is otherwise blown with cooling air by a blower (not shown) according to the arrows 24 and thus the temperature of the inert gas can be reduced.
  • the line section 20 connects the outlet of the pre-separator and cooler 5 to the dedusting device 6; the output of which is connected to the blower 7 via the line piece 21.
  • the line section 22 leads to a controllable shut-off device 25, from which the line section 23 leads to the heat exchanger 8.
  • the inert gas circuit 18 to 23 is formed from the line 18 and the line sections 19, 20, 21, 22, 23.
  • Two short-circuit lines 26 and 27 are provided in the inert gas circuit, in which controllable shut-off devices 28 and 29 are arranged.
  • a feed line 30 for water or steam for water or steam and a control device 31 which is required for start-up purposes.
  • the feed line 32 is required when the system is switched off.
  • the coal is gently dried and preheated in the driven rotating drying drum 4, with rapid condensation first taking place on the still cold coal. Later, a gentle and relatively precise temperature increase can be achieved by evaporating the water. It is easily possible to operate the plant in such a way that at the end of the drying drum 4 there is only a temperature difference of approximately 10 ° C. between the water vapor and the preheated coal.
  • the dried coal passes from the exit of the drying drum via an encapsulated conveying device 34 into a bucket elevator 35 and from there into an intermediate silo 36, from which it can be transferred in batches to a weighing device 37. The coal then continues to get into the mixer 38.
  • the dried coal is coated or coated with a binder.
  • This is fed into the mixer 38 from a binder tank 40 via an injection device 41.
  • the binder tank 40 is kept at the desired preprocessing temperature by a thermal oil heating unit 42.
  • the applied binder not only serves to bind dust, but also at the same time to improve the cohesion of the coal in the ramming device, so that a manageable cake is then formed.
  • the access of oxygen to the coal grain during further processing is prevented or further processing is possible without, for example, the ramming device having to be placed under inert gas.
  • the partial circuit 43 to 47 formed from the line sections 43 to 47 branches off from the line section 22.
  • This partial circuit 43 to 47 of the inert gas protects the dried one Coal and the relevant plant components over which it is conducted.
  • a shut-off device 51 is arranged in line piece 43.
  • Overpressure valve 49 always maintains an overpressure in the inert gas circuit 18 to 23 and in the sub-circuit 43 to 47, which can be 20-40 mbar, for example, at the outlet of the drying drum 4.
  • steam is continuously released to the exhaust gas chimney 10 via the pressure relief valve 49, both during the start-up phase and during the operation of the system, because water vapor is continuously enriched by the water introduced or by the water entrained by the coal.
  • the pre-separator and cooler 5 and the dedusting device 6 are connected to the Beckerwerk 35 via conveyor screws 50, so that the dry coal separated in the pre-separator and cooler 5 and the dedusting device 6 is added again to the dried coal brought in via the conveying line 34.
  • the controllable overpressure valve 49 is made ready for opening so that it can discharge a partial gas flow into the exhaust gas stack 10.
  • the amount of water supplied is measured so that the water vapor produced is sufficient to reduce the oxygen content in the circulating vapors to below 2%, preferably below 1%.
  • this opening process takes about 15 minutes.
  • drying of the coal can be started by switching on the material conveyor 2 and removing moist, ground coal from the material silo 1 and feeding it to the drying drum 4 via the rotary feeder 3. It is understood that at this point in time no more water is introduced via the feed line 30.
  • the damp coal to be dried reaches the material silo 1 in some way via a grinding device (not shown).
  • the material conveyor 2 is equipped with a direct current control drive.
  • the quantity discharged can be measured volumetrically by hand or set manually from a control center.
  • the amount of coal to be dried should be kept constant during operation.
  • the interior of the drying drum 4 is largely airtight against the environment. Above all, no atmospheric oxygen can penetrate, since the inert gas circuit 18 to 23 has the above-mentioned overpressure at the sealing points of the drying drum 4.
  • the temperature of the dried coal present at the end of the drying drum 4 is specified as a setpoint and is matched to the coking process. When the value falls below the setpoint, the shut-off device 25 on the pressure side of the fan 7 is opened, so that the amount of vapors in the inert gas circuit 18 to 23 is increased. If the temperature of the coal at the outlet of the drying drum 4 falls below the target value, the amount of vapors is reduced by the control device described above.
  • the entry temperature of the hot vapors into the drying drum 4 should be about 450 ° C. If the value falls below this target value, the gas supply to the burner 14 is increased. By introducing more energy, the exhaust gas temperature of the heating circuit 9 rises, so that the temperature of the inert gas circuit 18 to 23 is also raised via the heat exchanger 8. When the setpoint of the temperature of the heating circuit 9 is exceeded at the entrance to the heat exchanger, which is approximately 1100 ° C., the shut-off device 13 in the heating circuit 9 is opened. As a result, an increased recirculation of the exhaust gas mixture is initiated, whereby the exhaust gas temperature in the mixing chamber 17 is reduced to the desired value.
  • the vapors or the inert gas circuit are cleaned with the dedusting device 6 and the upstream indirectly working pre-separator and cooler 5.
  • the dried and preheated coal present at the end of the drying drum 4 is conveyed into the intermediate silo 36 via the conveying device 34 and via a bucket elevator 35.
  • the coal which is also dry and separated in the pre-separator 5 and in the dedusting device 6, is fed to the bucket elevator 35 via the conveyor screws 50.
  • the coal is removed from the intermediate silo 36 by means of cellular wheel locks and fed to the weighing device 37.
  • the cellular wheel sluices are switched off and the coal is introduced into the mixer 38.
  • the nozzle 41 becomes the bandage medium injected into the mixer 38.
  • the mixer opens and the dried, heated and coated material, namely the coal, reaches the coal tower 53 by means of a screw conveyor 52 the entry of atmospheric oxygen.
  • the coal arrives in batches from the coal tower 53 into the ramming machine 54, where it is compacted into a solid cake by tamping.
  • the compression or the specific tamped weight is at least about 1.0 kg / dm 3 (based on anhydrous substance).
  • a higher compaction results in an improvement in the properties of the coke produced or in the possibility of using non-baking or only weakly baking hard coal in higher proportions.
  • the pounded cake is then pushed out of the ramming device 54 into the coke oven 55 or in each case into the individual coke oven chamber, so that the volatile constituents of the coal can be extracted and the coke produced; the introduction of the mashed coal in the form of a cake into the coke oven 55 is advantageous in that the dust formation which is usual when using a dumping operation is avoided.
  • the heat transfer in the pressed cake is much better than in a loosely poured pile.
  • the material conveyor 2 is first stopped. Since the drying drum 4 no longer consumes as much heat, the temperature of the dry coal at the outlet of the drying drum 4 rises. Likewise, the temperature of the inert gas in the line section 19 also rises. Water is now introduced into the drying drum 4 via the control device 31 for water. Even now, atmospheric oxygen is prevented from entering the system. After the mixing of the coal in the mixer 38 has ended, the water supply to the drying drum 4 is switched off and the air supply via the second feed line 32 is made possible by opening the shut-off device 33. The amount of vapors circulating increases by sucking in air. Exhaust gas is continuously released into the exhaust stack 10 via the opened pressure relief valve 49.
  • the feed mixture considered shows only about 20% good-baking coals, while the rest is weak or non-baking. This is reflected in the key figures of the mixture:
  • the following table shows the grain size> 40 mm, the amount of grit> 10 mm and the mechanical coke qualities Micum 40, Micum 10, Irsid 20 and Irsid 10 for the three process variants. It can be seen that a usable coke can only be produced from the selected, very weakly baking mixture (low puff number, small dilatation) if the proposed method “preheating, binding, pounding” is used.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)

Claims (6)

1. Procédé de prétraitement de la houille, utilisant de la houille maigre ou peu grasse, par broyage, séchage et préchauffage, le séchage et le préchauffage étant exécutés de manière inerte avec de la vapeur d'eau provenant elle-même du charbon à sécher et les particules de houille étant ensuite mélangées à un liant en présence de vapeur d'eau, avant d'être mises en oeuvre pour le pilonnage et la cokéfaction, caractérisé en ce que le temps de mélange de la houille avec le liant est fixé de sorte qu'il se produise un enrobage des particules de houille par le liant et que le liant assure la protection contre l'oxygène de l'air sur le trajet allant à la cokéfaction.
2. Procédé suivant la revendication 1, caractérisé en ce que la houille enrobée de liant est pilonnée à une desité d'environ 1,0 kg/dm3 par rapport à la substance sèche.
3. Procédé suivant la revendication 1, caractérisé en ce que le séchage, le préchauffage et l'enrobage avec le liant s'exécutent en présence de vapeur d'eau, avec une proportion d'oxygène inférieure à 2%.
4. Procédé suivant les revendications 1 à 3, caractérisé en ce que le séchage et le préchauffage de la houille sont exécutés de sorte qu'on obtient une différence de température d'environ 10°C entre la vapeur d'eau et le charbon sec à la fin du trajet de préchauffage.
5. Procédé suivant les revendications 1 à 4, caractérisé en ce que le circuit de vapeur d'eau est dirigé, en courant parallèle, au-dessus de la houille à sécher et préchauffer.
6. Procédé suivant la revendication 1, caractérisé en ce que le liant est ajouté à la houille préchauffée sous forme de deux à huit % en poids et de préférence sous forme de cinq % en poids.
EP81106956A 1980-09-05 1981-09-04 Procédé de séchage, respectivement préchauffage de charbon en utilisant des charbons maigre ou peu gras Expired EP0047509B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT81106956T ATE11303T1 (de) 1980-09-05 1981-09-04 Verfahren zur trocknung bzw. vorerhitzung von kohle unter verwendung nicht oder nur schwachbackender steinkohlen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3033461 1980-09-05
DE3033461A DE3033461C2 (de) 1980-09-05 1980-09-05 Verfahren zur Trocknung und Vorerhitzung von feinfkörniger Steinkohle unter Verwendung nicht oder nur schwach backender Kohle und/oder Kohlenstoffträgern

Publications (3)

Publication Number Publication Date
EP0047509A2 EP0047509A2 (fr) 1982-03-17
EP0047509A3 EP0047509A3 (en) 1982-04-21
EP0047509B1 true EP0047509B1 (fr) 1985-01-16

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Application Number Title Priority Date Filing Date
EP81106956A Expired EP0047509B1 (fr) 1980-09-05 1981-09-04 Procédé de séchage, respectivement préchauffage de charbon en utilisant des charbons maigre ou peu gras

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EP (1) EP0047509B1 (fr)
AT (1) ATE11303T1 (fr)
DE (1) DE3033461C2 (fr)
DK (1) DK161712C (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0759709B2 (ja) * 1987-09-03 1995-06-28 三井鉱山株式会社 石炭の調湿方法

Family Cites Families (15)

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Publication number Priority date Publication date Assignee Title
DE1187584B (de) * 1954-07-30 1965-02-25 Steinmueller Gmbh L & C Verfahren zur Vortrocknung von Kohle
DE2211372C3 (de) * 1972-03-09 1980-10-02 Rheinische Braunkohlenwerke Ag, 5000 Koeln Verfahren zur Herstellung von Formkoks aus Braunkohle
US3793743A (en) * 1972-08-23 1974-02-26 Waagner Biro American Apparatus for drying coal
DE2434827A1 (de) * 1973-08-06 1975-02-27 Waagner Biro Ag Verfahren zur energierueckgewinnung bei gaserzeugungsprozessen
DE2415758A1 (de) * 1974-04-01 1976-02-26 Buettner Schilde Haas Ag Anlage zur kohletrocknung und vorerhitzung
DE2435500A1 (de) * 1974-07-24 1976-02-12 Hugo Dr Ing Schaefer Verfahren zur vorerhitzung von kokskohle unter benutzung von ueberhitztem abhitzedampf, der in einer trockenkokskuehlanlage in besonderer weise erzeugt wird
US4008042A (en) * 1974-08-16 1977-02-15 Coaltek Associates Coal heating temperature control
DE2555431B2 (de) * 1975-12-10 1978-12-21 Fa. Carl Still, 4350 Recklinghausen Verfahren zur Herstellung von Hochofenkoks
DE2626653C3 (de) * 1976-06-15 1982-01-07 Bergwerksverband Gmbh Verfahren und Vorrichtung zum Trocknen und Vorerhitzen von Kokskohle
DE2633789C3 (de) * 1976-07-28 1980-08-14 Wintershall Ag, 3100 Celle Verfahren und Vorrichtung zur Herstellung von Petrolkokskalzinat
DE2659335C2 (de) * 1976-12-29 1985-10-24 Bergwerksverband Gmbh Betrieb einer Kohleerhitzungsanlage
DE2719189C2 (de) * 1977-04-29 1984-07-19 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Verfahren zum Betrieb einer Kohlevortrocknungs- bzw. -erhitzungsanlage in Verbindung mit einer Kokerei
DE2748423A1 (de) * 1977-10-28 1979-05-03 Bergwerksverband Gmbh Verfahren zur inertisierung von kohleerhitzungsanlagen
DE2810694C2 (de) * 1978-03-11 1985-06-27 Alfelder Eisenwerke Carl Heise, KG vorm. Otto Wesselmann & Cie., 3220 Alfeld "Verfahren zur Vortrocknung von feinkörniger Steinkohle und zur Weiterverarbeitung zu hochwertigem Steinkohlenkoks"
DE2949720C2 (de) * 1979-12-11 1982-08-26 Alfelder Eisenwerke Carl Heise, KG vorm. Otto Wesselmann & Cie., 3220 Alfeld Verfahren und Vorrichtung zum Trocknen und Erhitzen von feuchter Kohle

Also Published As

Publication number Publication date
EP0047509A2 (fr) 1982-03-17
DK161712C (da) 1992-02-24
DE3033461C2 (de) 1982-11-04
ATE11303T1 (de) 1985-02-15
DK391981A (da) 1982-03-06
DK161712B (da) 1991-08-05
EP0047509A3 (en) 1982-04-21
DE3033461A1 (de) 1982-03-25

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