EP0329705B1 - Process and device for the cooling of and the removal of dust from high-temperature coke - Google Patents
Process and device for the cooling of and the removal of dust from high-temperature coke Download PDFInfo
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- EP0329705B1 EP0329705B1 EP87907757A EP87907757A EP0329705B1 EP 0329705 B1 EP0329705 B1 EP 0329705B1 EP 87907757 A EP87907757 A EP 87907757A EP 87907757 A EP87907757 A EP 87907757A EP 0329705 B1 EP0329705 B1 EP 0329705B1
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- coke
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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
- C10B39/00—Cooling or quenching coke
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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
- C10B39/00—Cooling or quenching coke
- C10B39/02—Dry cooling outside the oven
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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
- C10B39/00—Cooling or quenching coke
- C10B39/04—Wet quenching
Definitions
- the invention relates to a method of cooling and dedusting of Kochtemperaturkoks in at least two stages, where the coke is cooled in the first stage to below about 800 o C, and to apparatus for performing the method with the features in the preamble of claim. 8
- DE-OS 25 33 606 a two-step process is described for cooling of coke, wherein said coke is cooled initially in giving current with the aid of an inert gas in a first closed container of 1100 o C to about 315-425 o C and thereafter in a sprayed closed container with water and the evaporation of the water to reduce the temperature of the coke to 95 to 150 o C.
- the steam rises and entrains dust particles, so that the exhaust gases have to be cleaned before being released into the atmosphere.
- the object of the invention is to improve the generic method for cooling and dedusting high-temperature coke and the device for carrying out the method in such a way that the environmental problems, in particular the dust problems when loading the coke, are largely eliminated and that the method is furthermore for coke dry cooling is simplified in view of a cheaper design.
- the energy of the coke is sometimes used considerably less in the first stage and therefore less steam is generated than in other known processes.
- This is particularly useful for coke oven plants, at who lack the ability to deliver large quantities of high-tension steam to external consumers.
- the actual coke dry cooling chamber can be provided smaller and in particular with a much lower overall height.
- the coke temperature is lowered so far in the first stage before the water immersion that the gasification reactions proceeding accelerated at higher temperatures are largely suppressed in the process according to the invention.
- the hot coke can expediently only be indirectly cooled to approx. 600 o C and either give off the heat to cooling surfaces installed in the shaft or on a continuously rotating hot coke conveyor belt to radiation cooling surfaces arranged above and below the conveyor belt.
- a direct cooling with cooling gas counter-current of coke can be appropriately selected depending are cooled to about 400 o C by the quantity and temperature of the cooling gas under certain circumstances.
- the coke can be rapidly cooled below 800 o C, preferably to about 600-650 o C, by introducing hot steam at about 120 ° C., so that there is no gasification of the coke.
- the steam drawn off at approx. 500 to 600 o C can either be used for preheating coal or for generating high-pressure steam in a waste heat boiler.
- the coke can be continuously cooled in the first stage to the temperature of 200 to 800 ° C., preferably 400-650 ° C., mentioned above , and then added to the subsequent immersion container in a closed system.
- the coke is conveyed through a water bath in a short time, whereby due to the short dwell time of the coke in the water bath there is generally no complete heat exchange within the coke pieces between the grain surface and the grain interior. Therefore, the coke is then kept in a third stage in a closed post-evaporation tank.
- there is an intensive heat exchange within the coke bed between the interior of the grain and the grain surface whereby a large part of the water adhering to the surface is evaporated and drawn off.
- the intensive heat exchange is promoted by the released water vapor, which then flows through the coke bed and can also be circulated.
- the coke leaves the post-evaporation tank with a uniform temperature and water content which does not change significantly during further loading.
- dust particles can no longer loosen during the further treatment of the coke, so that dust emissions are avoided. Dipping times of less than 3 minutes, preferably 10 to 60 seconds, are sufficient to almost completely detach the coke dust adhering to the coke piece and to discharge it to the sewage treatment plant with the rinse water. The adhering coke dust is no longer carried into the subsequent evaporation container.
- the coke has a relatively low water content after leaving the post-evaporation tank, which is favorable for later use in the blast furnace.
- the temperature of the coke after leaving the Nachverdampfungs constituteers is preferably to 70 - 80 o C, so that an undesirable steam development during the further transport of the coke can be turned to open conveyors substantially below the evaporation temperature.
- the water vapor formation is relatively low in direct immersion.
- the water vapor can be drawn off from the closed container and processed in a simple manner on the raw gas cleaning side of the coking plant, preferably by introducing it into the raw gas receiver.
- Even in the immersion tank a large part of the water vapor is condensed again by constant sprinkling over the entire surface of the water basin. The same happens when the steam is introduced into the receiver with the help of the water sprinkling there.
- cold fresh water and cooled circulating water from the sewage treatment plant keep the water temperature in the plunge pool at approx. 60 to 80 o C, so that as much of the heat contained in the coke as possible is dissipated via the heating of the water and thus little water vapor is generated.
- a device according to claim 8 is proposed, wherein the coke discharge from the coke drying chute or the hot coke conveyor belt and the immersion tank and the downstream post-evaporation tank are each connected to one another in a gastight manner, so that no emissions occur when the coke is transferred from one tank to another can.
- the lower end of the filler neck can be immersed in the water of the immersion container and a dense coke bed can be kept in the entire filler neck and the outlet funnel.
- a backflow of water vapor can be prevented with the help of a butterfly valve in the absence of coke.
- the coke discharge device from the coke dry cooling can also be designed without the usual lock bunkers or gas-tight discharge locks.
- the discharge on non-gas-tight conveying bodies, such as. B. discharge rockers are limited.
- the antechamber (19) in the figure is filled with one or more coke transport bucket fillings in a manner known per se and the coke slides continuously over the coke feed (2) into the coke drying cooling shaft (1). There it gives off heat either indirectly to the cooling walls (6) and / or directly to the cooling gases, which are supplied or discharged via the connections (3/5) in countercurrent (solid arrows) or in direct current (dashed arrows). In the latter case, the Connection (3) about 120 o C hot water vapor for direct current cooling of the coke, which is drawn off at the lower end of the cooling chamber below the discharge rockers (20) via the cooling gas suction (5) at a temperature of 500 to 600 o C. After leaving the dry cooling zone, the coke has a temperature of approx.
- the residence time of the coke in the water immersion bath is determined by the speed of the coke conveyor (13), which is circulated around the deflection rollers (11) and expediently consists of a plate conveyor with sieve-shaped plates.
- the coke conveyor (13) there is a scraper conveyor (18), with the help of which the coke particles separated from the coke are transported to the water outlet (16).
- the coke conveyor (13) With the coke conveyor (13) the coke is brought directly into the gas-tight adjoining the immersion tank (8) subsequent evaporation tank (14), from which the coke after a certain time in a manner known per se, for. B. is withdrawn via locks or cellular wheels on the coke discharge (15).
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Die Erfindung bezieht sich auf ein Verfahren zur Kühlung und Entstaubung von Kochtemperaturkoks in mindestens zwei Stufen, wobei der Koks in der ersten Stufe auf unterhalb etwa 800 oC gekühlt wird, und auf Vorrichtungen zur Durchführung des Verfahrens mit den Merkmalen im Oberbegriff des Anspruches 8.The invention relates to a method of cooling and dedusting of Kochtemperaturkoks in at least two stages, where the coke is cooled in the first stage to below about 800 o C, and to apparatus for performing the method with the features in the preamble of claim. 8
In der DE-OS 25 33 606 ist ein zweistufiges Verfahren zum Kühlen von Koks beschrieben, wobei der Koks zunächst im Gebenstrom mit Hilfe eines Inertgases in einem ersten geschlossenen Behälter von 1.100 oC auf etwa 315 bis 425 oC gekühlt wird und danach in einem geschlossenen Behälter mit Wasser besprüht und durch die Verdampfung des Wassers die Temperatur des Kokses auf 95 bis 150 oC gesenkt werden soll. Ähnlich wie beim üblichen Naßlöschen unter dem Kokslöschturm steigt dabei der Dampf auf und reißt Staubpartikel mit, so daß die Abgase vor dem Ablassen in die Atmosphäre gereinigt werden müssen.In DE-OS 25 33 606, a two-step process is described for cooling of coke, wherein said coke is cooled initially in giving current with the aid of an inert gas in a first closed container of 1100 o C to about 315-425 o C and thereafter in a sprayed closed container with water and the evaporation of the water to reduce the temperature of the coke to 95 to 150 o C. Similar to the usual wet quenching under the coke quenching tower, the steam rises and entrains dust particles, so that the exhaust gases have to be cleaned before being released into the atmosphere.
Aus der DE-PS 35 23 897 ist schließlich ein Verfahren zur Kühlung und Entstaubung von Koks ersichtlich, wobei der Koks nach Verlassen der Kokstrockenkühlung mit einer Temperatur von ca. 150 bis 200 oC in einen Tauchbehälter mit einer Flüssigkeitstemperatur von ca. 100 oC gegeben und mit stufenlos regelbarer Geschwindigkeit aus dem Tauchbehälter herausbefördert und dabei vom Feinstaub befreit wird. Es hat sich hierbei gezeigt, daß der Koks und auch der abgetrennte Koksgrus nach Verlassen des Tauchbehälters noch erheblich ausdampft und es aufgrund des teilweise offenen Behälters zu einer Umweltbelastung kommen kann. Weiterhin kann es insbesondere bei extrem kurzen Tauchzeiten des Kokses von weniger als 30 Sekunden noch nicht zu einem vollständigen intensiven Wärmeaustausch innerhalb des Koksstückes zwischen Koksoberfläche und Koksinnerem kommen. Auf der nachfolgenden Fördereinrichtung führt daher, vor allem bei größeren Koksstücken, bei denen die Wasseraufnahme auf die oberflächennahen Kokspartien beschränkt bleibt, der Wärmeaustausch zu einer vollständigen Wasserverdampfung. Dadurch kann es zu einem ungleichmäßigen Wassergehalt der verschiedenen Koksstücke mit unterschiedlicher Größe kommen. Es hat sich gezeigt, daß sich bei der weiteren Handhabung des Kokses aus den vollständig abgetrockneten Koksstücken immer wieder Staubpartikel lösen, die Emissionsprobleme mit sich bringen.From DE-PS 35 23 897 a method for cooling and dedusting coke can finally be seen, the coke after leaving the coke dry cooling at a temperature of about 150 to 200 o C in an immersion container with a liquid temperature of about 100 o C. given and conveyed out of the immersion tank at infinitely variable speed and it is freed from fine dust. It has been shown here that the coke and also the separated coke breeze evaporates considerably after leaving the immersion container and that the partially open container can cause environmental pollution. Furthermore, especially with extremely short coke immersion times of less than 30 seconds, a complete intensive heat exchange within the coke piece between the coke surface and the interior of the coke cannot yet occur. On the subsequent conveyor, the heat exchange leads to complete water evaporation, especially in the case of larger pieces of coke, in which the water absorption is limited to the near-surface coke sections. This can lead to an uneven water content of the different pieces of coke with different sizes. It has been shown that during further handling of the coke, dust particles that release emission problems always come loose from the completely dried coke pieces.
Aufgabe der Erfindung ist es, das gattungsgemäße Verfahren zur Kühlung und Entstaubung von Hochtemperaturkoks und die Vorrichtung zur Durchführung des Verfahrens in der Weise zu verbessern, daß die Umweltschutzprobleme, insbesondere die Staubprobleme bei der Verladung des Kokses, weitgehend beseitigt werden und daß darüber hinaus das Verfahren zur Kokstrockenkühlung in Hinblick auf eine billigere Bauweise vereinfacht wird.The object of the invention is to improve the generic method for cooling and dedusting high-temperature coke and the device for carrying out the method in such a way that the environmental problems, in particular the dust problems when loading the coke, are largely eliminated and that the method is furthermore for coke dry cooling is simplified in view of a cheaper design.
Zur Lösung dieser Aufgabe werden die im Kennzeichen des ersten Anspruches aufgeführten Verfahrensmerkmale vorgeschlagen. Die Unteransprüche 2 bis 7 enthalten sinnvolle AuSführungsmerkmale dazu. In den Ansprüchen 8 bis 10 sind die erfindungsgemäßen Vorrichtungsmerkmale wiedergegebenTo achieve this object, the method features listed in the characterizing part of the first claim are proposed.
Erfindungsgemäß wird die Energie des Kokses in der ersten Stufe teilweise erheblich weniger genutzt und somit auch weniger hochgespannter Dampf erzeugt als bei anderen bekannten Verfahren. Das ist insbesondere bei Kokereianlagen sinnvoll, bei denen die Möglichkeit fehlt, größere Mengen hochgespannten Dampfes an fremde Verbraucher abzugeben. Dadurch kann die eigentliche Kokstrockenkühlkammer kleiner und insbesondere mit einer sehr viel geringeren Bauhöhe vorgesehen werden. Die Kokstemperatur wird allerdings in der ersten Stufe vor der Wassertauchung so weit gesenkt, daß die bei höheren Temperaturen beschleunigt ablaufenden Vergasungsreaktionen beim erfindungsgemäßen Verfahren weitestgehend unterdrückt werden.According to the invention, the energy of the coke is sometimes used considerably less in the first stage and therefore less steam is generated than in other known processes. This is particularly useful for coke oven plants, at who lack the ability to deliver large quantities of high-tension steam to external consumers. As a result, the actual coke dry cooling chamber can be provided smaller and in particular with a much lower overall height. However, the coke temperature is lowered so far in the first stage before the water immersion that the gasification reactions proceeding accelerated at higher temperatures are largely suppressed in the process according to the invention.
Der heiße Koks kann in der ersten Stufe zweckmäßig ausschließlich indirekt auf ca. 600 oC gekühlt werden und dabei entweder die Wärme an im Schacht eingebaute Kühlflächen oder auf einem kontinuierlich umlaufenden Heißkoksförderband an oberhalb und unterhalb des Förderbandes angeordnete Strahlungskühlflächen abgeben. Bei einer direkten Kühlung mit Kühlgas mit Gegenstrom kann zweckmäßig abhängig von der Menge und Temperatur des Kühlgases der Koks unter Umständen bis auf ca. 400 oC gekühlt werden. Bei der Gleichstromkühlung kann der Koks durch Einleiten von ca. 120 oC heißen Wasserdampf rasch unter 800 oC, vorzugsweise auf ca. 600 - 650 oC, abgekühlt werden, so daß keine Vergasung des Kokses erfolgt. Der mit ca. 500 bis 600 oC abgezogene Dampf kann entweder zur Kohlevorerhitzung oder auch zur Erzeugung von Hochdruckdampf in einem Abhitzekessel genutzt werden.In the first stage, the hot coke can expediently only be indirectly cooled to approx. 600 o C and either give off the heat to cooling surfaces installed in the shaft or on a continuously rotating hot coke conveyor belt to radiation cooling surfaces arranged above and below the conveyor belt. In a direct cooling with cooling gas counter-current of coke can be appropriately selected depending are cooled to about 400 o C by the quantity and temperature of the cooling gas under certain circumstances. In the case of direct current cooling, the coke can be rapidly cooled below 800 o C, preferably to about 600-650 o C, by introducing hot steam at about 120 ° C., so that there is no gasification of the coke. The steam drawn off at approx. 500 to 600 o C can either be used for preheating coal or for generating high-pressure steam in a waste heat boiler.
Nach dem Vorschlag der Erfindung kann der Koks in der ersten Stufe bis auf die eingangs genannte Temperatur von 200 bis 800 oC, vorzugsweise 400 - 650 oC, kontinuierlich gekühlt und anschließend in einem geschlossenen System in den nachfolgenden Tauchbehälter gegeben werden. Dabei wird der Koks in kurzer Zeit durch ein Wasserbad gefördert, wobei es aufgrund der kurzen Verweilzeit des Kokses im Wasserbad in der Regel zu keinem vollständigen Wärmeaustausch innerhalb der Koksstücke zwischen Kornoberfläche und Korninneren kommt. Deshalb wird der Koks anschließend in einer dritten Stufe in einem geschlossenen Nachverdampfungsbehälter gehalten. Hier kommt es innerhalb der Koksschüttung zu einem intensiven Wärmeaustausch zwischen Korninneren und Kornoberfläche, wobei ein Großteil des an der Oberfläche anhaftenden Wassers verdampft und abgezogen wird. Der intensive Wärmeaustausch wird durch den frei werdenden Wasserdampf begünstigt, der dann durch die Koksschüttung strömt und auch im Kreislauf geführt werden kann. Am Ende verläßt der Koks den Nachverdampfungsbehälter mit einer gleichmäßigen Temperatur und einem gleichmäßigen Wassergehalt, der sich bei der weiteren Verladung nicht mehr wesentlich ändert. Insbesondere können sich bei der Weiterbehandlung des Kokses keine Staubpartikel mehr losen, so daß Staubemissionen vermieden werden. Tauchzeiten von weniger als 3 Minuten, vorzugsweise 10 bis 60 Sekunden reichen dabei aus, um den am Koksstück anhaftenden Koksstaub nahezu vollständig abzulösen und mit dem Spülwasser zur Kläranlage abzuführen. Der anhaftende Koksstaub wird nicht mehr in den nachfolgenden Verdampfungsbehälter getragen.According to the proposal of the invention, the coke can be continuously cooled in the first stage to the temperature of 200 to 800 ° C., preferably 400-650 ° C., mentioned above , and then added to the subsequent immersion container in a closed system. The coke is conveyed through a water bath in a short time, whereby due to the short dwell time of the coke in the water bath there is generally no complete heat exchange within the coke pieces between the grain surface and the grain interior. Therefore, the coke is then kept in a third stage in a closed post-evaporation tank. Here there is an intensive heat exchange within the coke bed between the interior of the grain and the grain surface, whereby a large part of the water adhering to the surface is evaporated and drawn off. The intensive heat exchange is promoted by the released water vapor, which then flows through the coke bed and can also be circulated. In the end, the coke leaves the post-evaporation tank with a uniform temperature and water content which does not change significantly during further loading. In particular, dust particles can no longer loosen during the further treatment of the coke, so that dust emissions are avoided. Dipping times of less than 3 minutes, preferably 10 to 60 seconds, are sufficient to almost completely detach the coke dust adhering to the coke piece and to discharge it to the sewage treatment plant with the rinse water. The adhering coke dust is no longer carried into the subsequent evaporation container.
Bei Einhaltung der im Anspruch 4 angegebenen Parameter besitzt der Koks nach Verlassen des Nachverdampfungsbehälters einen relativ geringen Wassergehalt, der für die spätere Verwendung im Hochofen günstig ist. Die Temperatur des Kokses nach Verlassen des Nachverdampfungsbehälters ist mit vorzugsweise 70 - 80 oC erheblich unter der Verdampfungstemperatur, so daß auch eine unerwünschte Dampfentwicklung beim weiteren Transport des Kokses auf offenen Fördereinrichtungen ausgeschaltet werden kann.If the parameters specified in claim 4 are observed, the coke has a relatively low water content after leaving the post-evaporation tank, which is favorable for later use in the blast furnace. The temperature of the coke after leaving the Nachverdampfungsbehälters is preferably to 70 - 80 o C, so that an undesirable steam development during the further transport of the coke can be turned to open conveyors substantially below the evaporation temperature.
Weiterhin hat sich gezeigt, daß bei der direkten Tauchung die Wasserdampfbildung relativ gering ist. Der Wasserdampf kann aus dem geschlossenen Behälter abgezogen und in einfacher Weise auf der Rohgasreinigungsseite der Kokerei vorzugsweise durch Einleitung in die Rohgasvorlage weiterverarbeitet werden. Schon in dem Tauchbehälter wird durch ständige Berieselung über der gesamten Fläche des Wasserbeckens ein großer Teil des Wasserdampfes wieder kondensiert. Dasselbe geschieht auch bei Einleitung des Dampfes in die Vorlage mit Hilfe der dort vorhandenen Wasserberieselung. Durch das ständige Einleiten von kaltem Frischwasser und gekühltem Umlaufwasser aus der Kläranlage wird die Wassertemperatur des Tauchbeckens bei ca. 60 bis 80 oC gehalten, so daß möglichst viel der im Koks enthaltenen Wärme über die Erwärmung des Wassers abgeführt wird und somit nur wenig Wasserdampf entsteht.Furthermore, it has been shown that the water vapor formation is relatively low in direct immersion. The water vapor can be drawn off from the closed container and processed in a simple manner on the raw gas cleaning side of the coking plant, preferably by introducing it into the raw gas receiver. Even in the immersion tank, a large part of the water vapor is condensed again by constant sprinkling over the entire surface of the water basin. The same happens when the steam is introduced into the receiver with the help of the water sprinkling there. Through the constant introduction cold fresh water and cooled circulating water from the sewage treatment plant keep the water temperature in the plunge pool at approx. 60 to 80 o C, so that as much of the heat contained in the coke as possible is dissipated via the heating of the water and thus little water vapor is generated.
Zur Durchführung des erfindungsgemäßen Verfahrens wird eine Vorrichtung nach Anspruch 8 vorgeschlagen, wobei der Koksaustrag des Kokstrockenkühlschachtes bzw. des Heißkoksförderbandes und der Tauchbehälter sowie der nachgeschaltete Nachverdampfungsbehälter jeweils gasdicht miteinander verbunden sind, so daß bei der Übergabe des Kokses von einem Behälter zum anderen keine Emissionen entstehen können. Um zu verhindern, daß Wasserdampf aus den Tauchbehälter zurück in die Kokstrockenkühlung strömt, kann das untere Ende des Einfüllstutzens in das Wasser des Tauchbehälters eingetaucht und in dem gesamten Einfüllstutzen und dem Auslauftrichter eine dichte Koksschüttung gehalten werden. Zusätzlich kann mit Hilfe einer Absperrklappe bei fehlender Koksschüttung ein Rückströmen von Wasserdampf verhindert werden. Die Koksaustragsvorrichtung aus der Kokstrockenkühlung kann aber erfindungsgemäß auch ohne die üblichen Schleusenbunker bzw. gasdichten Austragsschleusen ausgeführt sein. Gegebenenfalls kann der Austrag auf nicht gasdichte Förderorgane, wie z. B. Austragswippen, beschränkt werden.To carry out the method according to the invention, a device according to claim 8 is proposed, wherein the coke discharge from the coke drying chute or the hot coke conveyor belt and the immersion tank and the downstream post-evaporation tank are each connected to one another in a gastight manner, so that no emissions occur when the coke is transferred from one tank to another can. In order to prevent water vapor from flowing out of the immersion container back into the dry coke cooling, the lower end of the filler neck can be immersed in the water of the immersion container and a dense coke bed can be kept in the entire filler neck and the outlet funnel. In addition, a backflow of water vapor can be prevented with the help of a butterfly valve in the absence of coke. According to the invention, the coke discharge device from the coke dry cooling can also be designed without the usual lock bunkers or gas-tight discharge locks. Optionally, the discharge on non-gas-tight conveying bodies, such as. B. discharge rockers are limited.
Die Erfindung wird anhand der beigefügten schematischen Figur beispielsweise näher erläutert.The invention is explained in more detail, for example, using the attached schematic figure.
Die Vorkammer (19) in der Figur wird in an sich bekannter Weise mit ein oder mehreren Kokstransportkübelfüllungen gefüllt und der Koks rutscht kontinuierlich über die Koksaufgabe (2) in den Kokstrockenkühlschacht (1). Dort gibt er Wärme entweder indirekt an die Kühlwände (6) und/oder direkt an die Kühlgase ab, die über die Anschlüsse (3/5) im Gegenstrom (durchgezogene Pfeile) oder in Gleichstrom (gestrichelte Pfeile) zu- bzw. abgeführt werden. Im letzteren Fall wird über den Anschluß (3) ca. 120 oC heißer Wasserdampf zur Gleichstromkühlung des Kokses aufgegeben, der am unteren Ende der Kühlkammer unterhalb der Austragswippen (20) über die Kühlgasabsaugung (5) mit einer Temperatur von 500 bis 600 oC abgezogen wird. Nach Verlassen der Trockenkühlzone besitzt der Koks je nach Kühlverfahren in dem Koksaustrag (4) eine Temperatur von ca. 200 bis 800 oC und rutscht über den Auslauftrichter (9) sowie den Einfüllstutzen (7) kontinuierlich in das Wasserbad des Tauchbehälters (8). In dem Einfüllstutzen (7) und teilweise auch in dem Auslauftrichter (9) staut sich die Koksschüttung auf und verhindert weitgehend eine Rückströmung des im Tauchbehälter (8) bei der Kokskühlung entstehenden Wasserdampfes. Wenn der Durchlauf des heißen Kokses durch den Kokstrockenkühlschacht mit Hilfe der gekühlten Austragswippen (20) geregelt wird, wird bei einem eventuellen Leerlauf des Einfüllstutzens (7) die in dessen oberen Bereich befindliche Absperrklappe (17) z. B. mit Hilfe eines Gegengewichtes automatisch geschlossen. Die Verweilzeit des Kokses in dem Wassertauchbad wird durch die Geschwindigkeit des Koksförderers (13) bestimmt, der um die Umlenkrollen (11) im Kreislauf geführt ist und zweckmäßigerweise aus einem Plattenförderer mit siebförmigen Platten besteht. Unterhalb des Koksförderers (13) befindet sich ein Kratzförderer (18), mit dessen Hilfe die von den Koks abgetrennten Kokspartikel zum Wasserablauf (16) transportiert werden. Mit dem Koksförderer (13) wird der Koks unmittelbar in den sich gasdicht an den Tauchbehälter (8) anschließenden Nachverdampfungsbehälter (14) gebracht, aus dem der Koks nach einer bestimmten Zeit in an sich bekannter Weise z. B. über Schleusen oder Zellenräder am Koksaustrag (15) abgezogen wird. Zumindest über der Einlaßstelle des Kokses in das Wasserbad, vorzugsweise aber auch über der gesamten Wasserfläche, befinden sich Bedüsungs- und Berieselungseinrichtungen (12), über die sowohl kaltes Frischwasser als auch im Kreislauf geführtes gekühltes Klärwasser aufgegeben wird. Der bei der Kokskühlung entstehende Wasserdampf wird zu einen großen Teil durch das aufgebrachte Wasser wieder kondensiert. Der nicht kondensierte Wasserdampf wird an verschiedenen Stellen, insbesondere über dem Nachverdampfungsbehälter (14), über die Dampfabsaugungen (10) zur weiteren Verarbeitung abgezogen. Zur Vermeidung von Korrosion hat es sich als günstig erwiesen, dem Wassertauchbad Kalk oder ähnliche Stoffe zuzugeben.The antechamber (19) in the figure is filled with one or more coke transport bucket fillings in a manner known per se and the coke slides continuously over the coke feed (2) into the coke drying cooling shaft (1). There it gives off heat either indirectly to the cooling walls (6) and / or directly to the cooling gases, which are supplied or discharged via the connections (3/5) in countercurrent (solid arrows) or in direct current (dashed arrows). In the latter case, the Connection (3) about 120 o C hot water vapor for direct current cooling of the coke, which is drawn off at the lower end of the cooling chamber below the discharge rockers (20) via the cooling gas suction (5) at a temperature of 500 to 600 o C. After leaving the dry cooling zone, the coke has a temperature of approx. 200 to 800 o C in the coke discharge (4) depending on the cooling method and slips continuously into the water bath of the immersion tank (8) via the discharge funnel (9) and the filler neck (7). The coke bed builds up in the filler neck (7) and partly also in the outlet funnel (9) and largely prevents backflow of the water vapor generated in the immersion container (8) during coke cooling. If the flow of hot coke through the coke drying chute is regulated with the help of the cooled discharge rockers (20), the shut-off flap (17) located in the upper area of the filler neck (17) is used when the filler neck (7) is possibly idling. B. automatically closed with the help of a counterweight. The residence time of the coke in the water immersion bath is determined by the speed of the coke conveyor (13), which is circulated around the deflection rollers (11) and expediently consists of a plate conveyor with sieve-shaped plates. Below the coke conveyor (13) there is a scraper conveyor (18), with the help of which the coke particles separated from the coke are transported to the water outlet (16). With the coke conveyor (13) the coke is brought directly into the gas-tight adjoining the immersion tank (8) subsequent evaporation tank (14), from which the coke after a certain time in a manner known per se, for. B. is withdrawn via locks or cellular wheels on the coke discharge (15). At least above the inlet point of the coke into the water bath, but preferably also over the entire water surface, there are spraying and sprinkling devices (12) via which both cold fresh water and cooled clarified water which is circulated are introduced. The water vapor generated during coke cooling is largely condensed again by the water applied. The uncondensed water vapor is released at various points, in particular the post-evaporation tank (14), via the steam exhaust (10) for further processing. To avoid corrosion, it has proven beneficial to add lime or similar substances to the water immersion bath.
- (1)(1)
- KokstrockenkühlschachtCoke dry cooling shaft
- (2)(2)
- KoksaufgabeCoke duty
- (3)(3)
- Anschluß für KühlgasConnection for cooling gas
- (4)(4)
- KoksaustragCoke discharge
- (5)(5)
- Anschluß für KühlgasConnection for cooling gas
- (6)(6)
- KühlflächenCooling surfaces
- (7)(7)
- EinfüllstutzenFiller neck
- (8)(8th)
- TauchbehälterImmersion tank
- (9)(9)
- AuslauftrichterDischarge funnel
- (10)(10)
- DampfabsaugungSteam extraction
- (11)(11)
- UmlenkrollenPulleys
- (12)(12)
- BedüsungseinrichtungSpraying device
- (13)(13)
- KoksfördererCoke conveyor
- (14)(14)
- NachverdampfungsbehälterPost-evaporation tank
- (15)(15)
- KoksaustragCoke discharge
- (16)(16)
- Wasser- und KokspartikelaustragWater and coke particle discharge
- (17)(17)
- AbsperrklappeButterfly valve
- (18)(18)
- KratzfördererScraper conveyor
- (19)(19)
- VorkammerAntechamber
- (20)(20)
- AustragswippenDischarge rockers
Claims (10)
- A process for the cooling of and the removal of dust from high-temperature coke in at least two stages, whereby the coke in the first stage is cooled down to less than 800 °C and then passed continuously through a water bath within a short time, characterized in that the coke in the first cooling stage is cooled down to a level of 200 to 800 °C, preferably to a level of 400 to 650 °C, then passed continuously through a water bath within a short time and subsequently kept in a closed post-evaporation container in a water steam atmosphere.
- A process according to Claim #1, characterized in that the coke in the first stage is cooled to a level of approx. 600 °C exclusively by application of indirect cooling surfaces, preferably built-in in the cooling shaft, or cooled to said level on a continuously circulating hot coke conveyor belt by way of radiation cooling surfaces located above and below said conveyor belt.
- A process according to Claim #1, characterized in that the coke in the first stage is cooled directly by way of a gaseous cooling medium down to a level of approx. 400 °C preferably in equal flow by way of water steam down to a level of approx. 600 to 650 °C.
- A process according to any of the Claims #1 to #3, characterized in that the residence time of coke in the post-evaporation container accounts for less than 30 minutes, preferably for 3 to 10 minutes, and that the coke is discharged from the post-evaporation container at a temperature of 40 to 80 °C, preferably at a temperature of 70 to 80 °C.
- A process according to any of the Claims #1 to #4, characterized in that the water steam withdrawn from the enclosed container on water immersion of coke is further processed on the crude gas purification side of the coke plant, preferably by way of being introduced into the crude gas collecting main and that appropriate volumes of cold fresh water are constantly fed to the immersion pond.
- A process according to Claim #5, characterized in that a part of the steam withdrawn from the immersion-type container and/or post-evaporation container is passed in counterflow through the coke in the post-evaporation container.
- A process according to any of the Claims #1 to #6, characterized in that a certain portion of the condensate burdened with coke particles and/or a certain portion of the effluent water are withdrawn continuously from the immersion-type pond and/or post-evaporation container, and that said portions then are largely liberated from dust in the settling plant and fed back to the immersion pond.
- A device for execution of the process being the subject of this invention, comprised of a coke dry cooling unit with facilities for upper coke feed (2) and lower coke discharge (4), with the coke being filled-in through a filling nozzle submerged in the water of the immersion pond, characterized in that the coke discharge is mounted in a gastight connection through the filling nozzle (9) submerged in the water of the immersion-type container (8) with the enclosed casing of the immersion-type container (8) and that the latter container is also mounted in a gastight connection with the downstream located post-evaporation container (14).
- A device according to Claim #8, characterized in that a shutoff flap (17) is mounted at the lower end of the discharge hopper (9) or in the upper area of the filling nozzle (7), with said shutoff flap closing automatically in the event of a lack of coke charge in the area of the shutoff flap (17).
- A device according to Claim #9, characterized in that the lower part of the coke conveyor (13) circulating in the immersion-type container (8) is also arranged with the backflow in the water bath and that a sieve-like tray is arranged between the pre-and backflow of the coke conveyor (13), with separated coke particles sliding through said sieve-like tray enabling them to sink down on the bottom of the immersion-type container (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT87907757T ATE88209T1 (en) | 1986-11-08 | 1987-11-09 | METHOD AND DEVICE FOR COOLING AND DUST REMOVAL OF HIGH TEMPERATURE COKE. |
Applications Claiming Priority (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3638165 | 1986-11-08 | ||
| DE3638166 | 1986-11-08 | ||
| DE3638166 | 1986-11-08 | ||
| DE19863638165 DE3638165A1 (en) | 1986-11-08 | 1986-11-08 | Process for cooling and dedusting coke after it has left dry coke cooling |
| DE3715355 | 1987-05-08 | ||
| DE19873715355 DE3715355A1 (en) | 1986-11-08 | 1987-05-08 | A process and device for cooling and dedusting high-temperature coke |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0329705A1 EP0329705A1 (en) | 1989-08-30 |
| EP0329705B1 true EP0329705B1 (en) | 1993-04-14 |
Family
ID=27195080
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP87907757A Expired - Lifetime EP0329705B1 (en) | 1986-11-08 | 1987-11-09 | Process and device for the cooling of and the removal of dust from high-temperature coke |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0329705B1 (en) |
| JP (1) | JP2532636B2 (en) |
| KR (1) | KR950006548B1 (en) |
| AT (1) | ATE88209T1 (en) |
| AU (1) | AU8277087A (en) |
| BR (1) | BR8707867A (en) |
| DE (1) | DE3785456D1 (en) |
| IN (1) | IN170882B (en) |
| WO (1) | WO1988003549A1 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100960379B1 (en) * | 2008-07-18 | 2010-05-28 | 주식회사 포스코 | Device for treating dust in coke dust colliecting plant |
| ITMI20130826A1 (en) | 2013-05-21 | 2014-11-22 | Ambiente E Nutrizione Srl | PROCEDURE FOR THE SHUTDOWN OF COKE |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE377006C (en) * | 1923-06-09 | Georgs Marien Bergwerks Und Hu | Coke extinguishing and loading wagons with an endless conveyor belt | |
| US3959084A (en) * | 1974-09-25 | 1976-05-25 | Dravo Corporation | Process for cooling of coke |
| US4100034A (en) * | 1976-07-19 | 1978-07-11 | Peabody Coal Company | Quenching method |
| DE3523897C1 (en) * | 1985-02-21 | 1986-08-14 | Carl Still Gmbh & Co Kg, 4350 Recklinghausen | Process for cooling and dedusting coke after leaving the coke dry cooling |
-
1987
- 1987-11-09 DE DE8787907757T patent/DE3785456D1/en not_active Expired - Fee Related
- 1987-11-09 EP EP87907757A patent/EP0329705B1/en not_active Expired - Lifetime
- 1987-11-09 WO PCT/EP1987/000693 patent/WO1988003549A1/en active IP Right Grant
- 1987-11-09 AU AU82770/87A patent/AU8277087A/en not_active Abandoned
- 1987-11-09 JP JP63500038A patent/JP2532636B2/en not_active Expired - Lifetime
- 1987-11-09 AT AT87907757T patent/ATE88209T1/en not_active IP Right Cessation
- 1987-11-09 BR BR8707867A patent/BR8707867A/en not_active IP Right Cessation
- 1987-11-09 KR KR1019880700801A patent/KR950006548B1/en not_active IP Right Cessation
-
1988
- 1988-04-22 IN IN325/CAL/88A patent/IN170882B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| BR8707867A (en) | 1989-10-03 |
| IN170882B (en) | 1992-06-06 |
| ATE88209T1 (en) | 1993-04-15 |
| JPH02500752A (en) | 1990-03-15 |
| DE3785456D1 (en) | 1993-05-19 |
| AU8277087A (en) | 1988-06-01 |
| KR950006548B1 (en) | 1995-06-16 |
| KR890700155A (en) | 1989-03-10 |
| EP0329705A1 (en) | 1989-08-30 |
| JP2532636B2 (en) | 1996-09-11 |
| WO1988003549A1 (en) | 1988-05-19 |
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