KR101733760B1 - Device and method for drying coal for coke oven - Google Patents

Device and method for drying coal for coke oven Download PDF

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Publication number
KR101733760B1
KR101733760B1 KR1020150152301A KR20150152301A KR101733760B1 KR 101733760 B1 KR101733760 B1 KR 101733760B1 KR 1020150152301 A KR1020150152301 A KR 1020150152301A KR 20150152301 A KR20150152301 A KR 20150152301A KR 101733760 B1 KR101733760 B1 KR 101733760B1
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South Korea
Prior art keywords
coal
dryer
cyclone
coke oven
waste gas
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KR1020150152301A
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Korean (ko)
Inventor
김경훈
장준상
황미나
장동민
강봉석
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주식회사 포스코
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Priority to KR1020150152301A priority Critical patent/KR101733760B1/en
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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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/14—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations
    • B04C5/185—Dust collectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/24—Multiple arrangement thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B1/00—Sieving, screening, sifting, or sorting solid materials using networks, gratings, grids, or the like
    • 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
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
    • C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/001—Heating arrangements using waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/001—Handling, e.g. loading or unloading arrangements

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Coke Industry (AREA)

Abstract

A coal drying apparatus for coke making according to an embodiment of the present invention includes: a waste gas supply unit for storing waste gas in a coke oven and supplying the waste gas to a dryer; A screening device for sorting coal by particle size and supplying coal with a particle size of 0.01 to 20 mm to the dryer; A dryer for supplying the coke oven waste gas from the waste gas supply unit and drying the coal; A cyclone connected to a downstream end of the dryer for collecting the fine particles discharged from the dryer; A dust collector connected to a downstream end of the cyclone and collecting the fine particles discharged from the cyclone; And a molding equipment for molding the collected fractions from the cyclone and the dust collector, wherein the waste gas supply part is connected to the cyclone to supply the coke oven waste gas to the cyclone front end.

Description

TECHNICAL FIELD [0001] The present invention relates to a coal drying apparatus and a drying method for a coke coal,

To a technique for drying coal charged into a coke oven for coke making. More particularly, to a coke drying apparatus and a drying method for coke using the coke oven waste gas so as to be used as a drying source of coal.

Demand for coal for iron ore and metallurgical coke production is increasing due to the rapid increase in global crude steel production. Therefore, it is increasingly difficult for coal prices to surge and concerns over the exhaustion of high quality coking coal. Under these circumstances, various technologies have been developed and developed to diversify the coal used for the production of coke for metallurgy and to increase the ratio of use of coal with weak point resistance (hereinafter referred to as "coking coal").

As a pretreatment technique for coal, a drying technique for reducing moisture of coal charged in a coke oven is mainly utilized. A fluidized bed dryer having excellent drying efficiency is mainly used for moisture drying of coal.

Inside the fluidized bed dryer, the coal is fluidized and dried by hot air. The dried coarse coal is discharged through the bottom of the fluidized bed dryer. The pulverized coal generated in the process of drying the coal is collected by the dust collector by the supplied hot air flow rate. The pulverized coal collected in a dust collecting facility such as a cyclone is mixed with water or a binder to form a predetermined form. The formed pulverized coal is mixed with dried coal in a fluid bed drier and then fed into a coke oven to produce coke.

However, in the conventional drying process for drying the coke coal, there is a problem that clogging of the lower end portion occurs due to clogging of fine particles at the lower end of the cyclone due to moisture remaining in the fine powder in the cyclone collecting the fine powder.

The present invention provides a coke drying apparatus and a drying method that can reduce energy and minimize environmental pollution by using waste gas generated from a coke oven as a heat source of a fluidized bed dryer.

The present invention also provides a coke drying apparatus and drying method capable of treating dust in waste gas generated in a coke oven and minimizing environmental pollution caused by dust.

The present invention also provides a coke drying apparatus and a drying method in which the clogging phenomenon at the lower end of the cyclone is solved.

A coal drying apparatus for coke making according to an embodiment of the present invention includes: a waste gas supply unit for storing waste gas in a coke oven and supplying the waste gas to a dryer; A screening device for sorting coal by particle size and supplying coal with a particle size of 0.01 to 20 mm to the dryer; A dryer for supplying the coke oven waste gas from the waste gas supply unit and drying the coal; A cyclone connected to a downstream end of the dryer for collecting the fine particles discharged from the dryer; A dust collector connected to a downstream end of the cyclone and collecting the fine particles discharged from the cyclone; And a molding equipment for molding the collected fractions from the cyclone and the dust collector, wherein the waste gas supply part is connected to the cyclone to supply the coke oven waste gas to the cyclone front end.

The screening apparatus can supply coal with a grain size of 0.1 to 10 mm to the dryer.

The dryer may include a fluidized-bed dryer that fluidizes and dries the coal by the coke oven off-gas that is ejected through a dispersing plate installed therein.

At least two fluid bed driers are provided and sequentially connected, so that the coal can be dried through each fluid bed dryer sequentially.

At least two cyclones are connected to the downstream end of each of the two or more fluidized bed dryers and the waste gas supply unit is connected to each cyclone to supply coke oven waste gas to the front end of each cyclone.

According to an embodiment of the present invention, there is provided a method of drying coal for coking, comprising: supplying coke oven waste gas to a dryer; Supplying coal having a particle size of 0.01 to 20 mm to a dryer by classifying coal by particle size; Drying the coal through a dryer; Collecting the fine particles generated during drying with a cyclone and a dust collector; And shaping the collected fine powder, and supplying a coke oven waste gas to the front end of the cyclone.

In the step of supplying the coal to the dryer, coal having a particle size of 0.1 to 10 mm may be supplied to the dryer.

The dryer may include a fluidized-bed dryer that fluidizes and dries the coal by the coke oven off-gas that is ejected through a dispersing plate installed therein.

At least two fluid bed driers are provided and sequentially connected, so that the coal can be dried through each fluid bed dryer sequentially.

At least two cyclones are provided and connected to the rear end of each of the fluidized bed driers provided with two or more cyclones, and the coke oven used gas can be supplied to the front end of each cyclone.

The coal can be lignite, sub-bituminous coal, or a mixture thereof.

The moisture content of the coal entering the dryer is 7 to 15 wt% and the moisture content of the dried coal can be 1 to 7 wt%.

The particle size of the fine particles collected in the cyclone and the dust collector may be 0.2 mm or less.

The temperature of the coke oven waste gas supplied to the dryer may be 120 to 300 캜.

The dried coal and the shaped powder may be used as a raw material for the coke oven.

According to one embodiment of the present invention, the waste gas generated in the coke oven can be recycled in drying the coal, and the coal can be efficiently and economically dried using the two-stage flow path, and the fine powder can be separated and utilized.

According to an embodiment of the present invention, the dryer is formed in two stages, and the drying is mainly performed in the first fluidized bed dryer, the dried coal to some extent is supplied to the second fluidized bed dryer, .

In addition, according to an embodiment of the present invention, the separated fine particles are separated from the cyclone, and the fine powder is used as a raw material for the coke oven such as dried coal after being mixed with a binder.

In addition, according to an embodiment of the present invention, the problem of generation of condensed water due to cyclone temperature drop by blowing a coke oven waste gas into the front end of the cyclone is eliminated, thereby eliminating the possibility of clogging due to fine particles at the lower end of the cyclone.

Further, according to an embodiment of the present invention, by supplying the coal with a particle size of an appropriate size by the screening device to the dryer, the generated derivative can be appropriately controlled.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic drawing of a coal drying apparatus for coking coal according to an embodiment of the present invention; FIG.
FIG. 2 is a schematic view showing a process in which a fine powder is generated during drying of coal.

The terms first, second and third, etc. are used to describe various portions, components, regions, layers and / or sections, but are not limited thereto. These terms are only used to distinguish any moiety, element, region, layer or section from another moiety, moiety, region, layer or section. Thus, a first portion, component, region, layer or section described below may be referred to as a second portion, component, region, layer or section without departing from the scope of the present invention.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the invention. The singular forms as used herein include plural forms as long as the phrases do not expressly express the opposite meaning thereto. Means that a particular feature, region, integer, step, operation, element and / or component is specified and that the presence or absence of other features, regions, integers, steps, operations, elements, and / It does not exclude addition.

Unless otherwise defined, all terms including technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Commonly used predefined terms are further interpreted as having a meaning consistent with the relevant technical literature and the present disclosure, and are not to be construed as ideal or very formal meanings unless defined otherwise.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

1 schematically shows a coal drying apparatus 100 for coke making according to an embodiment of the present invention. The coal drying apparatus for producing coke in Fig. 1 is merely for illustrating the present invention, and the present invention is not limited thereto. Accordingly, the coal drying apparatus for coke making can be variously modified.

As shown in FIG. 1, a coal drying apparatus 100 for coke making includes a waste gas supply unit 10 for storing a coke oven waste gas and supplying the coke oven waste gas to the dryer 20; A screening device 22 for sorting coal by particle size and supplying coal with a particle size of 0.01 to 20 mm to the dryer; A dryer (20) for receiving the coke oven waste gas from the waste gas supply unit (10) and drying the coal; A cyclone 30 connected to a downstream end of the dryer 20 and collecting the fine particles discharged from the dryer 20; A dust collector (40) connected to a downstream end of the cyclone (30) and collecting the fine particles discharged from the cyclone (30); And a molding apparatus 50 for molding the fine particles collected from the cyclone 30 and the dust collector 40. The waste gas supplying unit 10 is connected to the cyclone 30 to supply a coke oven waste gas .

According to an embodiment of the present invention, the coal is sorted by particle size through the screening device 22, and only the coal having a particle size of 0.01 to 20 mm is supplied to the dryer to reduce the generation of fine powder. This will be described with reference to FIG. As shown schematically in FIG. 2, on the surface of the coal 1, the fine powder 3 is attached together with the water 2. When the coal 1 is dried, the fine powder 3 attached to the water 2 is separated from the coal 1 as the water 2 disappears. When such a fine powder is generated in large quantities, it becomes a factor to lower the efficiency of the coal drying apparatus 100. In one embodiment of the present invention, only the coal having a particle size of 0.01 to 20 mm is supplied to the dryer through the screening device 22, thereby preventing a large amount of fine particles from being generated. More specifically, coal having a particle size of 0.1 to 10 mm can be supplied to the dryer through the screening device 22.

Also, in the embodiment of the present invention, the problem of generation of condensed water due to the temperature drop of the cyclone 30 is blown by blowing off the coke oven waste gas to the front end of the cyclone 30, thereby eliminating the possibility of clogging due to the fine particles at the lower end of the cyclone 30 have.

The waste gas supply unit 10 stores the coke oven waste gas discharged from the combustion chamber of the coke oven and supplies the coke oven waste gas to the drier 20. At this time, the temperature of the coke oven offgas is 120 to 300 캜, and it contains a little dust and is sufficiently usable as a hot air source of the dryer (20).

The dryer 20 receives the coke oven waste gas from the waste gas supply unit 10 and dries the coal. At this time, coal may be coal such as lignite, sub-bituminous coal, or a mixture thereof. The water content of the coal introduced into the dryer 20 is 7 to 15 wt%, and the moisture content of the coal dried through the dryer 20 may be 1 to 7 wt%.

In an embodiment of the present invention, the dryer 20 may include a fluidized-bed dryer that fluidizes and dries coal by a coke oven waste gas that is ejected through a dispersing plate installed therein. Of course, the dryer 20 is not limited to the fluidized bed dryer, but may be applied to both the drying structure for drying the coal.

The fluidized bed dryer is arranged in a vertical form and a dispersing plate for spraying the coke oven waste gas upward is installed inside.

The side of the fluidized bed dryer is provided with a charging port for charging coal and a discharging port for discharging coal dried in the fluidized bed. A cyclone 30 is connected to the upper portion of the fluidized bed dryer to collect the fine powder generated in the coal drying process. In the fluidized bed dryer, a heat insulating material is installed on the outer surface to prevent heat loss, and a thermocouple pressure sensor may be provided to detect temperature and pressure in the fluidized bed.

In the drying apparatus according to an embodiment of the present invention, two fluidized bed dryers are provided, and two fluidized bed dryers may be connected in a multi-stage structure. For convenience of explanation, the front fluidized bed dryer is referred to as a first fluidized bed dryer, and the rear fluidized bed dryer connected to the first fluidized bed dryer is referred to as a second fluidized bed dryer in accordance with the coal moving order.

In an embodiment of the present invention, the first fluidized bed dryer and the second fluidized bed dryer are sequentially disposed, and a connection pipe for moving coal is installed between the outlet of the first fluidized bed dryer and the inlet of the second fluidized bed dryer.

The second fluidized bed dryer has the same structure as that of the first fluidized bed dryer. The second fluidized bed dryer dries the coal by fluidizing the coal to the coke oven waste gas supplied from the waste gas supplying unit 10.

For example, the coal supplied to the coal feeder 21 is fed through a screw feeder at the lower end of the hopper, and the coal supplied to the coal feeder 21 through the screening device 22, And is supplied to the inside of the fluidized bed dryer. In an embodiment of the present invention, the second fluidized bed dryer receives flow-dried coal from the first fluidized-bed dryer through the connecting pipe, so that a separate coal feeder is unnecessary.

A cyclone 30 is connected to a downstream end of the dryer 20 and the cyclone 30 collects fine particles scattered during the drying process of the coal in the dryer 20. The cyclone 30 is connected to the waste gas supply unit 10 to supply the coke oven used gas to the front end of the cyclone 30. [ By supplying the coke oven waste gas to the front end of the cyclone 30 as described above, the clogging of the lower end, which is caused by the condensation of the fine particles at the bottom of the cyclone due to the moisture remaining in the fine particles, is solved. According to an embodiment of the present invention, when two or more fluid bed driers are provided, the cyclone 30 may be provided in correspondence with two or more thereof. At this time, the waste gas supply unit 10 is connected to the front end of each cyclone 30 to supply the coke oven waste gas.

 The fine particles not collected in the cyclone 30 are collected in the dust collector 40 connected to the end of the cyclone. The particle size of the fine particles collected in the cyclone 30 and the dust collector 40 may be 0.2 mm or less. The fine particles collected in the cyclone 30 and the dust collector 40 are molded through the molding equipment 50. At this time, the molding facility 50 is a facility for molding the fine powder to produce the molded coal. For example, the molding equipment 50 may include a mixer for mixing the collected fine powder and the binder to produce blended carbon, and a molding machine for producing the blended carbon by applying pressure to the blended carbon.

Hereinafter, the operation of the apparatus will be described.

The waste gas supply unit 10 stores the coke oven waste gas discharged from the combustion chamber of the coke oven and supplies the coke oven used gas to the drier. At this time, the temperature of the coke oven offgas is 120 to 300 캜, and it includes a little dust, so that it is sufficiently usable as a hot air source of the fluidized bed dryer.

The coke oven off-gas introduced into the first fluidized bed dryer passes through the dispersion plate and is sprayed upward. The fluidized bed is formed on the dispersion plate by the upward flow generated by the coke oven offgas blown upward through the dispersion plate. As the coal flows in this fluidized bed, the coke oven is dried by the waste gas. The coal supplied from the coal supply unit 21 to the first fluidized bed dryer through the screening device 22 is firstly fluidized by the coke oven waste gas in the first fluidized bed dryer and then dried. The coal scattered upward in the fluidized bed of the coal dried in the fluidized bed of the first fluidized bed dryer is introduced into the second fluidized bed dryer through the connecting pipe connected to the outlet of the first fluidized bed dryer.

In the second fluidized bed dryer, since the dried coal to some extent is supplied to the first fluidized bed dryer, the drying and classification of the coal is more effectively achieved.

The fine particles generated in the fluidized bed dryer are classified and collected through the cyclone 30 connected to the downstream end of the dryer. The minute fine particles not collected in the cyclone 30 are collected through the dust collector 40 connected to the rear end of the cyclone 30. The fine particles collected by the cyclone 30 and the dust collector 40 are bulked through a separate molding facility 50 and charged into the coke oven together with the coal dried through the dryer 20. [

As described above, the coal according to the embodiment of the present invention can be used to dry the coal using the waste gas of the coke oven as the hot air of the dryer. The coal dried through the dryer is stored in the coal storage tank 23, Can be used as a raw material for the coke oven.

The method of drying coal for coking according to an embodiment of the present invention includes the steps of supplying a coke oven waste gas to a dryer 20; Supplying coal having a particle size of 0.01 to 20 mm to the dryer 20 by classifying coal by particle size; Drying the coal through a dryer (20); Collecting the fine particles generated in drying by the cyclone 30 and the dust collector 40; And shaping the collected fine powder, and supplying coke oven waste gas to the front end of the cyclone 30. [

Hereinafter, a method of drying coal for coke production according to an embodiment of the present invention will be described in each step.

First, the coke oven used gas is supplied to the dryer (20). At this time, the temperature of the coke oven offgas is 120 to 300 캜, and it contains a little dust, so that it is sufficiently usable as a hot air source of the dryer.

Next, the coal is classified into the grain sizes, and coal having a grain size of 0.01 to 20 mm is supplied to the dryer 20. Only the coal having a grain size of 0.01 to 20 mm can be supplied to the dryer 20 to reduce the generation of fine powder. On the surface of the coal there is a fine powder with moisture. When these coals are dried, the moisture that has adhered with moisture is separated from the coal as moisture is removed. When such a fine powder is generated in large quantities, it becomes a factor to lower the efficiency of the coal drying apparatus 100. In one embodiment of the present invention, only coal having a particle size of 0.01 to 20 mm is sorted and supplied to a dryer, whereby a large amount of fine powder can be prevented from being generated. More specifically, coal having a grain size of 0.1 to 10 mm may be classified and supplied to a dryer.

Next, the coal is dried through the dryer (20). At this time, coal may be coal such as lignite, sub-bituminous coal, or a mixture thereof. The water content of the coal introduced into the dryer 20 is 7 to 15 wt%, and the moisture content of the coal dried through the dryer 20 may be 1 to 7 wt%.

In an embodiment of the present invention, the dryer 20 may include a fluidized-bed dryer that fluidizes and dries coal by a coke oven waste gas that is ejected through a dispersing plate installed therein. Of course, the dryer 20 is not limited to the fluidized bed dryer, but may be applied to both the drying structure for drying the coal. In particular, at least two fluidized-bed dryers are provided and sequentially connected, so that coal can be dried through each fluidized bed dryer in turn.

Next, the fine particles generated during drying are collected by the cyclone 30 and the dust collector 40. A cyclone 30 is connected to a downstream end of the dryer 20 and the cyclone 30 collects fine particles scattered during the drying process of the coal in the dryer 20. The cyclone 30 is connected to the waste gas supply unit 10 to supply the coke oven used gas to the front end of the cyclone 30. [ By supplying the coke oven waste gas to the front end of the cyclone 30 as described above, the clogging of the lower end, which is caused by the condensation of the fine particles at the bottom of the cyclone due to the moisture remaining in the fine particles, is solved. According to an embodiment of the present invention, when two or more fluid bed driers are provided, the cyclone 30 may be provided in correspondence with two or more thereof. At this time, the waste gas supply unit 10 is connected to the front end of each cyclone 30 to supply the coke oven waste gas. The fine particles not collected by the cyclone 30 are collected by the dust collector 40 connected to the rear end of the cyclone. The particle size of the fine particles collected in the cyclone 30 and the dust collector 40 may be 0.2 mm or less.

Next, the collected derivatives are formed. The step of molding the fine powder may include a step of mixing the fine powder and the binder to produce a blended carbon, and a step of molding the blended carbon to produce the blast furnace.

As described above, the method according to one embodiment of the present invention enables the coal to be dried by using the coke oven waste gas as the hot air of the dryer, and the coal and the shaped powder dried through the dryer can be used as a raw material of the coke oven

It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the present invention as defined by the following claims. As will be understood by those skilled in the art. It is therefore to be understood that the above-described embodiments are illustrative in all aspects and not restrictive.

1. Coal
2. Moisture
3. Differential
10. Waste gas supplier
20. Dryer
21. Coal Supply Department
22. Screening device
23. Coal Storage
30. Cyclone
40. Dust collector
50. Forming equipment
100. Coal dryer

Claims (15)

A waste gas supply part for storing the coke oven waste gas and supplying it to the drier;
A screening device for sorting coal by particle size and supplying coal with a particle size of 0.01 to 20 mm to the dryer;
A dryer for receiving the coke oven offgas from the waste gas supply unit and drying the coal;
A cyclone connected to a downstream end of the dryer for collecting the fine particles discharged from the dryer;
A dust collector connected to a downstream end of the cyclone and collecting the fine particles discharged from the downstream end of the cyclone; And
A molding equipment for molding the fine powder collected from the cyclone and the dust collector;
Lt; / RTI >
Wherein the waste gas supply unit is connected to the cyclone to supply the coke oven used gas to the front end of the cyclone. The method according to claim 1,
Wherein the screening apparatus supplies coal having a particle size of 0.1 to 10 mm to a dryer. The method according to claim 1,
Wherein the dryer includes a fluidized bed dryer for fluidizing and drying coal by a coke oven waste gas blown out through a dispersing plate installed in the coke oven. The method of claim 3,
Wherein at least two of said fluidized bed dryers are provided and sequentially connected to each other so that coal is sequentially passed through each fluidized bed dryer to be dried. 5. The method of claim 4,
At least two cyclones are connected to a rear end of each of the fluid bed driers provided with two or more cyclones,
The waste gas supply unit is connected to each cyclone to supply the coke oven used gas to the front end of each cyclone, Supplying coke oven waste gas to the dryer;
Supplying coal having a particle size of 0.01 to 20 mm to the dryer by sorting coal by particle size;
Drying the coal through the dryer;
Collecting the fine particles generated during drying with a cyclone and a dust collector; And
And molding the collected derivative,
And supplying the coke oven used gas to the front end of the cyclone. The method according to claim 6,
A method for drying coking coal, comprising the steps of supplying coal to a dryer at a stage of supplying coal with a size of 0.1 to 10 mm. 8. The method of claim 7,
Wherein the dryer comprises a fluidized bed dryer for fluidizing and drying coal by a coke oven waste gas blown out through a dispersing plate installed in the inside thereof. 9. The method of claim 8,
Wherein at least two fluidized bed dryers are provided and sequentially connected to each other so that coal is sequentially dried through each fluidized bed dryer to dry the coal for coke production. 10. The method of claim 9,
Wherein the at least two cyclones are connected to a rear end of each of the at least two fluidized bed dryers, and the coke oven used gas is supplied to the front end of each cyclone. The method according to claim 6,
Wherein the coal is coal tar, sub-coal, or a mixture thereof. The method according to claim 6,
Wherein the moisture content of the coal introduced into the dryer is 7 to 15 wt% and the moisture content of the dried coal is 1 to 7 wt%. The method according to claim 6,
Wherein the fine particles collected in the cyclone and the dust collector have a particle size of 0.2 mm or less. The method according to claim 6,
Wherein the temperature of the coke oven off-gas supplied to the dryer is 120 to 300 ° C. The method according to claim 6,
Wherein the dried coal and the shaped powder are used as a raw material for a coke oven.

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Citations (1)

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Publication number Priority date Publication date Assignee Title
KR101198895B1 (en) * 2010-12-28 2012-11-07 주식회사 포스코 Device and method for drying coal for coke oven

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101198895B1 (en) * 2010-12-28 2012-11-07 주식회사 포스코 Device and method for drying coal for coke oven

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