EP0073368A2 - Chauffage de charbon - Google Patents

Chauffage de charbon Download PDF

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Publication number
EP0073368A2
EP0073368A2 EP82107206A EP82107206A EP0073368A2 EP 0073368 A2 EP0073368 A2 EP 0073368A2 EP 82107206 A EP82107206 A EP 82107206A EP 82107206 A EP82107206 A EP 82107206A EP 0073368 A2 EP0073368 A2 EP 0073368A2
Authority
EP
European Patent Office
Prior art keywords
coal
solids
traveling layer
dryer
heating
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
EP82107206A
Other languages
German (de)
English (en)
Other versions
EP0073368A3 (en
EP0073368B1 (fr
Inventor
Vladan Dr. Dipl.-Ing. Petrovic
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 AT82107206T priority Critical patent/ATE24331T1/de
Publication of EP0073368A2 publication Critical patent/EP0073368A2/fr
Publication of EP0073368A3 publication Critical patent/EP0073368A3/de
Application granted granted Critical
Publication of EP0073368B1 publication Critical patent/EP0073368B1/fr
Expired legal-status Critical Current

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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
    • C10B57/10—Drying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/18—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact
    • F26B3/20—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source being a heated surface, e.g. a moving belt or conveyor
    • F26B3/205—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source being a heated surface, e.g. a moving belt or conveyor the materials to be dried covering or being mixed with heated inert particles which may be recycled

Definitions

  • the invention relates to a method for heating cold, moist coal, in particular coal intended for subsequent coking, and a device for carrying out the method.
  • the coal intended for coking is generally at ambient temperature (0 - 20 ° C) with a water content of up to 15% and a grain size distribution of 1 - 10 mm, with approx. 85% of the grain sizes being ⁇ 3 mm.
  • the coking properties are important for their use in the coke oven, characterized by dilatation, degree of swelling, fluidity, etc. It is known that by heating the coal to 200-250 ° C., the cooking time of the coke in the oven can be reduced considerably, e.g. B. from 20 h to 14 h by the water is removed to a slight residual content by heating. It is important that the coking properties of the coals are not impaired when heated. On the contrary, it has been found that the coking of the coal in the coke oven can be improved by proper heating, so that even coal that is difficult to coke without pretreatment can be used successfully in the coke oven.
  • coal heating must therefore be carried out carefully. In order to prevent oxidation, coal heating must be operated largely free of oxygen.
  • a number of process principles are known for carrying out coal heating, some of which are already being carried out on an industrial scale, such as, for. B. heating by hot gases in the entrained flow or by indirect heating via heat exchange surfaces in dryers or by direct heating by hot gases in moving bed, for example in a rotating drum.
  • a plant for heating coal can be operated particularly advantageously with regard to the energy consumption of the coking plant if the energy obtained during cooling of the coke produced can be used for heating the coal, as is done in the earlier patent application P 31 18 931.8.
  • the invention has for its object to provide a method which combines economical energy consumption with low investment costs and which ensures the protection of the properties of coal which are valuable in terms of coking technology and avoids comminution of the coal particles.
  • hot solids are added to the coal, the starting temperature of which is above the desired final temperature of the coal.
  • solid bodies are to be used which have a largely uniform shape without edges, sharp corners, projections or notches.
  • Solid bodies with a spherical shape are particularly suitable.
  • solid bodies with a narrow size range for example spheres of uniform size, preferably with a diameter of less than 40 mm, for thorough mixing of the coal with the heat-transferring solids.
  • the solids can consist of metallic materials, preferably steel or cast iron, or of non-metallic materials, for example ceramic or porcelain. Solid materials made of mechanically resistant and temperature-resistant plastics can also be used.
  • the solids can also be of natural origin, e.g. B. pebbles, which should be selected in a certain shape and size. Essential when choosing the material for the solids is that it is resistant to abrasion. Mechanical abrasion resistance according to DIN 52108 of less than 0.45 cm 3 / cm 2 is preferred for non-metallic materials.
  • the thermal properties of the solids are of particular importance. Solids with a heat coefficient of less than 16,000 (J / m 2 K s 0.5 ), preferably less than 5,000 (J / m 2 K s 0.5 ) are recommended.
  • the temperature control number should be less than 700.10 -4 (m 2 / h), preferably less than 150. 10 -4 (m 2 / h), and the specific heat of the solids greater than 400 (J / kg K), preferably greater than 800 (J / kg K).
  • efforts will of course be made to keep the amount of heat-transferring solids small in relation to the amount of coal to be heated. It is therefore advantageous to select solids that have the highest possible heat storage capacity.
  • the operating temperature of the heat-transferring solid bodies is limited. It has proven to be advantageous not to raise the temperature of the solids above 500 ° C. and to select solids from a material whose heat penetration number and temperature coefficient allow slow and gentle transfer of the thermal energy stored in the solid to the coal.
  • the solids can be heated in any way.
  • a preferred embodiment provides for the use of the hot cooling gases occurring here in the presence of a coke dry cooling system within the coking plant. These cooling gases can be introduced into a container holding the solid and release some of their sensible heat there before they flow back to the coke-drying cooling system.
  • Another possibility for heating the solid bodies is to provide a separate combustion chamber and to bring the flue gases generated there by means of a solid, liquid or gaseous fuel into heat exchange with the solid bodies.
  • the installation of such a combustion chamber is recommended in. the rest even if a coquette drying plant is available.
  • This combustion chamber then ensures that the coal is heated to the desired extent even in the event of a failure or malfunction of the coke oven cooling system. Since the flue gases generated during combustion are too high at around 1400 ° C to heat the coal, this can be reduced to the required value, for example by adding water vapor.
  • the moist coal from the coal bunker A is fed to the device for heating the coal F via the metering device B with the heated solids from the solid-state heater C via a metering device D by means of a suitable distributor device E.
  • Coal and solids pass through this facility in direct current. The solids give off part of the energy stored in them to the coal. The expelled coal moisture is drawn off via suitable vapor rooms.
  • the coal thus heated is in a suitable separation device G, z. B. a vibrating screen, separated from the solids and supplied to the coke oven in a suitable manner.
  • the solids are fed back to the solids heater C again, for example by a bucket elevator H.
  • the solid-state heater C can be operated with flue gases from a furnace. It is particularly advantageous with regard to the energy consumption of the coking plant to use the hot gases from dry coke cooling.
  • the heating gas supply is designated I, the heating gas outlet K.
  • Fig. 2 1 denotes the feed bunker, from which the moist coal is continuously fed via a rotary valve 2 into the Traveling layer dryer 3, which in the present case is designed as an upright, cylindrical container, is introduced. Solid materials, for example in the form of steel balls, are also continuously fed from the heater 4 via the cellular wheel sluice 5 to the traveling bed dryer.
  • the coal and the added balls flow continuously through the traveling layer dryer from top to bottom, whereby the coal and balls are kept in constant motion by the agitator 6 with the agitator arms 7.
  • the drive of the agitator is designated 8.
  • the agitator thus ensures that new coal grains always come into contact with the hot balls, so that the coal as a whole is subjected to an essentially uniform heat treatment.
  • the resistances in the downward flow of the coal are overcome by its own weight and the weight of the balls, the variable residence time of the coal in the traveling bed dryer being determined by the withdrawal of the coal and the balls in the lower region.
  • coal and balls are discharged from the traveling layer dryer 3 by means of a screw conveyor 9, which leads to a pneumatic separating device 10.
  • the coal which has now been heated to approximately 200 ° C., is separated from the balls with the aid of the carrier gas supplied through line 11 and transported via line 12 to the coal tower (not shown here) with an upstream separator.
  • the specifically heavier balls fall into the collecting container 13 and become through the transport device 14 (chain conveyor, bucket elevator or the like.) Returned to the heater 4.
  • the discharge of coal and balls from the traveling bed dryer can also be supported by a bunker emptying device 15 of a suitable design arranged in its lower region.
  • the vapor-containing vapors separated from the moist coal in the traveling layer dryer 3 are drawn off in various levels via the lines 16 and the collecting line 17 and pass via the cyclone 18, the line 19 and the blower 20 into the circuit washer 21, in which, in addition to condensation, the leaching of contamination.
  • a venturi washer could of course also be used.
  • coal grains separated in the cyclone 18 pass via the cellular wheel lock 22 and the line 23 to the separating device 10, from where they are conveyed together with the heated coal to the coal tower already mentioned.
  • the liquid running out of the circuit washer 21 is fed via the line 24 and the pump 25 to the cooling tower 26, in which the further cooling takes place to approximately 20 ° C.
  • the cooled liquid is then introduced into the cooling water distributor 28 via the line 27. From here, the required cooling water is fed back via lines 29 31 to the different levels of the circuit washer 21.
  • the gases escaping from the circuit washer are drawn off through line 32 and passed to the chimney, not shown.
  • the hot stream of the cooling gases emerging from the upper part of the coke dry cooler 33 at a temperature of approximately 800 ° C. is drawn off through the line 34. From this branches off the line 35, through which a partial flow of the gases is passed over the heat exchanger 36 and is then reintroduced into the coke dryer cooler.
  • the remaining hot cooling gases pass through line 37 to heater 4, in which they are used for heat transfer to the balls located therein. These gases leave the heater through line 38 and, after passing through blower 39, are introduced into line 35 at a temperature of approximately 220 ° C. From this line, part of the gases is introduced through line 61 into the middle and another part through line 62 into the lower part of the coke oven cooler.
  • Line 40 branches off from line 38, through which a partial flow of the gas through the chimney 41 can be blown off into the atmosphere.
  • a bypass line 42 is provided behind the blower 39 and is connected to the line 37 to the heater 4. This bypass line allows cold gas from line 38 to be mixed with the hot gas flowing out of line 34 from the coke oven cooler for temperature control purposes.
  • a combustion chamber 43 is additionally provided, to which a gaseous, liquid or solid fuel is fed via line 44 and the necessary combustion air is fed via line 45 becomes. Because it arises during combustion hot flue gases at approx. 1400 ° C are too high a temperature, water vapor is fed through line 46, which is branched off from line 19. By adding water vapor, the flue gas temperature can be reduced to the desired value of, for example, 800 - 900 ° C. At this temperature, the flue gas is then via the line 47 in the Er-. Heater 4 leading line 37 fed. Finally, a control flap (not shown here) is also provided in line 47, so that the amount of gas released may also be throttled accordingly and the combustion chamber 43 can also be used as an additional heater if necessary.
  • FIG. 3 differs from that according to FIG. 2 only in that a vibrating screen 48 is provided as a separating device below the traveling layer dryer. From this the balls in turn fall into the collecting container 13, while the coal reaches a bucket elevator 50 via the line 49, which transports it to the coal tower (not shown).
  • a vibrating screen 48 is provided as a separating device below the traveling layer dryer. From this the balls in turn fall into the collecting container 13, while the coal reaches a bucket elevator 50 via the line 49, which transports it to the coal tower (not shown).
  • FIG. 4 again shows an upright traveling layer dryer 3, in which, however, the separating device in the form of a vibrating screen 51 is installed in the lower region of the traveling layer dryer itself.
  • the separated balls return to the collecting container 13.
  • the coal is transported to the bucket elevator 50 by means of a screw conveyor 52 and the line 49.
  • electromagnets 53 may also be provided offset on the outside of the moving bed dryer, which are periodically activated and keep the steel spheres distributed in the dryer.
  • the dwell time of the coal in the moving bed dryer is determined on the one hand by the screw conveyor 52 and on the other hand by the position of the throttle flaps 54 in the interior of the traveling bed dryer.
  • the traveling layer dryer 3 is designed as a floor dryer.
  • the added coal and the balls are mixed by the agitator 6 with the agitator arms 7 and move through openings in the floors 55 from floor to floor.
  • FIG. 6 shows the traveling bed dryer 3 as an inclined rotating drum, in which the coal and balls are fed by means of a screw conveyor 56 and mixed with one another in the process.
  • the discharge is also carried out via a screw conveyor 57, which feeds the material to the pneumatic separating device 10.
  • the vapors are withdrawn from the drum through line 58, which, as can be seen from the drawing, extends into the drum.
  • drivers 59 are also arranged, which are intended to keep the balls in motion.
  • an inclined container is provided as the traveling layer dryer 3, in which the feed and discharge, as in the device according to FIG. 6, is carried out by the screw conveyors 56 and 57 consequences.
  • the steel balls are alternately attracted by electromagnets 60 on the top and bottom of the container, which are offset with respect to one another, so that they take a sinusoidal path from the inlet to the outlet. This prevents the material from segregating and loosens the coal.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Coke Industry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)
EP82107206A 1981-08-25 1982-08-10 Chauffage de charbon Expired EP0073368B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT82107206T ATE24331T1 (de) 1981-08-25 1982-08-10 Erwaermung von kohle.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19813133491 DE3133491A1 (de) 1981-08-25 1981-08-25 Verfahren und einrichtung zur erwaermung von kohle
DE3133491 1981-08-25

Publications (3)

Publication Number Publication Date
EP0073368A2 true EP0073368A2 (fr) 1983-03-09
EP0073368A3 EP0073368A3 (en) 1984-04-11
EP0073368B1 EP0073368B1 (fr) 1986-12-17

Family

ID=6140020

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82107206A Expired EP0073368B1 (fr) 1981-08-25 1982-08-10 Chauffage de charbon

Country Status (11)

Country Link
EP (1) EP0073368B1 (fr)
JP (1) JPS5847093A (fr)
AR (1) AR228907A1 (fr)
AT (1) ATE24331T1 (fr)
AU (1) AU551656B2 (fr)
BR (1) BR8204941A (fr)
CA (1) CA1201408A (fr)
DE (2) DE3133491A1 (fr)
ES (1) ES8305404A1 (fr)
IN (1) IN158088B (fr)
ZA (1) ZA825368B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014000861A1 (fr) 2012-06-25 2014-01-03 Thyssenkrupp Uhde Gmbh Procédé et dispositif pour un préchauffage amélioré de charbon par échange de chaleur avec le gaz de refroidissement d'une installation de refroidissement à sec de coke

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB407665A (en) * 1932-06-17 1934-03-22 Pierre Eugene Henri Forsans Improvements in or relating to the treatment of coal and like materials
GB744742A (en) * 1950-05-11 1956-02-15 Weber Ludwig A process for the gasification of fine-grained and like fuels
GB1023491A (en) * 1962-02-02 1966-03-23 Oil Shale Corp Method for pyrolyzing solid carbonaceous materials
US4247987A (en) * 1979-09-26 1981-02-03 Exxon Research & Engineering Co. Continuous countercurrent fluid-solids contacting process stabilized by a magnetic field

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4894050A (fr) * 1972-03-14 1973-12-04
JPS5084959A (fr) * 1973-11-29 1975-07-09
JPS5327162A (en) * 1976-08-25 1978-03-14 Yamato Sanko Seisakushiyo Kk Drying apparatus utilizing heated ball medium

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB407665A (en) * 1932-06-17 1934-03-22 Pierre Eugene Henri Forsans Improvements in or relating to the treatment of coal and like materials
GB744742A (en) * 1950-05-11 1956-02-15 Weber Ludwig A process for the gasification of fine-grained and like fuels
GB1023491A (en) * 1962-02-02 1966-03-23 Oil Shale Corp Method for pyrolyzing solid carbonaceous materials
US4247987A (en) * 1979-09-26 1981-02-03 Exxon Research & Engineering Co. Continuous countercurrent fluid-solids contacting process stabilized by a magnetic field

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014000861A1 (fr) 2012-06-25 2014-01-03 Thyssenkrupp Uhde Gmbh Procédé et dispositif pour un préchauffage amélioré de charbon par échange de chaleur avec le gaz de refroidissement d'une installation de refroidissement à sec de coke
DE102012012417A1 (de) 2012-06-25 2014-04-24 Thyssenkrupp Uhde Gmbh Verfahren und Vorrichtung zur verbesserten Vorerhitzung von Kohle durch Wärmetausch mit dem Kühlglas einer Kokstrockenkühlanlage
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
ES514984A0 (es) 1983-05-01
AR228907A1 (es) 1983-04-29
EP0073368A3 (en) 1984-04-11
DE3133491A1 (de) 1983-03-17
CA1201408A (fr) 1986-03-04
ATE24331T1 (de) 1987-01-15
ES8305404A1 (es) 1983-05-01
ZA825368B (en) 1983-05-25
DE3274746D1 (en) 1987-01-29
AU551656B2 (en) 1986-05-08
EP0073368B1 (fr) 1986-12-17
BR8204941A (pt) 1983-08-02
AU8755582A (en) 1983-03-03
IN158088B (fr) 1986-08-30
JPS5847093A (ja) 1983-03-18

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