EP0064617A2 - Procédé et dispositif pour l'exploitation d'une installation de fours à coke - Google Patents

Procédé et dispositif pour l'exploitation d'une installation de fours à coke Download PDF

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Publication number
EP0064617A2
EP0064617A2 EP82103250A EP82103250A EP0064617A2 EP 0064617 A2 EP0064617 A2 EP 0064617A2 EP 82103250 A EP82103250 A EP 82103250A EP 82103250 A EP82103250 A EP 82103250A EP 0064617 A2 EP0064617 A2 EP 0064617A2
Authority
EP
European Patent Office
Prior art keywords
cascade
fluidized bed
coal
gas
bed dryer
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
EP82103250A
Other languages
German (de)
English (en)
Other versions
EP0064617A3 (en
EP0064617B1 (fr
Inventor
Vladan Dr. Dipl.-Ing. Petrovic
Karl Dr. Dipl.-Chem. Schmid
Friedrich Dr. Dipl.-Ing. Jokisch
Heinz Rotthaus
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.)
Krupp Koppers GmbH
Original Assignee
Krupp Koppers 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
Application filed by Krupp Koppers GmbH filed Critical Krupp Koppers GmbH
Priority to AT82103250T priority Critical patent/ATE15062T1/de
Publication of EP0064617A2 publication Critical patent/EP0064617A2/fr
Publication of EP0064617A3 publication Critical patent/EP0064617A3/de
Application granted granted Critical
Publication of EP0064617B1 publication Critical patent/EP0064617B1/fr
Expired legal-status Critical Current

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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
    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S165/00—Heat exchange
    • Y10S165/92—Particulate heat exchange

Definitions

  • the invention relates to a method for operating a coke oven plant, in which the coke ovens are periodically charged with preheated or predried coal and the coke produced is subjected to dry cooling by means of a gaseous cooling medium, the plant for coke drying cooling and for coal preheating being connected to one another by a common gas circuit through which the heat extracted from the hot coke during cooling is transferred to the preheated coal. Furthermore, the invention relates to a special cascade fluidized bed dryer which can advantageously be used for preheating coal when the method according to the invention is used.
  • the invention is therefore based on the object of improving the method of the type described at the outset in such a way that on the one hand the disadvantages described above are avoided and on the other hand, of course, the operating conditions in general are improved both in the case of coal preheating and coke oven cooling.
  • this consists of three cascades arranged one above the other, which are separated from one another by the gas-permeable inflow trays 4.
  • the number of cascades depends on the moisture content and the desired degree of drying or preheating of the coal used.
  • the coal used has a water content of 9%.
  • the coal is heated to approx. 80 ° C and dried to a water content of approx. 1.5%.
  • the partially dried coal is then transferred via line 5, which is provided with a rotary valve 6, into the second cascade below.
  • the coal reaches a temperature of approx. 150 ° C and a water content of approx. 0.5%.
  • the coal then passes via line 7, which in turn is provided with a cellular wheel sluice 8, into the third [bottom] casa practical, in which it is dried / to a residual water content of ⁇ 0% and to a temperature of approx. 200 ° C. is heated.
  • the dried coal is drawn off from the cascade fluidized bed dryer 3 and transported via a screw conveyor 9 and a chain conveyor 10 to the coal tower of the coking plant, not shown in the flow diagram. Both the screw conveyor 9 and the chain conveyor 10 can be electrically heated in order to prevent heat losses.
  • the entire conveyor system is rendered inert in order to avoid the penetration of water vapor from the cascade fluidized bed dryer 3.
  • This water vapor is responsible for maintaining the coal-water vapor fluidized bed in the cascade fluidized bed dryer 3 and is at a pressure of about 2 bar and a temperature of about 200 ° C via the line 11 and the inflow floor 4 from below into the third (bottom ) Cascade initiated.
  • the water vapor then flows through the individual cascades from bottom to top and emerges from the first (top) cascade at a temperature of approx. 140 ° C. He then passes through line 12 to the dust collector (cyclone) 13, in which the mitge cracked coal dust is separated.
  • This separated coal dust is fed via line 14, which is provided with cellular wheel locks 15 and 16, to the screw conveyor 9 and mixed there with the dried and preheated coal.
  • the dedusted water vapor is withdrawn from the dust separator 13 via the line 17. Since the steam flow has additionally absorbed water vapor separated from the moist coal when it passes through the individual cascades of the cascade fluidized bed dryer 3, this excess water vapor must be removed from the circuit by partial condensation. For this purpose, a partial flow of the water vapor is branched off from the line 17 via the line 18, which is provided with the control / 19, and is condensed in the circuit washer 20. The majority of the water vapor, however, gets into the blower 21, in which the required recompression takes place to approx. 2 bar, the water vapor also being heated up again to approx nothing stands in the way. The water vapor cycle is now closed. If necessary, inert gas can be fed into the water vapor circuit via line 32.
  • the partial stream of water vapor drawn off through line 18 is introduced into the circuit washer 20, in which, in addition to condensation, impurities are also washed out.
  • the liquid running out of the circuit washer 20 is fed via the line 22 and the pump 23 to the cooling tower 24, in which it cools down to 40 ° C.
  • the GE Cooled liquid is then introduced into the cooling water distributor 26 via the line 25. From here, the required circuit water is fed back to the circuit washer 20 at different heights via lines 27, 28 and 29. Excess water, however, is withdrawn via line 30 and introduced into the sewer 31.
  • a wastewater treatment device not shown in the flow diagram, can also be provided in the line 22 leading from the circuit washer 20 to the cooling tower 24.
  • the solids separated from the wastewater which have a high proportion of fine coal, can either be deposited in a landfill or incinerated.
  • the hot gas stream emerging from the upper part of the coke dry cooler 33 at a temperature of approximately 800 ° C. is withdrawn via line 34, from which branches off the gas inlet line 35, through which the partial stream of the gas is withdrawn, which is used for indirect heat transfer in the cascade fluidized bed dryer 3 becomes.
  • This partial stream which contains about 50% by volume of the total gas quantity, reaches the heating tubes 36 of the first (top) cascade of the cascade fluidized bed dryer 3 at a temperature of about 600 ° C. After passing through the heating tubes 36, the gas stream still has a temperature from approx. 400 ° C.
  • the gas stream is now further divided, one partial stream entering the heating tubes 37 of the second (middle) cascade and the other partial stream entering the heating tubes 38 of the third (lowest) cascade.
  • the gas stream emerging from this cascade at a temperature of approximately 288 ° C. is withdrawn through the gas outlet line 39.
  • the line 40 opens into this, through which the gas stream emerging from the heating pipes 37 at a temperature of approximately 266 ° C. mixes with the gas stream in the gas outlet line 39 becomes.
  • the line 42 branches off from the gas outlet line 39, through which, with the corresponding position of the control flaps 44 and 45, a partial flow of the gas can be discharged into the atmosphere via the chimney 43.
  • a bypass line 46 is provided behind the blower 41, through which the gas outlet line 39 is connected to the gas inlet line 35.
  • This bypass line 46 allows cold gas from the gas outlet line 39 to be mixed into the hot gas in the gas inlet line 35 for the purpose of temperature control.
  • the temperature measuring point 47 is provided in the gas inlet line 35, the value determined there being transmitted via the interrupted pulse line 48 to the control device 49, which in turn actuates the motor-driven control flap 50 in the gas outlet line 39 as a function of a predetermined target value. If the gas temperature determined at the temperature measuring point 47 falls below the predetermined target value, the control flap 50 is correspondingly opened further, so that the gas supply to the line 34 and thus to the coke dry cooler 33 is increased.
  • the line 34 is used to recycle the gaseous cooling medium which is used in the coke dry cooler 33 to cool the hot coke coming from the coke oven battery, not shown.
  • the hot coke is fed in via line 69 in the upper part of the dry coke cooler 33, while the cooled coke is withdrawn from the lower part thereof via line 70.
  • the provided heat boilers 52 and 54 in which the hot gas emerging from the coke dryer cooler 33 is cooled again to a temperature of approximately 150.degree.
  • the two waste heat boilers 52 and 54 are connected to one another by the line (pipe system) 53, which is used for the feed water supply and steam discharge.
  • the line 71 branches off from the line 34, through which a partial flow of the gas is introduced into the central part of the coke dry cooler 33, in which the coke to be cooled still has a temperature of approximately 400-600 ° C.
  • the remaining part of the gas is simultaneously introduced into the lower part of the coke oven cooler 33 in a manner known per se.
  • the control flap 72 and the control flap 73 are provided in line 34 for the necessary regulation of the two partial flows. This procedure on the one hand reduces the pressure loss of the gas in the coke dryer cooler 33. On the other hand, this results in a favorable influence on the temperature differences between the gas and the coke to be cooled and, moreover, is associated with improved controllability both with regard to the gas supply and with regard to the heat removal from the coke to be cooled.
  • a combustion chamber 56 is additionally provided, to which a gaseous, liquid or solid fuel is fed via line 57 and the required oxygen (air) is fed via line 58. Since the hot flue gases produced during the combustion are too high at approx. 1400 ° C., water vapor is supplied via line 59, which was branched off from line 18. By adding water vapor, the flue gas temperature can be reduced to the desired value of, for example, 600 ° C., and at this temperature the gas is then fed via line 60 into the gas supply line 35.
  • the control flap 61 is provided in the line 60, so that the amount of gas released can also be throttled accordingly, if appropriate, and the combustion Chamber 56 can also be used as an additional heater if necessary.
  • FIG. 2 shows the representation of a cascade with horizontally installed heating pipes.
  • the gas supplied via the gas inlet line, not shown, passes through the opening 62 into the distribution box 63, in which the baffle plates 64 can be arranged.
  • the arrangement of these baffle plates 64 can be seen in FIG. 3, which shows a top view of the cascade shown in FIG. 2.
  • the baffle plates 64 have the task of distributing the gas evenly as it enters the cascade and partially separating the dust in the gas. This separated dust collects in the tapered lower part of the distribution box 63 and can be removed there from time to time.
  • the gas passes from the distribution box 63 into the horizontal heating pipes, which in the present case bear the reference symbol 36, which indicates that the cascade shown should be the first (top) cascade.
  • the cascades underneath also have the same construction.
  • the diameter of the heating pipes it has proven to be expedient if the diameter of the heating pipes in the first (top) cascade is larger than in the heating pipes of the cascades below.
  • the outer diameter of the heating pipes in the first cascade can be 60.3 mm and in the second and third th cascade be 48.3 mm.
  • the pipe diameter should be selected so that an average gas velocity of approx. 20 m / s can be maintained in the heating pipes. It has been shown that, if this gas velocity is maintained, no significant dust deposits on the pipe walls are to be expected.
  • the outside of the heating tubes can of course also be provided with a certain profile, for. B. the heating pipes as so-called. Fin tubes are designed. The coal to be heated flows, as can be seen from the statements made above, on the outside of the heating pipes from top to bottom.
  • the gases After passing through the heating pipes, the gases enter the rear distribution box 65 and from there via the opening 66 into the line (not shown), which either leads to the cascade below or to the gas outlet line 39.
  • the system can be quickly made operational again by closing the tube end in the distribution box 63. If an entire cascade fails, operation is not disrupted by the use of the other cascades.
  • the cascades are made of wear-resistant steel and can be stiffened with profile iron on the outside. They are each located in a housing (not shown in FIG. 2), which normally consists of a steel frame construction with wall plates that are insulated from the outside.
  • the individual cascades are connected to each other by compensators, which absorb the thermal expansion and prevent the transmission of vibrations.
  • the housing can also taper in the area of the inflow bases 4. This means that the inflow bases 4 then have a smaller diameter than the part of the housing above and below.
  • the coal to be preheated or dried is fed onto the cascade fluidized bed dryer 3 from above, so that the coal flows through it and thus onto the individual cascades from top to bottom.
  • the casings in which the cascades are accommodated are separated from one another by the gas-permeable inflow trays 4. These have the task of ensuring that the water vapor is distributed as evenly as possible at the entry into the coal-water vapor fluidized bed of the respective cascade.
  • the pressure loss of the inflow floor is only approx. 10-15% of the pressure loss of the coal-water vapor fluidized bed.
  • a grating 68 as the inflow base, which has been loaded with coarse coal 67, the grain size of which is approximately> 40 mm.
  • Fig. 4 shows a schematic representation of such an inflow floor.
  • sandwich floor This consists of two grids arranged one above the other and offset against each other, between which there is a gas-permeable packing layer.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
EP82103250A 1981-05-13 1982-04-17 Procédé et dispositif pour l'exploitation d'une installation de fours à coke Expired EP0064617B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT82103250T ATE15062T1 (de) 1981-05-13 1982-04-17 Verfahren und vorrichtung zum betrieb einer kokereianlage.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3118931 1981-05-13
DE19813118931 DE3118931A1 (de) 1981-05-13 1981-05-13 Verfahren und vorrichtung zum betrieb einer kokereianlage

Publications (3)

Publication Number Publication Date
EP0064617A2 true EP0064617A2 (fr) 1982-11-17
EP0064617A3 EP0064617A3 (en) 1984-03-28
EP0064617B1 EP0064617B1 (fr) 1985-08-21

Family

ID=6132152

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82103250A Expired EP0064617B1 (fr) 1981-05-13 1982-04-17 Procédé et dispositif pour l'exploitation d'une installation de fours à coke

Country Status (12)

Country Link
US (2) US4430161A (fr)
EP (1) EP0064617B1 (fr)
JP (1) JPS57198784A (fr)
AR (1) AR228393A1 (fr)
AT (1) ATE15062T1 (fr)
AU (1) AU547340B2 (fr)
BR (1) BR8202750A (fr)
CA (1) CA1195946A (fr)
DE (2) DE3118931A1 (fr)
ES (1) ES510104A0 (fr)
IN (1) IN158295B (fr)
ZA (1) ZA822644B (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0066096A2 (fr) * 1981-05-29 1982-12-08 Krupp Koppers GmbH Procédé de traitement thermique simultané de plusieurs courants de charbon
EP0273406A2 (fr) * 1986-12-31 1988-07-06 Rheinbraun Aktiengesellschaft Procédé et installation pour sécher du lignite dans un sécheur à lit fluidisé
KR101124629B1 (ko) * 2010-09-02 2012-03-20 주식회사 포스코 코크스 오븐의 석탄 장입 방법
DE102012012417B4 (de) 2012-06-25 2019-06-13 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur verbesserten Vorerhitzung von Kohle durch Wärmetausch mit dem Kühlgas einer Kokstrockenkühlanlage

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DE3615622A1 (de) * 1986-05-09 1987-11-12 Metallgesellschaft Ag Verfahren zur durchfuehrung endothermer prozesse
DE3615624A1 (de) * 1986-05-09 1987-11-12 Metallgesellschaft Ag Vorrichtung zur vorwaermung und gegebenenfalls trocknung feinkoerniger feststoffe
AT390018B (de) * 1988-05-05 1990-03-12 Waagner Biro Ag Verfahren und regenerationseinrichtung zur thermischen behandlung wie z.b. trocknung, verschwelung, vergasung pastoeser oder schlammartiger substanzen
US5361513A (en) * 1992-11-25 1994-11-08 Amax Coal Industries, Inc. Method and apparatus for drying and briquetting coal
US6655043B1 (en) * 2001-09-21 2003-12-02 Apac Inc. Dryer moisture indicator
US8197561B2 (en) 2001-10-10 2012-06-12 River Basin Energy, Inc. Process for drying coal
US7695535B2 (en) * 2001-10-10 2010-04-13 River Basin Energy, Inc. Process for in-situ passivation of partially-dried coal
KR100434737B1 (ko) * 2002-06-11 2004-06-07 주식회사 포스코 석탄건조기의 증기발생 방지장치
US8523963B2 (en) * 2004-10-12 2013-09-03 Great River Energy Apparatus for heat treatment of particulate materials
US7275644B2 (en) * 2004-10-12 2007-10-02 Great River Energy Apparatus and method of separating and concentrating organic and/or non-organic material
US7540384B2 (en) * 2004-10-12 2009-06-02 Great River Energy Apparatus and method of separating and concentrating organic and/or non-organic material
US8579999B2 (en) 2004-10-12 2013-11-12 Great River Energy Method of enhancing the quality of high-moisture materials using system heat sources
US7987613B2 (en) * 2004-10-12 2011-08-02 Great River Energy Control system for particulate material drying apparatus and process
US8062410B2 (en) 2004-10-12 2011-11-22 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
JP2007039608A (ja) * 2005-08-05 2007-02-15 Sumitomo Metal Ind Ltd コークス乾式消火設備の循環冷却ガス利用方法および利用設備
DE102007061136A1 (de) * 2007-12-19 2009-06-25 Glatt Ingenieurtechnik Gmbh Verfahren und Vorrichtung zur mehrstufigen Behandlung von dispersen Feststoffen
JP5473732B2 (ja) * 2010-04-02 2014-04-16 三菱重工業株式会社 低品位炭乾燥システム
US8956426B2 (en) 2010-04-20 2015-02-17 River Basin Energy, Inc. Method of drying biomass
US9057037B2 (en) 2010-04-20 2015-06-16 River Basin Energy, Inc. Post torrefaction biomass pelletization
US9475023B2 (en) 2011-07-27 2016-10-25 The Research Foundation Of The City University Of New York Optimum process design of packed bed type thermal storage systems and other applications
CN102967134B (zh) * 2012-11-30 2014-11-05 山东科院天力节能工程有限公司 一种回收废热蒸汽热量的干燥系统及工艺
JP5588077B1 (ja) * 2014-01-27 2014-09-10 長松院 泰久 小型蒸気発電機を添えたバイオマス回転乾燥装置
CN108559535B (zh) * 2017-12-29 2021-12-14 浙江百能科技有限公司 一种用于煤热解制高热值煤气和高热值块焦的多级换热装置
CN113091481A (zh) * 2021-04-15 2021-07-09 唐山市宝凯科技有限公司 一种桥管荒煤气余热回收装置及方法

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US3253650A (en) * 1960-07-11 1966-05-31 Frank J Mcentee Jr Heat-exchange apparatus
US3814176A (en) * 1973-01-22 1974-06-04 R Seth Fixed-fluidized bed dry cooling tower
FR2265840A1 (fr) * 1974-04-01 1975-10-24 Buettner Schilde Haas Ag
FR2314458A1 (fr) * 1975-06-13 1977-01-07 Waagner Biro Ag Procede de refroidissement de produits en vrac chauds et installation servant a son execution
EP0023455A1 (fr) * 1979-07-30 1981-02-04 Etablissement public dit: CHARBONNAGES DE FRANCE Procédé et installation de séchage et/ou préchauffage de charbon à cokéfier

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DE3013325C2 (de) * 1980-04-05 1985-07-18 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Verfahren zur Trocknung und Vorerhitzung von Kohle unter Ausnutzung der fühlbaren Kokswärme bei der trockenen Kokskühlung bzw. -löschung

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3253650A (en) * 1960-07-11 1966-05-31 Frank J Mcentee Jr Heat-exchange apparatus
US3814176A (en) * 1973-01-22 1974-06-04 R Seth Fixed-fluidized bed dry cooling tower
FR2265840A1 (fr) * 1974-04-01 1975-10-24 Buettner Schilde Haas Ag
FR2314458A1 (fr) * 1975-06-13 1977-01-07 Waagner Biro Ag Procede de refroidissement de produits en vrac chauds et installation servant a son execution
EP0023455A1 (fr) * 1979-07-30 1981-02-04 Etablissement public dit: CHARBONNAGES DE FRANCE Procédé et installation de séchage et/ou préchauffage de charbon à cokéfier

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0066096A2 (fr) * 1981-05-29 1982-12-08 Krupp Koppers GmbH Procédé de traitement thermique simultané de plusieurs courants de charbon
EP0066096A3 (en) * 1981-05-29 1984-03-28 Krupp-Koppers Gmbh Process for the simultaneous heat treatment of several coal streams
EP0273406A2 (fr) * 1986-12-31 1988-07-06 Rheinbraun Aktiengesellschaft Procédé et installation pour sécher du lignite dans un sécheur à lit fluidisé
EP0273406A3 (en) * 1986-12-31 1989-03-22 Rheinische Braunkohlenwerke Ag. Process and plant for drying lignite in a fluidised-bed dryer
KR101124629B1 (ko) * 2010-09-02 2012-03-20 주식회사 포스코 코크스 오븐의 석탄 장입 방법
DE102012012417B4 (de) 2012-06-25 2019-06-13 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur verbesserten Vorerhitzung von Kohle durch Wärmetausch mit dem Kühlgas einer Kokstrockenkühlanlage

Also Published As

Publication number Publication date
DE3265554D1 (en) 1985-09-26
BR8202750A (pt) 1983-04-19
US4470878A (en) 1984-09-11
AU547340B2 (en) 1985-10-17
CA1195946A (fr) 1985-10-29
ES8302070A1 (es) 1983-02-01
AU8361382A (en) 1982-11-18
US4430161A (en) 1984-02-07
ZA822644B (en) 1983-03-30
EP0064617A3 (en) 1984-03-28
AR228393A1 (es) 1983-02-28
ES510104A0 (es) 1983-02-01
IN158295B (fr) 1986-10-11
JPS57198784A (en) 1982-12-06
ATE15062T1 (de) 1985-09-15
DE3118931A1 (de) 1982-12-02
EP0064617B1 (fr) 1985-08-21

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