EP0155318B1 - Process and unit for producing briquette material for hot briquetting - Google Patents

Process and unit for producing briquette material for hot briquetting Download PDF

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Publication number
EP0155318B1
EP0155318B1 EP84903714A EP84903714A EP0155318B1 EP 0155318 B1 EP0155318 B1 EP 0155318B1 EP 84903714 A EP84903714 A EP 84903714A EP 84903714 A EP84903714 A EP 84903714A EP 0155318 B1 EP0155318 B1 EP 0155318B1
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Prior art keywords
bed reactor
moving bed
briquetting
distribution
arms
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German (de)
French (fr)
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EP0155318A1 (en
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Otto Gmbh Still
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Still Otto GmbH
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Still Otto GmbH
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    • 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms 
    • B01F27/902—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms  cooperating with intermeshing elements fixed on the receptacle walls

Definitions

  • the invention relates to a method for producing a briquette for hot briquetting by pyrolytic decomposition of baking hard coal in a mixture with two to five times the volume of fine-grained, thermally largely stable substances and to an apparatus for carrying out the method.
  • Such a method for producing a briquette is known from GB-A-1 168 283, which is based on priority applications DE-A-1571710 and 1671377.
  • the methods described in these two documents relate in particular to measures to achieve a certain level of the Urteer yield of the briquetted material at the time of deformation.
  • the yield from Urteer should amount to 0.2 to 0.8% and according to DE-A-16 71 377 between 0.07 and 0.2%.
  • the main task was to achieve the maximum possible de-emptying of the briquetted goods.
  • Mixing temperatures of 450 ° C to 530 ° C and a residence time of the briquetted material of 1 to 15 minutes are already mentioned as important process features.
  • the solid components are introduced into a container in which the mixing and degassing takes place.
  • the container contains an agitator with a vertical axis.
  • the briquetted material is fed to the roller press via a feeder in the manner of a cellular wheel, which rotates about a horizontal axis. This allocator is not described in detail.
  • the object of the invention is therefore to propose a method and a device for carrying out this method, with which a briquetted good consistency for the hot briquetting is produced, this briquetted material being evenly distributed over the roller width of more than 400 mm, always briquettes uniform consistency and strength and very high throughput rates of more than 7 t / h up to about 70 t / h can be achieved.
  • the briquetted material should remain in the moving bed reactor for a certain time, since on the one hand sufficient pyrolysis and degassing must take place - because insufficiently degassed, specially de-emptied briquette material tends to burst again after pressing, on the other hand there is a risk that the product that is too strongly degassed will The fat coal loses its binding ability and the product silted up and thus tends to extremely high abrasion. Finally, according to the invention, the briquetted material should be uniformly distributed over the entire briquetting roller width in a certain time using certain measures.
  • the briquetted material should finally be pre-compressed in a space sealed against the atmosphere of the press chamber and distributed evenly over the entire width of the roller.
  • air penetration and thus the formation of an explosive mixture is prevented.
  • the briquettes fall into an open space so that the press can be easily monitored.
  • a moving bed reactor which consists of a container in which one or more agitators with a vertical axis of rotation and horizontal agitator arms are arranged and whose distribution zone below consists of a distributor with a horizontal central axis of rotation, with the aim of achieving an intensive mixing and Kneading movement in the distribution zone is proposed according to the invention that fixed arms are attached to the end walls of the housing of the distribution zone, which project in the axial direction into the cylindrical distributor basket.
  • the number and shape of the distributor webs which in the direction of rotation in the middle, i.e. at half the length of the distributor basket, advance and are bent or angled towards the ends.
  • the distribution webs which are angled backwards in the running direction from the prescaler basket, create a force component with the aid of which sufficient material is transported to the outside.
  • Fixed arms are attached to the end walls of the housing of the distributor zone and protrude axially into the cylindrical distributor basket. It is also achieved that the briquetting material arriving in the middle at the transition to the distribution zone is mixed again with the briquetting material emerging at the outer edges below. In this way, a possibly not yet uniform composition of the briquetted material is compensated for by simple means due to the different peripheral speeds distributed over the radius.
  • the part of the moving bed reactor with a vertical axis of rotation can, according to claim 6, in particular consist of an upper and a lower cylindrical region, the outer diameter in the upper region being about 1.5 to 5 times, preferably 1.5 to 3 times, so is as large as in the lower area and the transition area between the upper and lower area narrows in a funnel shape and the lower area of the moving bed reactor merges into the distribution zone without constriction.
  • the horizontally rotating stirrer arms in the upper region have approximately 1.5 to 5 times, preferably 1.5 to 3 times, the amount compared to the stirrer arms in the lower region. With the help of this device, a different average speed of the briquetted material is achieved at the same angular velocity in the upper and lower region.
  • a much higher speed is provided in the upper area for mixing the insert components. Due to the considerably larger diameter of the moving bed reactor in the upper area, there is also a considerably larger outlet area for the degassing gas escaping upwards, so that the outlet velocity of this gas can be kept relatively low. This ensures that only very small amounts of fine dust particles are entrained by the degassing gas.
  • FIG. 1 shows the moving bed reactor with the upper and lower region (2, 4) and the distributor zone (5) directly adjoining it at the bottom as well as the two double roller presses (1a, 1b).
  • the components with different temperatures are introduced into the moving bed reactor via at least two inlet openings (20).
  • the drive (15) of which is arranged above the moving bed reactor, the horizontal stirring arms (3) are fastened uniformly at different heights.
  • the outlet opening (19) for the degassing gas is also arranged in the upper cover of the moving bed reactor.
  • the vertical agitation axis (16) is guided at the bottom in the bearings (17) and (18), which are supported on the inside by the walls of the traveling reactor.
  • the briquetted material arrives directly in the distribution zone (5), in which a distribution basket (6) rotates about a horizontal axis of rotation (22).
  • the distributor basket (6) is equipped on the circumference with a series of distributor webs (7), with the aid of which the brittling material is pressed into the lower lateral outlet opening (10) and is distributed evenly over the length of the rollers.
  • the distributor webs (7) are bent in the middle and angled at the ends in the direction of rotation of the distributor basket (6) to the rear. It is thereby advantageously achieved that the briquetting material is also exchanged in the axial direction of the distributor basket.
  • the two rollers are also arranged in plan view. On the one hand, they consist of a fixed roller (1 a) and a loose roller (1b) which can be moved in the radial direction and which is pressed against the fixed roller with a specific, adjustable contact pressure.
  • the dies (21) for the briquettes are arranged on the circumference of the rollers.
  • the distributor zone (5) is shown again in itself, in particular one can see the storage of the distributor basket and the connection of the distributor webs with the central drive axis. Below the distributor basket, the amount of the briquetted material is adjusted using the control flap (12), which rotates about the axis of rotation (13). At the ends of the rollers there are closure flaps (11) which are attached at (14).
  • (23), (24) and (25) denote the fixed arms directed from the outer wall of the moving bed reactor in the radial direction and (26) the inwardly directed arms in the axial direction. They can either be distributed uniformly around the circumference of the moving bed reactor or else only on one side, as shown in FIG. 1.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Coke Industry (AREA)

Abstract

Process for producing briquette material for hot briquetting by pyrolytic decomposition of agglutinated coal mixed with thermally stable substances at a temperature comprised between 450 and 530oC, and appropriate units for implementing such process. In a moving bed reactor (2, 4, 5), the briquette material, which is more accurately defined in the generic term of the main claim and which is formed by pyrolytic decomposition of the agglutinated coal part, is maintained in a continuous mixing and kneading motion. The briquette material is first moved into a rotary mixing and kneading motion substantially parallel to the roller axes and falls at an average speed which is lower than 3 cm/s by gravity before it is finally evenly distributed throughout the width of the rolls in a substantially perpendicular rotation motion.

Description

Die Erfindung bezieht sich auf ein Verfahren zur Herstellung eines Brikettiergutes für die Heißbrikettierung durch pyrolytische Zersetzung backender Steinkohlen im Gemisch mit dem zwei- bis fünffachen Volumen feinkörniger, thermisch weitgehend stabiler Stoffe und auf eine Vorrichtung zur Durchführung des Verfahrens.The invention relates to a method for producing a briquette for hot briquetting by pyrolytic decomposition of baking hard coal in a mixture with two to five times the volume of fine-grained, thermally largely stable substances and to an apparatus for carrying out the method.

Bekannt ist ein derartiges Verfahren zur Herstellung eines Brikettiergutes aus der GB-A-1 168 283, die sich auf die Prioritätsanmeldungen DE-A-1571710 und 1671377 stützt. Die in diesen beiden Schriften beschriebenen Verfahren beziehen sich insbesondere auf Maßnahmen zur Erreichung eines bestimmten Maßes der Urteerausbeute des Brikettiergutes zum Zeitpunkt der Verformung. Die Urteerausbeute soll dabei gemäß der DE-A-15 71 710 bei einem Betrag von 0,2 bis 0,8% liegen und gemäß der DE-A-16 71 377 zwischen 0,07 und 0,2%. Man hat es sich dabei vor allem zur Aufgabe gesetzt, die maximal mogliche Entteerung des Brikettiergutes zu erreichen. Als wichtige Verfahrensmerkmale werden dabei bereits Mischtemperaturen mit 450°C bis 530°C und eine Verweilzeit des Brikettiergutes von 1 bis 15 Minuten genannt. Es hat sich dabei gezeigt, daß nicht immer ein gleichmäßig durchmischtes Brikettiergut zur Brikettierung gelangt, und insbesondere ist der Entgasungs- und Entteerungsgehalt nicht immer gleichbleibend. Das wirkt sich bei Brikettierpressen mit größerer Walzenbreite bereits als nachteilig aus.Such a method for producing a briquette is known from GB-A-1 168 283, which is based on priority applications DE-A-1571710 and 1671377. The methods described in these two documents relate in particular to measures to achieve a certain level of the Urteer yield of the briquetted material at the time of deformation. According to DE-A-15 71 710, the yield from Urteer should amount to 0.2 to 0.8% and according to DE-A-16 71 377 between 0.07 and 0.2%. The main task was to achieve the maximum possible de-emptying of the briquetted goods. Mixing temperatures of 450 ° C to 530 ° C and a residence time of the briquetted material of 1 to 15 minutes are already mentioned as important process features. It has been shown that briquetting does not always result in a uniformly mixed briquetting product, and in particular the degassing and de-emptying content is not always constant. This already has a disadvantage in briquetting presses with a larger roller width.

Bei dem Verfahren nach der GB-A-1 168 283 werden die Feststoffkomponenten in einen Behälter eingeschleust, in dem die Durchmischung und Entgasung stattfindet. Der Behälter enthält ein Rührwerk mit senkrecht stehender Achse. Nach Verlassen des Rührwerkes wird das Brikettiergut über einen Zuteiler nach Art eines Zellenrades, der sich um eine waagerechte Achse dreht, auf die Walzenpresse aufgegeben. Dieser Zuteiler ist dabei nicht näher beschrieben.In the process according to GB-A-1 168 283, the solid components are introduced into a container in which the mixing and degassing takes place. The container contains an agitator with a vertical axis. After leaving the agitator, the briquetted material is fed to the roller press via a feeder in the manner of a cellular wheel, which rotates about a horizontal axis. This allocator is not described in detail.

Aufgabe der Erfindung ist es also, ein Verfahren und eine Vorrichtung zur Durchführung dieses Verfahrens vorzuschlagen, mit dem ein Brikettiergut möglichst gleichmäßiger Konsistenz für die Heißbrikettierung hergestellt wird, wobei dieses Brikettiergut gleichmäßig auf die Walzenbreite von mehr als 400 mm verteilt wird, es immer zu Briketts einheitlicher Konsistenz und Festigkeit kommt und auch sehr hohe Durchsatzleistungen von mehr als 7 t/h bis hin zu etwa 70 t/h erreicht werden.The object of the invention is therefore to propose a method and a device for carrying out this method, with which a briquetted good consistency for the hot briquetting is produced, this briquetted material being evenly distributed over the roller width of more than 400 mm, always briquettes uniform consistency and strength and very high throughput rates of more than 7 t / h up to about 70 t / h can be achieved.

Diese Aufgabe wird erfindungsgemäß durch die Merkmale des Hauptanspruches gelöst. Die Verfahrensvorschläge nach den Ansprüchen 2 bis 4 sind zweckmäßige Ergänzungen dazu. In den Ansprüchen 5 bis 7 sind darüber hinaus besonders günstige Vorrichtungen zur Durchführung dieses Verfahrens beansprucht.This object is achieved by the features of the main claim. The proposed methods according to claims 2 to 4 are useful additions. In addition, particularly favorable devices for carrying out this method are claimed in claims 5 to 7.

Es hat sich erfindungsgemäß gezeigt, daß es insbesondere auf den zeitlichen Ablauf bei der Herstellung des Brikettiergutes für die Heißbrikettierung innerhalb der verschiedenen Zonen ankommt. Zunächst ist es erforderlich, daß die Einzelkomponenten mit den verschiedenen Temperaturen sehr schnell und sehr wirksam miteinander vermischt werden und daß sie im gesamten Wanderbettreaktor ausreichend Zeit zur Pyrolyse besitzen.It has been shown according to the invention that the timing in the production of the briquetting material for hot briquetting within the different zones is particularly important. First of all, it is necessary that the individual components with the different temperatures are mixed very quickly and very effectively and that they have sufficient time for pyrolysis in the entire moving bed reactor.

Dabei sollte das Brikettiergut im Wanderbettreaktor eine bestimmte Zeit verweilen, da einerseits eine ausreichende Pyrolyse und Entgasung stattfinden muß-denn ungenügend entgastes, speziell entteertes Brikettiergut neigt dazu, nach dem Verpressen wieder zu zerplatzen-, andererseits besteht bei zu stark entgastem Produkt die Gefahr, daß die Fettkohle ihre Bindefähigkeit verliert und das Produkt versandet und damit zu extrem hohem Abrieb neigt. Schließlich sollte erfindungsgemäß das Brikettiergut in einer bestimmten Zeit mit bestimmten Maßnahmen gleichmäßig auf die gesamte Brikettierwalzenbreite verteilt werden.The briquetted material should remain in the moving bed reactor for a certain time, since on the one hand sufficient pyrolysis and degassing must take place - because insufficiently degassed, specially de-emptied briquette material tends to burst again after pressing, on the other hand there is a risk that the product that is too strongly degassed will The fat coal loses its binding ability and the product silted up and thus tends to extremely high abrasion. Finally, according to the invention, the briquetted material should be uniformly distributed over the entire briquetting roller width in a certain time using certain measures.

Durch das Wechselspiel der Misch- und Knetbewegung in waagerechter Richtung mit der anschließenden, um 90° gedrehten Rotationsbewegung, bei der das Durchmischen und Kneten ebenfalls durch die feststehenden Arme verstärkt wird, wird eine sehr gleichmäßige Konsistenz des Brikettiergutes über der gasamten Walzenbreite erreicht. Dabei wird außerdem die frühzeitige Wiederverfestigung des Brikettiergutes verhindert, so daß auch Doppelwalzenpressen mit Walzenbreiten von weit mehr als 400 mm und sehr hohen Durchsatzleistungen gleichmäßig beaufschlagt werden können.Through the interplay of the mixing and kneading movement in the horizontal direction with the subsequent rotation movement rotated by 90 °, in which the mixing and kneading is also reinforced by the fixed arms, a very uniform consistency of the briquetted material is achieved over the entire width of the roller. This also prevents the briquetting material from reconsolidating at an early stage, so that double-roller presses with roller widths of more than 400 mm and very high throughput rates can also be applied uniformly.

Es hat sich erfindungsgemäß als zweckmäßig erwiesen, die Misch- und Knetbewegung durch mindestens ein Rührwerk zu erzeugen, dessen Rührarme eine mittlere Umfangsgeschwindigkeit von 1 bis 4 m/s haben und daß gleichzeitig die unteren, um eine nahezu waagerechte Achse rotierenden Rühr- und Verteilerarme eine Umfangsgeschwindigkeit von 0,5 bis 2,5 m/s haben. Von Vorteil ist es in diesem Zusammenhang auch, wenn das Verhältnis der Verweilzeiten für die parallel zu den Walzenachsen ausgeführte Misch- und Knetbewegung gegenüber der um 90° dazu gedrehten Bewegung mindestens 4:1 beträgt. Neben der Zusammensetzung der Einsatzkomponenten in dem Wanderbettreaktor sind die Drehbewegungen und das Verhältnis der Geschwindigkeit des Brikettiergutes in dem Wanderbettreaktor von entschiedender Bedeutung. Wenn man sich innerhalb der erfindungsgemäß angegebenen Grenzen bewegt, ist gewährleistet, daß ohne Betriebsstörungen aufgrund von Verstopfungen in jedem Fall nach Verlassen des Wanderbettreaktors ein brikettierfähiges Gemisch der Doppelwalzenpresse zugeleitet wird.It has proven to be advantageous according to the invention to generate the mixing and kneading movement by at least one agitator, the agitator arms of which have an average peripheral speed of 1 to 4 m / s, and that at the same time the lower agitator and distributor arms rotating about an almost horizontal axis Peripheral speed of 0.5 to 2.5 m / s. In this context, it is also advantageous if the ratio of the dwell times for the mixing and kneading movement carried out parallel to the roller axes is at least 4: 1 compared to the movement rotated through 90 °. In addition to the composition of the feed components in the moving bed reactor, the rotary movements and the ratio of the speed of the briquetting material in the moving bed reactor are of crucial importance. If one moves within the limits specified according to the invention, it is ensured that a briquettable mixture is fed to the double roller press in any case after leaving the moving bed reactor without operational disturbances due to blockages.

Es hat sich als günstig erwiesen, bei einer Preßleistung von mehr als 12 t/h die Gesamtverweilzeit im Wanderbettreaktor unter 8 Minuten zu halten. Bei den erfindungsgemäß vorgeschlagenen Geschwindigkeiten ist auch bei derartigen Pressenleistungen einerseits eine ausreichende Entgasung gewährleistet und andererseits kommt es zu keinerlei Verstopfungen im Wanderbettreaktor.It has proven to be favorable to keep the total residence time in the moving bed reactor below 8 minutes at a pressing capacity of more than 12 t / h. At the speeds proposed according to the invention, adequate degassing is ensured on the one hand even with such press outputs and on the other hand comes there are no blockages in the moving bed reactor.

Nach Anspruch 4 soll schließlich das Brikettiergut in einem gegen die Atmosphäre der Pressenkammer abgedichteten Raum vorverdichtet werden und gleichmäßig auf die gesamte Walzenbreite verteilt werden. Im Aufgabebereich des Brikettiergutes auf die Doppelwalzenpresse wird ein Eindringen von Luft und damit das Entstehen eines explosionsfähigen Gemisches verhindert. Am Austritt aus der Doppelwalzenpresse fallen die Briketts in einen offenen Raum, so daß eine einfache Überwachung der Presse möglich ist.According to claim 4, the briquetted material should finally be pre-compressed in a space sealed against the atmosphere of the press chamber and distributed evenly over the entire width of the roller. In the feed area of the briquetted material on the double roller press, air penetration and thus the formation of an explosive mixture is prevented. At the exit from the double roller press, the briquettes fall into an open space so that the press can be easily monitored.

Zur Durchführung des Verfahrens wird ein Wanderbettreaktor vorgesehen, der aus einem Behälter besteht, in dem ein oder mehrere Rührwerke mit senkrechter Drehachse und waagerechten Rührarmen angeordnet sind und dessen Verteilerzone unten aus einem Verteiler mit waagerechter zentraler Drehachse besteht, wobei zur Erreichung einer intensiven Misch- und Knetbewegung in der Verteilerzone erfindungsgemäß vorgeschlagen wird, daß an den Stirnwänden des Gehäuses der Verteilerzone feststehende Arme angebracht sind, die in axialer Richtung in den zylinderförmigen Verteilerkorb hineinragen.To carry out the process, a moving bed reactor is provided, which consists of a container in which one or more agitators with a vertical axis of rotation and horizontal agitator arms are arranged and whose distribution zone below consists of a distributor with a horizontal central axis of rotation, with the aim of achieving an intensive mixing and Kneading movement in the distribution zone is proposed according to the invention that fixed arms are attached to the end walls of the housing of the distribution zone, which project in the axial direction into the cylindrical distributor basket.

Von besonderer Bedeutung zur Verteilung des Brikettiergutes in der Verteilerzone auf die gesamte Breite der Walzen ist dabei die Anzahl und Form der Verteilerstege, die in Drehrichtung in der Mitte, d.h. bei halber Länge des Verteilerkorbes, voreilen und zu ihren Enden hin nach hinten abgebogen oder abgewinkelt sind. Durch die von dem Vorteilerkorb in Laufrichtung rückwärts abgewinkelten Verteilerstege entsteht eine Kraftkomponente, mit deren Hilfe genügend Material zu den Außenseiten hin transportiert wird. An den Stirnwänden des Gehäuses der Verteilerzone sind feststehende Arme angebracht, die in axialer Richtung in den zylinderförmigen Verteilerkorb hineinragen. Außerdem wird erreicht, daß nochmals eine Vermischung des in der Mitte am Übergang zur Verteilerzone ankommenden Brikettiergutes mit dem an den Außenrändern unten austretenden Brikettiergut erfolgt. Auf diese Weise wird eine eventuell noch nicht gleichmäßige Zusammensetzung des Brikettiergutes aufgrund der unterschiedlichen Umfangsgeschwindigkeiten über den Radius verteilt mit einfachen Mitteln ausgeglichen.Of particular importance for the distribution of the briquetted material in the distribution zone over the entire width of the rollers is the number and shape of the distributor webs, which in the direction of rotation in the middle, i.e. at half the length of the distributor basket, advance and are bent or angled towards the ends. The distribution webs, which are angled backwards in the running direction from the prescaler basket, create a force component with the aid of which sufficient material is transported to the outside. Fixed arms are attached to the end walls of the housing of the distributor zone and protrude axially into the cylindrical distributor basket. It is also achieved that the briquetting material arriving in the middle at the transition to the distribution zone is mixed again with the briquetting material emerging at the outer edges below. In this way, a possibly not yet uniform composition of the briquetted material is compensated for by simple means due to the different peripheral speeds distributed over the radius.

Der Teil des Wanderbettreaktors mit senkrechter Drehachse kann gemäß Anspruch 6, insbesondere aus einem oberen und einem unteren zylinderförmigen Bereich bestehen, wobei der Außendurchmesser im oberen Bereich etwa 1,5- bis 5- mal, vorzugsweise 1,5- bis 3-mal, so groß ist wie im unteren Bereich und der Übergangsbereich zwischen dem oberen und unteren Bereich sich trichterförmig verengt und der untere Bereich des Wanderbettreaktors ohne Einschnürung in die Verteilerzone übergeht. Günstig ist es dabei, wenn die waagerecht rotierenden Rührarme im oberen Bereich etwa die 1,5- bis 5-fache, vorzugsweise 1,5- bis 3-fache, Menge gegenüber den Rührarmen im unteren Bereich haben. Mit Hilfe dieser Vorrichtung wird bei gleicher Winkelgeschwindigkeit im oberen und unteren Bereich eine unterschiedliche mittlere Geschwindigkeit des Brikettiergutes erreicht. Zur Vermischung der Einsatzkomponenten ist dabei im oberen Bereich eine sehr viel höhere Geschwindigkeit vorgesehen. Durch den erheblich größeren Durchmesser des Wanderbettreaktors im oberen Bereich ist auch eine erheblich größere Austrittsfläche für das nach oben austretende Entgasungsgas vorhanden, so daß die Austrittsgeschwindigkeit dieses Gases relativ gering gehalten werden kann. Dadurch ist gewährleistet, daß nur sehr geringe Mengen an Feinstaubpartikeln von dem Entgasungsgas mitgerissen werden.The part of the moving bed reactor with a vertical axis of rotation can, according to claim 6, in particular consist of an upper and a lower cylindrical region, the outer diameter in the upper region being about 1.5 to 5 times, preferably 1.5 to 3 times, so is as large as in the lower area and the transition area between the upper and lower area narrows in a funnel shape and the lower area of the moving bed reactor merges into the distribution zone without constriction. It is advantageous if the horizontally rotating stirrer arms in the upper region have approximately 1.5 to 5 times, preferably 1.5 to 3 times, the amount compared to the stirrer arms in the lower region. With the help of this device, a different average speed of the briquetted material is achieved at the same angular velocity in the upper and lower region. A much higher speed is provided in the upper area for mixing the insert components. Due to the considerably larger diameter of the moving bed reactor in the upper area, there is also a considerably larger outlet area for the degassing gas escaping upwards, so that the outlet velocity of this gas can be kept relatively low. This ensures that only very small amounts of fine dust particles are entrained by the degassing gas.

In Anspruch 7 sind schließlich noch zweckmäßige Ausführungsformen für den Querschnitt am Übergang zur Verteilerzone angegeben.In claim 7 finally expedient embodiments are given for the cross section at the transition to the distribution zone.

Die Erfindung wird anhand er beigefügten Figuren 1 bis 4 beispielsweise näher erläutert;

  • Figur 1 zeigt die erfindungsgemäße Vorrichtung des Wanderbettreaktors mit oberem und unteren Bereich der Pyrolysezone und der Verteilzone sowie den beiden Walzenpressen.
  • Figur 2 und Figur 3 zeigen im Querschnitt und Längsschnitt die Verteilerzone mit der Verteilkorb und den darunter angeordneten Regelklappen.
  • Figur 4 ist eine Draufsicht auf die Verteilzone, wobei das Gehäuse geöffnet ist und der Verteilerkorb mit den am Ende abgewinkelten Verteilerstegen zu sehen ist.
The invention is explained in more detail with reference to the accompanying FIGS. 1 to 4;
  • Figure 1 shows the device according to the invention of the moving bed reactor with the upper and lower region of the pyrolysis zone and the distribution zone and the two roller presses.
  • Figure 2 and Figure 3 show in cross section and longitudinal section the distribution zone with the distribution basket and the control flaps arranged below.
  • FIG. 4 is a plan view of the distribution zone, the housing being open and the distributor basket with the distributor webs angled at the end being visible.

BezugszeichenlisteReference symbol list

  • (1a) Festwalze der Doppelwalzenpresse(1a) Fixed roller of the double roller press
  • (1 b) Loswalze der Doppelwalzenpresse . (1 b) loose roller of the double roller press .
  • (2) oberer, erweiterter Bereich der Misch- und Knetzone des Wanderbettreaktors(2) Upper, expanded area of the mixing and kneading zone of the moving bed reactor
  • (3) Rührarme(3) stirring arms
  • (4) unterer Bereich der Misch- und Knetzone des Wanderbettreaktors(4) lower area of the mixing and kneading zone of the moving bed reactor
  • (5) Verteilerzone des Wanderbettreaktors(5) Distribution zone of the moving bed reactor
  • (6) Verteilerkorb(6) Distribution basket
  • (7) Verteilerstege(7) Manifolds
  • (8) Drehrichtung von (6)(8) Direction of rotation of (6)
  • (9) nach hinten abgewinkelte Enden von (7)(9) angled ends of (7)
  • (10) Auslaßöffnung aus (5)(10) outlet opening from (5)
  • (11) Verschlußklappen an den Enden der Walzen(11) Flaps on the ends of the rollers
  • (12) Regelklappe(12) control flap
  • (13) Drehachse von (12)(13) axis of rotation of (12)
  • (14) Befestigung von (11)(14) fastening of (11)
  • (15) Antrieb für die Rührarme(15) Drive for the stirring arms
  • (16) senkrechte Achse für die Rührarme(16) vertical axis for the mixing arms
  • (17) untere Lagerung von (16)(17) lower storage of (16)
  • (18) untere Lagerung von (16)(18) lower storage of (16)
  • (19) Einlaßöffnung für die Mischkomponenten(19) Inlet opening for the mixing components
  • (20) Austrittsöffnungen für das Entgasungsgas(20) Outlets for the degassing gas
  • (21) Matrizen am Umfang der Brikettierwalzen (1a,1b)(21) Matrices on the circumference of the briquetting rollers (1a, 1b)
  • (22) Antriebsachse des Verteilerkorbes(22) Drive axis of the distributor basket
  • (23) feststehende Arme(23) fixed arms
  • (24) feststehende Arme(24) fixed arms
  • (25) feststehende Arme(25) fixed arms
  • (26) feststehende Arme(26) fixed arms

In der schematischen Zusammenstellung der Figur 1 ist der Wanderbettreaktor mit dem oberen und unteren Bereich (2, 4) und der unten direkt daran anschließenden Verteilerzone (5) sowie den beiden Doppelwalzenpressen (1a, 1b) dargestellt. Über mindestens zwei Einlaßöffnungen (20) werden die Komponenten mit unterschiedlichen Temperaturen in den Wanderbettreaktor gegeben. Am Umfang der senkrechten Drehachse (16), deren Antrieb (15) oberhalb des Wanderbettreaktors angeordnet ist, sind die waagerechten Rührarme (3) gleichmäßig in verschiedenen Höhen befestigt. Im oberen Deckel des Wanderbettreaktors ist außerdem die Austrittsöffnung (19) für das Entgasungsgas angeordnet. Die senkrecht Rührachse (16) ist unten in den Lagern (17) und (18), die sich innen an den Wandungen des Wanderreaktors abstützen, geführt. Aus der Misch- und Knetzone gelangt das Brikettiergut direkt in die Verteilerzone (5), in der ein Verteilerkorb (6) sich um eine waagerechte Drehachse (22) dreht. Der Verteilerkorb (6) ist am Umfang mit einer Reihe von Verteilerstegen (7) ausgerüstet, mit deren Hilfe das Brittiergut in die seitliche untere Austrittsöffnung (10) gedrückt wird und auf die Länge der Walzen gleichmäßig verteilt wird. Wie aus der Figur 4, insbesondere in der Draufsicht, ersichtlich ist, sind die Verteilerstege (7) in der Mitte geknickt und an den Enden in Drehrichtung des Verteilerkorbes (6) nach hinten abgewinkelt. Dadurch wird in vorteilhafter Weise erreicht, daß auch eine Austausch des Brikettiergutes in axialer Richtung des Verteilerkorbes erfolgt. In der Figur 4 sind ebenfalls die beiden Walzen in der Draufsicht angeordnet. Sie bestehen einerseits aus einer Festwalze (1 a) und einer in radialer Richtung verschiebbaren Loswalze (1b), die mit bestimmter einstellbarer Anpreßkraft gegen die Festwalze gedrückt wird. Auf dem Umfang der Walzen sind die Matrizen (21) für die Briketts angeordnet. In den Figuren 2 und 3 ist die Verteilerzone (5) noch einmal für sich dargestellt, wobei man insbesondere die Lagerung des Verteilerkorbes und die Verbindung der Verteilerstege mit der zentralen Antriebsachse erkennen kann. Unterhalb des Verteilerkorbes wird die Menge des Brikettiergutes mit Hilfe der Reglerklappe (12), die sich um die Drehachse (13) dreht, eingestellt. An den Enden der Walzen befinden sich Verschlußklappen (11), die bei (14) befestigt sind. Mit (23), (24) und (25) sind die von der Außenwand des Wanderbettreaktors in radialer Richtung und mit (26) die in axialer Richtung nach innen gerichteten feststehenden Arme bezeichnet. Sie können entweder gleichmäßig verteilt am Umfang des Wanderbettreaktors oder auch nur an einer Seite, wie in Figur 1 dargestellt, angeordnet sein.In the schematic compilation of the FIG. 1 shows the moving bed reactor with the upper and lower region (2, 4) and the distributor zone (5) directly adjoining it at the bottom as well as the two double roller presses (1a, 1b). The components with different temperatures are introduced into the moving bed reactor via at least two inlet openings (20). On the circumference of the vertical axis of rotation (16), the drive (15) of which is arranged above the moving bed reactor, the horizontal stirring arms (3) are fastened uniformly at different heights. The outlet opening (19) for the degassing gas is also arranged in the upper cover of the moving bed reactor. The vertical agitation axis (16) is guided at the bottom in the bearings (17) and (18), which are supported on the inside by the walls of the traveling reactor. From the mixing and kneading zone, the briquetted material arrives directly in the distribution zone (5), in which a distribution basket (6) rotates about a horizontal axis of rotation (22). The distributor basket (6) is equipped on the circumference with a series of distributor webs (7), with the aid of which the brittling material is pressed into the lower lateral outlet opening (10) and is distributed evenly over the length of the rollers. As can be seen from FIG. 4, in particular in a top view, the distributor webs (7) are bent in the middle and angled at the ends in the direction of rotation of the distributor basket (6) to the rear. It is thereby advantageously achieved that the briquetting material is also exchanged in the axial direction of the distributor basket. In Figure 4, the two rollers are also arranged in plan view. On the one hand, they consist of a fixed roller (1 a) and a loose roller (1b) which can be moved in the radial direction and which is pressed against the fixed roller with a specific, adjustable contact pressure. The dies (21) for the briquettes are arranged on the circumference of the rollers. In Figures 2 and 3, the distributor zone (5) is shown again in itself, in particular one can see the storage of the distributor basket and the connection of the distributor webs with the central drive axis. Below the distributor basket, the amount of the briquetted material is adjusted using the control flap (12), which rotates about the axis of rotation (13). At the ends of the rollers there are closure flaps (11) which are attached at (14). (23), (24) and (25) denote the fixed arms directed from the outer wall of the moving bed reactor in the radial direction and (26) the inwardly directed arms in the axial direction. They can either be distributed uniformly around the circumference of the moving bed reactor or else only on one side, as shown in FIG. 1.

Claims (7)

1. Process for the production of a briquetting material for hot briquetting by pyrolitic decomposition of agglutinating hard coals mixed with two to five times the volume of fine-grained, largely thermally stable substances such as anthracite, lean coal, petroleum coke, coke breeze, sand, metal ores, phosphates, fine-grained metal oxides etc., while below a temperature of 650°C do not agglutinate and do not, or only insignificantly, soften, at a temperature ranging approximately between 450 and 530°C which is obtained by mixing the predried and/or preheated agglutinating coal, with preheating only taking place until the temperature of softening is just about reached, with the largely thermally stable substances of suitably higher initial temperature, the mixed material being pyroliti- cally decomposed, detarred in a moving bed reactor with agitating means and subsequently distributed over the width of a double roller press (1a/1b), and the briquetting material forming in a moving bed reactor by the pyrolitic decomposition of the caking hard coal portion is, during its forming phase, first maintained in a rotary mixing and kneading motion caused by rotating (3,7) and stationary (23 to 26) arms substantially parallel to the roller axes (1a/1b) and at the end in a rotary motion almost perpendicular to the roller axes until the detarred finished briquetting material immediately following its last rotational motion is pressed into the feed gap of the more than 400 mm wide roller press by bars (7) arranged parallel to the rotational axis.
2. Process for the production of a briquetting material for hot briquetting by pyrolitic decomposition in a moving bed reactor according to claim 1 characterized in that the rotary mixing and kneading motion substantially parallel to the roller axes (1a/1b) is produced by at least one agitator unit whose agitating arms (3) having a mean circumferential speed to 1 to 4 m/s and that the lower agitating and distribution arms (7) rotating about an almost horizontal axis have a circumferential speed of 0.5 to 2.5 m/s.
3. Process for the production of a briquetting material for hot briquetting by pyrolitic decomposition in a moving bed reactor according to claim 1 or 2 characterized in that the mixing and kneading motion carried out substantially parallel to the roller axes (1 a/1 b) amounts to at least 4/5 of the total retention time in the moving bed reactor.
4. Process for the production of a briquetting material for hot briquetting by pyrolitic decomposition in a moving bed reactor according to one of the aforementioned claims 1 to 3 characterized in that the briquetting material is pressed downward from the distribution zone (5) of the moving bed reactor into a space sealed against the atmosphere of the press compartment from where the partially degassed and pre-compacted briquetting material is fed to briquetting gap in an almost even distribution over the entire width of the rollers.
5. Unit for the implementation of a process according to the above mentioned claims with a moving bed reactor which consists of one tank in which one or several agitating units are arranged with a vertical rotational axis (16) and horizontal agitating arms (3) and whose distribution zone (5) comprises a cylindrical distribution basket with horizontal central rotational axis, and with stationary arms (26) being attached to the front walls of the housing of the distribution zone (5) which project into the cylindrical distribution basket (6) in axial direction, and the cylindrical distribution basket (6) having at least 3, preferably 6 to 8, distribution bars (7) arranged in axial direction which in the direction of rotation (8) are leading in the middle in an arc-shaped manner and/or are provided with one or several angles bent backwards towards the ends (9).
6. Unit according to claim 5 characterized in that the portion of the moving bed reactor with perpendicular rotational axis (16) consists of an upper (2) and a lower (4) cylindrical area with the outer diameter in the upper area (2) being about 1.5 to 5 times, preferably 1.5 to 3 times, as large as that in the lower area (4) and the transitional area between the upper (2) and lower (4) area being necked down in a funnel shaped manner and that the lower area (2) of the moving bed reactor passes into the distribution zone (5) without neckdown.
7. Unit for the implementation of the process according to one or several of the above claims characterized in that the lower cross sectional area of the moving bed reactor at the point of transition to the distribution zone (5) is of round or oval shape and that the diameter of the round cross section or the length of the oval cross section roughly corresponds to the width of the briquetting roller.
EP84903714A 1983-09-06 1984-09-04 Process and unit for producing briquette material for hot briquetting Expired - Lifetime EP0155318B1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84903714T ATE53227T1 (en) 1983-09-06 1984-09-04 PROCESS AND DEVICE FOR THE MANUFACTURE OF BRIQUETTE PRODUCTS FOR HOT BRIQUETTE.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3332053 1983-09-06
DE19833332053 DE3332053A1 (en) 1983-09-06 1983-09-06 METHOD AND DEVICE FOR PRODUCING A BRIKETTING GOOD FOR HOT BRIKETTING

Publications (2)

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EP0155318A1 EP0155318A1 (en) 1985-09-25
EP0155318B1 true EP0155318B1 (en) 1990-05-30

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EP84903714A Expired - Lifetime EP0155318B1 (en) 1983-09-06 1984-09-04 Process and unit for producing briquette material for hot briquetting

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US (1) US4601728A (en)
EP (1) EP0155318B1 (en)
JP (1) JPH0631361B2 (en)
AU (1) AU562571B2 (en)
BR (1) BR8407057A (en)
CA (1) CA1231668A (en)
DE (1) DE3332053A1 (en)
ES (1) ES8504908A1 (en)
GB (1) GB2157312B (en)
IN (1) IN162692B (en)
WO (1) WO1985001061A1 (en)
ZA (1) ZA847025B (en)

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US4696634A (en) * 1985-06-06 1987-09-29 Triple "F", Inc. Apparatus for particulating an oleaginous product
DE3809616C1 (en) * 1988-03-22 1989-05-24 Laborlux S.A., Esch-Sur-Alzette, Lu
DE4003342A1 (en) * 1990-02-05 1991-08-08 Koeppern & Co Kg Maschf Roller press for aerated solids - extracts surplus air into angled collector chambers laterally of vertical pass-line
JPH08503737A (en) * 1993-09-30 1996-04-23 マシネンファブリーク・ケッパーン・ゲゼルシャフト・ミット・ベシュレンクテル・ハフツング・ウント・コンパニー・コマンデイト・ゲゼルシャフト Method for producing spongy iron briquettes from fine-grained ore
US6719956B1 (en) 2000-09-15 2004-04-13 Siddhartha Gaur Carbonaceous material products and a process for their production
US8906336B2 (en) * 2000-09-15 2014-12-09 Siddhartha Gaur Blast furnace metallurgical coal substitute products and method
US8753410B2 (en) 2009-02-17 2014-06-17 University Of Kentucky Research Foundation Method for producing fuel briquettes from high moisture fine coal or blends of high moisture fine coal and biomass
CN107583492A (en) * 2017-10-30 2018-01-16 深圳润丰投资咨询有限公司 A kind of feed stirring-granulating device
WO2019159119A1 (en) 2018-02-15 2019-08-22 Flsmidth A/S Comminution device feed mechanism and method
CN110898777A (en) * 2019-12-09 2020-03-24 潘苗妃 Improved generation reation kettle
CN111992136A (en) * 2020-08-24 2020-11-27 程亮 Probiotics fodder granulating device

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BE699931A (en) * 1966-06-15 1967-12-14
DE1671377C3 (en) * 1967-05-19 1975-07-31 Eschweiler Bergwerks-Verein, 5122 Kohlscheid Process for the production of compacts, in particular fuel briquettes
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JPS56160900A (en) * 1980-05-16 1981-12-10 Mitsubishi Heavy Ind Ltd Briquette machine

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Publication number Publication date
AU3504384A (en) 1985-03-29
DE3332053C2 (en) 1992-09-17
GB2157312A (en) 1985-10-23
AU562571B2 (en) 1987-06-11
GB8511229D0 (en) 1985-06-12
JPS61500070A (en) 1986-01-16
DE3332053A1 (en) 1985-03-21
ES535664A0 (en) 1985-05-16
EP0155318A1 (en) 1985-09-25
BR8407057A (en) 1985-08-13
CA1231668A (en) 1988-01-19
ZA847025B (en) 1985-06-26
IN162692B (en) 1988-07-02
JPH0631361B2 (en) 1994-04-27
US4601728A (en) 1986-07-22
GB2157312B (en) 1987-11-04
ES8504908A1 (en) 1985-05-16
WO1985001061A1 (en) 1985-03-14

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