US3888742A - Pollution-free coal-preheating with waste heat from dry coke-quenching - Google Patents

Pollution-free coal-preheating with waste heat from dry coke-quenching Download PDF

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Publication number
US3888742A
US3888742A US435749A US43574974A US3888742A US 3888742 A US3888742 A US 3888742A US 435749 A US435749 A US 435749A US 43574974 A US43574974 A US 43574974A US 3888742 A US3888742 A US 3888742A
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Prior art keywords
coal
inert gas
drying
gas
coke
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US435749A
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English (en)
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Roland Kemmetmueller
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AMERICAN WAAGNER-BIRD Co Inc
WAAGNER BIRO AMERICAN
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WAAGNER BIRO AMERICAN
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Priority to US435749A priority Critical patent/US3888742A/en
Priority to AT21875A priority patent/AT359461B/de
Priority to GB308175A priority patent/GB1452454A/en
Priority to JP1009675A priority patent/JPS5342321B2/ja
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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
    • 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
    • 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
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • an inert completely dry [2]] Appl 435,749 gas is directed through a body of hot coke which has just been discharged from a coke oven in order to cool the hot coke, which is thus dry-quenched, while the [52] US. Cl. 201/39; 201/43; 202/150; inert gas becomes heated.
  • the hot inert gas is the 202/228 laced directly in contact with the wet coal so that the P l] ll'lt.
  • the coke which is discharged from the coke oven is placed in contact with a gas so as to carry out dry-quenching of the coke, and the gas which extracts heat from the coke in this way is then directed through a heat exchanger so that in the heat exchanger heat is taken from the dry-quenching gas which may then be returned to the coke from the coke oven in order to further dry quench coke and extract additional heat therefrom.
  • a second gas which is heated by the heat exchanger may be used for purposes such as drying and preheating coal.
  • an inert gas is circulated along a closed path while being directed in a perfectly dry state through a body of hot coke shortly after discharge of the latter from a coke oven so that the inert gas will cool the hot coke while extracting heat therefrom, thus raising the temperature of the inert gas.
  • Wet coal is fed to a part of the path to which the thus-heated inert gas travels after passing through the body of hot coke so that the wet coal is dried by direct contact with the heated inert gas.
  • the inert gas is cooled while drying the coal with the heat extracted from the hot coke as a result of the direct contact between the wet coal and the heated inert gas.
  • the coal which is dried in this way is delivered to a coke oven while the inert gas is cleaned, dried, and then returned along the closed path of flow thereof to a body of hot coke to again be heated by the latter before again returning to the location where the wet coal is situated in order to be dried by the heated inert gas.
  • the temperature of the inert gas which contacts the wet coal is sufficiently high to bring about not only drying of the coal but also preheating thereof, so that in this way a dry preheated coal is available for supply to the coke oven.
  • a dry-quenching bunker means is provided to contain a body of hot coke received from a coke oven, and a coal-drying means is provided for drying coal prior to delivery of the coal to a coke oven.
  • a conduit means has one portion extending from the bunker means to the coal drying means and another portion extending from the coal-drying means to the bunker means, so that the conduit means defines with the bunker means and the coal-drying means a closed path along which an inert gas may be circulated for extracting heat from the hot coke in the bunker means during dry quenching of the hot coke and for then drying the coal with heat extracted from the hot coke during direct contact between the coal and the inert gas prior to return of the inert gas to the bunker means.
  • a means is provided at the portion of the conduit means carrying gas from the coal-drying means to the bunker means for cleaning and drying the gas, so that the inert gas is completely free of moisture when reaching the hot coke.
  • FIGS. IA and 1B which are a continuation of each other, illustrate schematically one possible method and apparatus according to the present invention
  • FIG. 13 there is schematically illustratcd at the right thereof it dryouenching bunker which is charged with hot coke pushed out of a col-re oven.
  • the hot coke is charged into the bunker it) through the top end thereof which in a known v ry is provided with n closure assembly 1.2.
  • this assembly 12 closes off the interior of the bunker it; from the outer atmosphere.
  • the closure assembly 3 is cupublc of being opened in a known way to receive a charge of hot coke directly from a coke oven.
  • the Ct lLL' After the Ct lLL' is cooled in the dryt'lurnching bunker it) it is discharged out oi the lower dis hurgc end 11 thereof also in a known way.
  • the bunker H At the lower end l-i the bunker H) is provided with suitable gates which are known and which control the discharge of the cooled coke from the coke oven. this tokc being screened und delivered to suitable bins where it is available for use in blast furnaces, for example.
  • the coke When the coke is discharged f om the dry-quenching bunker lfi it has a temperature on the order of fifl -itl F, since at this temperature the coke has been cooled sulficientiy so that will not burn belt conveyers.
  • the inert gas which flows upuuirdly through the hot col-re in older to cool that latter while extracting heat therefrom is preferably nitrogen or Lt mixture of nitrogen and carbon dioxide.
  • This inert gas fed in a pen lectly dry condition to the lower end region ol the bunker lit by may of u recirculating fun 18 which drives the 1 ii conduit 20 into the interior of the limiter i r.
  • the hitter carries a ditching; head 22 in the form ct i: holiow i orrir-oncnt oi"snbstuntiuiiy cii niczrl coniigw rio the interior ol which the inert gals is delivi t d with opcn t in; to litW f, the body oi hot raise in buniicr i ga r 1 us out o 'theuci i cr lit at ti tempera or" tit l -hi b' if and iziirriedi; .ly gion oi" the bur :er thicott'w tiir lgli tlz: ninlticyclrtne is removed l'toni the inert gas, This t is r .lll gil
  • timing ripper coils llilfl hm n dr mr from which the steam is delivered through suitable stcam'main 34 to any desired location where use will be made of the steam which is generated in this way.
  • Part of the inert gas, which is still in a perfectly dry condition. is returned from the steam generating means 26 to a conduit 36 which communiates with the suction end of the recirculating fan 18, and through the conduit 36 the perfectly dry inert gas is returned to the fan 18 to be delivered thereby to the bunker 10 as described above
  • the proportion of inert gas from the steam generating means 26 which is mixed with the inert gas flowing along the conduit 36 can be controlled by a valve 38 in the conduit 40 which communicates with the conduit 36 and with the lower end region of the steam generator 26. It will be noted that additional dust is delivered out of the steam generator 26. This dust also is combustible and forms a valuable product.
  • the inert gas flowing along the conduit 40 to the conduit .36 will have a temperature on the order of flOtl lftl C and approximately 30 percent of the gas delivered by the fan 18 to the bunker 10 will be derived from the conduit 40 the remaining 70 percent being derived through the conduit 36 which in a manner described below delivers a cool dry inert gas to the fan 18, this latter gas which flows along the conduit 36 to join with the gas from the conduit 40 having a temperature on the order of 0l0" C in this way the temperature or the gas flowing into the bunker 10 can be controlled.
  • the flow of the inert gas from the the steam gener utor means 26 along the conduit 42 is controlled by a valve or damper 46, and the arrangement is such that a completely dry gas having a temperature on the order of nutr ent C flows out of the steam generator means 2s along the conduit 42.
  • a valve or damper 46 Of the inert gas which flows to the waste-bent boiler 26 from the bunker l0, approxhnntely two thirds of the will flow out of the boiler is along the conduit 42 while the remaining inert gas "will llo-w along the conduit 40 to be recirculated back :11 the bunker by way ofthe fan 18 together with the re muining cool inert gas derived from the conduit 36 uperun of its connection with the conduit 40.
  • the conduit 42 may he provided with an auxiliary gas burner 18 for starting purposes, this unit being used oniy at the beginning ofau operating cycle, and the initinl heating provided by way of the unit 48 will serve to pct! :ratc is certain amount of inert gas.
  • Part of the dust tlisclmrgotl out of the units 24 and 26 may be used in the nuxi iary gus burner 48a itcl'trring now to FIG. 1A, it will be seen that the perf ctly dry inert gas which in the above example is at a rw-riipcrnture on the order of 600-o50 C reaches a trmlvlrying means St).
  • ? r ng on runs 50 is at twostagc dryer, and the hot. flows through the second stage 52 of Wilt) 5t] before reaching the first stage 54 thereof.
  • the coal-drying means 50 the coal is dried in a countercurrent manner with respect to the flow of inert gas in the sense that the second stage 52 is situated upstream of first stage, but in each stage the coal flows concurrently with the gas so that concurrent drying takes place in each stage of the coal-drying means while the stages thereof are arranged in a countercurrent manner with respect to the flow of inert gas.
  • FIG. IA a two-stage dryer is illustrated in FIG. IA and described in detail below, the invention can equally well be used with a single stage dryer or with a fluidized bed type of coal dryer installation.
  • the first stage dryer unit 54 is in the form of an elongated tubular structure which has an upstream end region 56 communicating with a conduit 58 through which the heated inert gas flows into the tubular structure of the first stage unit 54 in order to dry coal therein.
  • the wet coal is fed in a crushed particulate form, after passing through suitable crushing mills as is well known, into the tubular structure of the dryer unit 54 at the region of the upstream end 56 thereof.
  • FIG. 1A shows schematically a wet coal feed means 60 which serves to feed the wet coal in particulate form into the tubular structure of the first stage unit 54.
  • the particles of wet coal become suspended in the flowing stream of inert gas to be be carried along with the gas, while being dried thereby, toward the downstream end region 62 of the unit 54.
  • This end region 62 is provided with a pair of classifier units 64 and 66.
  • the larger and therefore heavier coal particles will discharge out of the classifier outlet 64 while the smaller and lighter coal particles will discharge out of the subsequent classifier outlet 66.
  • a classification is carried out to separate particles which are larger than a given size from coal particles which are smaller than a given size.
  • the particles larger than a given size which discharge out of the classifier outlet 64 are carried along with part of the inert gas through a conduit 68 to a hammer mill 70 which is situated outside the path of flow of the inert gas and the coal suspended therein, and in the hammer mill the size of the particles is further reduced after which the particles of reduced size are returned to the tubular structure of the first stage dryer unit 54 through a conduit 72, as schematically represented in FIG. 1A.
  • the invention provides outside of the path of flow of the inert gas and the coal suspended therein a means for reducing the size of coal particles which are greater than a given size.
  • the inert gas with the coal particles suspended therein is received by a first stage cyclone means 76 wichh includes a number of cyclones in which the particles of coal dried at the first stage 54 are separated from the inert gas.
  • the inert gas continues to flow beyond the cyclone separator means 76 along a conduit 78 where the inert gas has a temperature on the order of 1 10 C.
  • the particles of coal which are discharged from the cyclone means 76 are received by a conveyer means 80 such as a suitable screw conveyer, as schematically illustrated, and these particles of coal which are dried in the first stage unit 54 are delivered by the conveyer 80 through a conduit 82 into an upstream end region 84 of the tubular structure 86 which forms the second stage unit 52 of the coal-drying means 50.
  • a conveyer means 80 such as a suitable screw conveyer, as schematically illustrated
  • these particles of coal which are dried in the first stage unit 54 are delivered by the conveyer 80 through a conduit 82 into an upstream end region 84 of the tubular structure 86 which forms the second stage unit 52 of the coal-drying means 50.
  • the temperature of the inert gas is higher than in the first stage unit 54, the temperature of the gas at the second stage being on the order of 600 C, as pointed out above.
  • the coal particles flow together with the inert gas toward the upstream end of the conduit 58 which interconnects the first and second stages, and in this second stage unit 52 the coal not only has been completely dried but is preheated to a temperature well above the ambient temperature so that coal in completely dry and preheated condition is discharged out of the second stage 52 of the coal-drying means 50.
  • the downstream end of the second stage unit 52 communicates also with a cyclone means 88 which include a plurality of second stage cyclones in which the inert gas is separated from the dry and preheated coal. This inert gas which is thus separated from the particles of coal at the second stage then flows through the conduit 58 to the first stage.
  • the dry and preheated coal is received from the sec 0nd stage cyclone means 88 by a conveyer means 90 which may also take the form of a suitable screw conveyer. It is to be noted that during drying and preheating the coal has been maintained entirely out of contact with oxygen.
  • the conveyer means 90 delivers the dry preheated coal to a plurality of hot coal bins 92 which form a bin means in which the dry, preheated coal is temporarily stored prior to delivery to a larry car installation 94 which serves in a known way to deliver the dry, preheated coal to the coke ovens as schematically illustrated in FIG. 1A.
  • the gas which discharges from the larry car unit 94 is delivered to a scrubber means 96 where the gas is cleaned before being discharged to the outer atmosphere so that pollution is in this way avoided, a suitable blower 98, or the like, being provided to draw the gases out of the larry car unit 94 and through the scrubber means 96 before discharging the clean gas to the outer atmosphere.
  • the gas discharged after the scrubber 96 by the fan 98 will still for the most part be in the form of an inert gas, and in this case the inert gas can be returned to any desired part of the closed path of flow along which the inert gas circulates in accordance with the invention. as will be apparent from the further description below.
  • an inert gas derived from any suitable source such as a nitrogen tank or the like is delivered to the interior of the bins 92 into upper regions thereof to form an inert gas cushion over the dry preheated coal which is temporarily stored in these bins.
  • the inert gas which thus forms the gas cushions over the dry. preheated coal in the bins 92 is capable of escaping through the conveyer means 90 into the second stage cyclone means 88 to be combined with inert gas flowing through the second stage dryer unit. so that in this way the inert gas which forms the gas cushions above the preheated coal in the coal bins also serves to make up any losses in the continuously circulating inert gas which flows first through the bunker l and then through the coal-drying means 50.
  • the inert gas which flows along the conduit 78 from the first stage cyclones 76 is delivered to a scrubber and condenser means 100.
  • the scrubber means 100 thus receives the cooled inert gas which has a temperature on the order of 100 C together with water vapor which has been removed from the coal during the drying thereof. in the scrubber and condenser means 100 the water is quenched out of the gas.
  • the scrubber means 100 may be a single or two-stage scrubber and spray water is pumped into the scrubber means 100 by way of a suitable pump 102. After traveling through the scrubber the gas flows through a demister unit 104 which serves further to remove any moisture from the gas.
  • the liquid which is removed being delivered to a clarifier means 106 which discharges the condensate and slurry.
  • Make-up water if required is delivered to the clarifier 106 with this water being delivered to the spray water pump I02.
  • the gas which has been dried flows from the demister unit 104 along a conduit 108 to the inlet of the system fan 110 with part of the gas being discharged to the outer atmosphere through a suitable vent unit 112 controlled by a valve or damper 114, so that in this way balanced operating conditions are maintained.
  • the gas in conduit 108 is a saturated gas at the dew point temperature of 30-40 C. This gas has on the order of 0.02 grams of water in each cubic meter of gas.
  • the system fan 110 delivers the inert gas to a conduit 116 which serves to deliver the inert gas to a cooling means 118.
  • a conduit 120 may be provided if desired to interconnect the conduits 116 and 42. This conduit 120 is optional. it may be used to deliver part of the inert gas directly from fan 110 to the conduit 42 in order to be combined with the hot inert gas from the steam generating means 26 before reaching the second stage dryer unit 52. If the connecting conduit 120 is provided, it will be equipped with a valve or damper 122 enabling the proportion of gas which flows from the conduit 116 to the conduit 42 to be regulated.
  • the inert gas may be a mixture of nitrogen and carbon dioxide and this inert gas flows from the demister unit 104 to the system fan 110 at a temperature on the order of 30-40 C.
  • desulfurization if necessary, is carried out at the demister unit 104. In this way a relatively cool. relatively dry, clean gas is delivered to the recirculating gas cooler means 118.
  • This cooling means 118 forms part of a refrigerating unit in which through suitable coils a refrigerant is circulated as by a compressor means 124, suitable cooling water being directed through a section 126 of the cooling means as illustrated in FIG. 1B.
  • the cooling installation 118 will include suitable compressors 124 which must be driven. and for this purpose in accordance with a further feature of the invention steam is tapped from the main 34 and delivered by way of a conduit 128 to the steam turbine unit 130 of the cooling means 118 so as to drive the compressors 124 thereof. Condensate from turbine 130 is delivered by conduit 131 to unit 126 together with the cooling water and is then fed by a pump and conduit to feedwater supply 44.
  • the temperature of the gas is lowered to the order of 05 C. and all moisture in the gas is condensed out of the gas at the cooling means H8, with the condensate being received by the conduit 132 which serves to deliver the condensate to the condensate treating unit 134 from which gas is discharged by the conduit 136 while the condensate is discharged by the outlet 138.
  • the temperature of the inert gas when it contacts the wet coal is sufficiently high not only to dry the coal but also to elevate the temperature thereof to a temperture substantially above the ambient temperature, for preheating the coal, and delivering the coal in a dry preheated condition to the coke oven.
  • the gas-drying step includes cooling the inert gas to condense moisture therefrom just before it returns to a body of hot coke, while utilizing at least as part of a source of energy for cooling the inert gas at least some of the steam generated with the inert gas during the partial cooling of the latter.
  • the gas-drying step includes cooling the inert gas to condense moisture therefrom just before it reaches a body of hot coke for extracting heat therefrom.
  • a coke plant dry-quenching bunker means for containing a body of hot coke received from a coke oven, coal-drying means for drying coal prior to delivery of the coal to a coke oven, conduit means having one portion extending from said bunker means to said coal-drying means and another portion extending from said coal-drying means to said bunker means, so that said conduit means defines with said bunker means and coal-drying means a closed path along which an inert gas may be circulated for extracting heat from hot coke in said bunker means during dry-quenching of the hot coke and for then drying coal with heat extracted from hot coke during direct contact between the coal and the inert gas prior to return of the inert gas to the bunker means, and gas-drying means operatively connected with that portion of the conduit means which delivers the inert gas to said bunker means for extracting all moisture from the inert gas, so that the inert gas is in a completely dry condition when reaching the bunker means.
  • said gas-drying means includes a gas-cooling means operatively connected with that portion of the conduit means which delivers the inert gas to said bunker means for condensing moisture out of the inert gas.
  • a steam generating means is operatively connected with that portion of the conduit means which delivers the inert gas from the bunker means to the coal-drying means for partially cooling the inert gas while generating steam therefrom prior to drying of the coal with the inert gas, and means for directing part of the generated steam from said steam-generating means to said gascooling means for operating the latter at least partially with steam generated from the inert gas during the partial cooling thereof.
  • a conveyer means communicates with said coal-drying means for conveying dry coal away from the latter, bin means communicating with said conveyer means for receiving the dry coal therefrom and storing the dry coal prior to delivery thereof to a coke oven, and inert gas supply means communicating with said bin means for maintaining a cushion of inert gas over dry coal stored at said bin means.
  • said coal-drying means includes an elongated tubular structure having an upstream end connected to said one portion of said conduit means which receives the inert gas from said bunker means and a downstream end portion from which the inert gas flows after drying coal in said elongated tubular structure.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)
US435749A 1974-01-23 1974-01-23 Pollution-free coal-preheating with waste heat from dry coke-quenching Expired - Lifetime US3888742A (en)

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Application Number Priority Date Filing Date Title
US435749A US3888742A (en) 1974-01-23 1974-01-23 Pollution-free coal-preheating with waste heat from dry coke-quenching
AT21875A AT359461B (de) 1974-01-23 1975-01-14 Verfahren und einrichtung zur trocknung und vorerhitzung von kohle
GB308175A GB1452454A (en) 1974-01-23 1975-01-23 Coke plant
JP1009675A JPS5342321B2 (enrdf_load_stackoverflow) 1974-01-23 1975-01-23

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US (1) US3888742A (enrdf_load_stackoverflow)
JP (1) JPS5342321B2 (enrdf_load_stackoverflow)
AT (1) AT359461B (enrdf_load_stackoverflow)
GB (1) GB1452454A (enrdf_load_stackoverflow)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2318919A1 (fr) * 1975-07-24 1977-02-18 Inland Steel Co Procede pour la recuperation de fines particules de charbon dans un prechauffeur
US4009080A (en) * 1974-10-16 1977-02-22 Osaka Gas Company, Ltd. Method of treating waste combustion gas from coke oven
DE2719189A1 (de) * 1977-04-29 1978-11-09 Still Fa Carl Verfahren zum betrieb einer kohlevortrocknungs- bzw. -erhitzungsanlage in verbindung mit einer kokerei
US4176011A (en) * 1976-10-19 1979-11-27 Firma Carl Still Method for operating coke oven chambers in connection with a predrying plant for the coal
US4240877A (en) * 1978-05-02 1980-12-23 Firma Carl Still Gmbh & Co. Kg Method for preheating coal for coking
US4284477A (en) * 1978-06-26 1981-08-18 Mansfield Carbon Products, Inc. Coking apparatus for producing coke
US4284476A (en) * 1978-07-24 1981-08-18 Didier Engineering Gmbh Process and apparatus for utilization of the sensible heat of hot coke for drying and preheating coking coal
US4308102A (en) * 1977-08-26 1981-12-29 Didier Engineering Gmbh Process and apparatus for drying and preheating coking coal by means of flue gas
US4354903A (en) * 1980-04-05 1982-10-19 Firma Carl Still Gmbh & Co. Kg Process for drying and preheating coal utilizing heat in dry cooling or quenching of coke
DE3123141A1 (de) * 1981-06-11 1982-12-30 Krupp-Koppers Gmbh, 4300 Essen Verfahren und vorrichtung zum betrieb einer kokereianlage
EP0151727A3 (de) * 1984-02-10 1987-01-14 Preussag Stahl Aktiengesellschaft Verfahren zur Nutzung der beim Trockenkühlen von Koks mittels eines Gases anfallenden fühlbaren Wärme
CN103484139A (zh) * 2013-10-12 2014-01-01 赛鼎工程有限公司 一种用于炼焦煤调湿的工艺
CN106566569A (zh) * 2016-10-27 2017-04-19 武汉悟拓科技有限公司 基于煤调湿的干法熄焦同步制备水煤气系统

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2733365C3 (de) * 1977-07-23 1980-06-19 Didier Engineering Gmbh, 4300 Essen Verfahren zur Nutzung der fühlbaren Kokswärme an einer Verkokungsanlage
DE2841088C2 (de) * 1978-09-21 1982-04-08 Bergwerksverband Gmbh Verfahren und Vorrichtung zur Trocknung und Vorerhitzung von Kokskohle in einem einzigen Flugstromrohr

Citations (4)

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Publication number Priority date Publication date Assignee Title
US1854407A (en) * 1927-11-03 1932-04-19 U G I Contracting Company Means for preheating coal and cooling coke
US2289917A (en) * 1942-07-14 Process of continuous carbonization
US3728230A (en) * 1972-02-07 1973-04-17 Waagner Biro American Indirectly heat exchanging plural gas streams for dry quenching hot coke and drying coal
US3843458A (en) * 1972-02-07 1974-10-22 Waagner Biro American Coal treating method and apparatus for coke plants

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2289917A (en) * 1942-07-14 Process of continuous carbonization
US1854407A (en) * 1927-11-03 1932-04-19 U G I Contracting Company Means for preheating coal and cooling coke
US3728230A (en) * 1972-02-07 1973-04-17 Waagner Biro American Indirectly heat exchanging plural gas streams for dry quenching hot coke and drying coal
US3843458A (en) * 1972-02-07 1974-10-22 Waagner Biro American Coal treating method and apparatus for coke plants

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4009080A (en) * 1974-10-16 1977-02-22 Osaka Gas Company, Ltd. Method of treating waste combustion gas from coke oven
FR2318919A1 (fr) * 1975-07-24 1977-02-18 Inland Steel Co Procede pour la recuperation de fines particules de charbon dans un prechauffeur
US4176011A (en) * 1976-10-19 1979-11-27 Firma Carl Still Method for operating coke oven chambers in connection with a predrying plant for the coal
DE2719189A1 (de) * 1977-04-29 1978-11-09 Still Fa Carl Verfahren zum betrieb einer kohlevortrocknungs- bzw. -erhitzungsanlage in verbindung mit einer kokerei
US4308102A (en) * 1977-08-26 1981-12-29 Didier Engineering Gmbh Process and apparatus for drying and preheating coking coal by means of flue gas
US4240877A (en) * 1978-05-02 1980-12-23 Firma Carl Still Gmbh & Co. Kg Method for preheating coal for coking
US4284477A (en) * 1978-06-26 1981-08-18 Mansfield Carbon Products, Inc. Coking apparatus for producing coke
US4284476A (en) * 1978-07-24 1981-08-18 Didier Engineering Gmbh Process and apparatus for utilization of the sensible heat of hot coke for drying and preheating coking coal
US4354903A (en) * 1980-04-05 1982-10-19 Firma Carl Still Gmbh & Co. Kg Process for drying and preheating coal utilizing heat in dry cooling or quenching of coke
DE3123141A1 (de) * 1981-06-11 1982-12-30 Krupp-Koppers Gmbh, 4300 Essen Verfahren und vorrichtung zum betrieb einer kokereianlage
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CN103484139A (zh) * 2013-10-12 2014-01-01 赛鼎工程有限公司 一种用于炼焦煤调湿的工艺
CN103484139B (zh) * 2013-10-12 2014-11-05 赛鼎工程有限公司 一种用于炼焦煤调湿的工艺
CN106566569A (zh) * 2016-10-27 2017-04-19 武汉悟拓科技有限公司 基于煤调湿的干法熄焦同步制备水煤气系统
CN106566569B (zh) * 2016-10-27 2019-03-12 武汉悟拓科技有限公司 基于煤调湿的干法熄焦同步制备水煤气系统

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GB1452454A (en) 1976-10-13
JPS50113501A (enrdf_load_stackoverflow) 1975-09-05
AT359461B (de) 1980-11-10
JPS5342321B2 (enrdf_load_stackoverflow) 1978-11-10
ATA21875A (de) 1980-04-15

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