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)

Priority Applications (5)

Applications Claiming Priority (6)

Publications (1)

Family

ID=27195080

Family Applications (1)

Country Status (9)

Cited By (1)

Families Citing this family (1)

Citations (4)

• 1987
  • 1987-11-09 JP JP63500038A patent/JP2532636B2/ja not_active Expired - Lifetime
  • 1987-11-09 DE DE8787907757T patent/DE3785456D1/de not_active Expired - Fee Related
  • 1987-11-09 EP EP87907757A patent/EP0329705B1/de not_active Expired - Lifetime
  • 1987-11-09 AU AU82770/87A patent/AU8277087A/en not_active Abandoned
  • 1987-11-09 BR BR8707867A patent/BR8707867A/pt not_active IP Right Cessation
  • 1987-11-09 AT AT87907757T patent/ATE88209T1/de not_active IP Right Cessation
  • 1987-11-09 WO PCT/EP1987/000693 patent/WO1988003549A1/de active IP Right Grant
  • 1987-11-09 KR KR1019880700801A patent/KR950006548B1/ko not_active Expired - Fee Related
• 1988
  • 1988-04-22 IN IN325/CAL/88A patent/IN170882B/en unknown

Patent Citations (4)

Also Published As

Similar Documents

Legal Events