EP0329705A1 - Procede et dispositif pour refroidir et depoussierer du coke a haute temperature. - Google Patents

Procede et dispositif pour refroidir et depoussierer du coke a haute temperature.

Info

Publication number
EP0329705A1
EP0329705A1 EP87907757A EP87907757A EP0329705A1 EP 0329705 A1 EP0329705 A1 EP 0329705A1 EP 87907757 A EP87907757 A EP 87907757A EP 87907757 A EP87907757 A EP 87907757A EP 0329705 A1 EP0329705 A1 EP 0329705A1
Authority
EP
European Patent Office
Prior art keywords
coke
cooling
water
post
immersion
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.)
Granted
Application number
EP87907757A
Other languages
German (de)
English (en)
Other versions
EP0329705B1 (fr
Inventor
Kurt Lorenz
Dieter Stalherm
Horst Dungs
Werner Schumacher
Willi Brinkmann
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.)
Thyssen Still Otto Anlagentechnik GmbH
Original Assignee
Still Otto GmbH
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
Priority claimed from DE19863638165 external-priority patent/DE3638165A1/de
Priority claimed from DE19873715355 external-priority patent/DE3715355A1/de
Application filed by Still Otto GmbH filed Critical Still Otto GmbH
Priority to AT87907757T priority Critical patent/ATE88209T1/de
Publication of EP0329705A1 publication Critical patent/EP0329705A1/fr
Application granted granted Critical
Publication of EP0329705B1 publication Critical patent/EP0329705B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • 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 for cooling and dedusting high-temperature coke in at least two stages, the coke being cooled to below about 800 ° C. in the first stage, and to devices for carrying out the method having the features in the preamble of claim 8.
  • DE-OS 25 33 606 describes a two-stage process for cooling coke, the coke first being cooled in countercurrent with the aid of an inert gas in a first closed container from 1,100 ° C. to about 315 to 425 ° C. and then in a closed container sprayed with water and the evaporation of the water to reduce the temperature of the coke to 95 to 150 ° C. Similar to the usual wet quenching under the coke quench tower, 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 in addition the method for coke dry cooling is simplified in view of a cheaper design.
  • the energy of the coke in the first stage is sometimes used considerably less and thus 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, however, 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 oC and either give off the heat to the 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.
  • the coke can expediently be cooled down to approximately 400 ° C.
  • direct current cooling the coke can be rapidly cooled below 800 ° C, preferably to about 600-650 ° C, by introducing hot steam at about 120 ° C so that there is no gasification of the coke.
  • the steam extracted at approx. 500 to 600 oC 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 above-mentioned temperature of 200 to 800 ° C, preferably 400-650 ° C, 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.
  • 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 dissolve 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 post-evaporation tank is preferably below 70-80 ° C., significantly below the evaporation temperature, so that undesired steam generation can also be eliminated when the coke is transported further on open conveyors.
  • 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.
  • the water temperature of the plunge pool is kept at approx. 60 to 80 oC, 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, the coke discharge from the coke drying chute or the hot coke conveyor belt and the immersion tank and the downstream post-evaporation tank being connected gas-tight to one another, 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 dip tank and a dense coke fill 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 conveyor cranes, 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 counterflow (solid arrows) or in cocurrent (dashed arrows). In the latter case, the Connection (3) about 120 ° 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 ° 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. 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).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Procédé pour refroidir et dépoussiérer du coke à haute température en au moins deux étapes, le coke étant refroidi à une température au-dessus de 800°C environ pendant la première étape. Au cours de cette première étape de refroidissement (1), le coke doit être refroidi à une température comprise entre 200 et 800°C, de préférence entre 400 et 650°C environ, puis décrassé en continu par barbotage dans l'eau (8) et ensuite maintenu dans un réservoir fermé d'évaporation ultérieure (14) dans une atmosphère de vapeur d'eau.
EP87907757A 1986-11-08 1987-11-09 Procede et dispositif pour refroidir et depoussierer du coke a haute temperature Expired - Lifetime EP0329705B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87907757T ATE88209T1 (de) 1986-11-08 1987-11-09 Verfahren und vorrichtung zur kuehlung und entstaubung von hochtemperaturkoks.

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
DE3638166 1986-11-08
DE3638166 1986-11-08
DE19863638165 DE3638165A1 (de) 1986-11-08 1986-11-08 Verfahren zur kuehlung und entstaubung von koks nach verlassen einer kokstrockenkuehlung
DE3638165 1986-11-08
DE19873715355 DE3715355A1 (de) 1986-11-08 1987-05-08 Verfahren und vorrichtung zur kuehlung und entstaubung von hochtemperaturkoks
DE3715355 1987-05-08

Publications (2)

Publication Number Publication Date
EP0329705A1 true EP0329705A1 (fr) 1989-08-30
EP0329705B1 EP0329705B1 (fr) 1993-04-14

Family

ID=27195080

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87907757A Expired - Lifetime EP0329705B1 (fr) 1986-11-08 1987-11-09 Procede et dispositif pour refroidir et depoussierer du coke a haute temperature

Country Status (9)

Country Link
EP (1) EP0329705B1 (fr)
JP (1) JP2532636B2 (fr)
KR (1) KR950006548B1 (fr)
AT (1) ATE88209T1 (fr)
AU (1) AU8277087A (fr)
BR (1) BR8707867A (fr)
DE (1) DE3785456D1 (fr)
IN (1) IN170882B (fr)
WO (1) WO1988003549A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100960379B1 (ko) * 2008-07-18 2010-05-28 주식회사 포스코 코크스 분진 집진설비의 분진 처리장치
ITMI20130826A1 (it) * 2013-05-21 2014-11-22 Ambiente E Nutrizione Srl Procedimento per lo spegnimento di coke

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE377006C (de) * 1923-06-09 Georgs Marien Bergwerks Und Hu Koksloesch- und Verladewagen mit endlosem Foerderband
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 (de) * 1985-02-21 1986-08-14 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Verfahren zur Kuehlung und Entstaubung von Koks nach Verlassen der Kokstrockenkuehlung

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO8803549A1 *

Also Published As

Publication number Publication date
EP0329705B1 (fr) 1993-04-14
WO1988003549A1 (fr) 1988-05-19
DE3785456D1 (de) 1993-05-19
KR890700155A (ko) 1989-03-10
IN170882B (fr) 1992-06-06
AU8277087A (en) 1988-06-01
KR950006548B1 (ko) 1995-06-16
ATE88209T1 (de) 1993-04-15
BR8707867A (pt) 1989-10-03
JP2532636B2 (ja) 1996-09-11
JPH02500752A (ja) 1990-03-15

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