KR20180047688A - Apparatus for recovering waste heat and coke oven system having the same - Google Patents

Apparatus for recovering waste heat and coke oven system having the same Download PDF

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Publication number
KR20180047688A
KR20180047688A KR1020160144297A KR20160144297A KR20180047688A KR 20180047688 A KR20180047688 A KR 20180047688A KR 1020160144297 A KR1020160144297 A KR 1020160144297A KR 20160144297 A KR20160144297 A KR 20160144297A KR 20180047688 A KR20180047688 A KR 20180047688A
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South Korea
Prior art keywords
heat
heat exchange
exchange medium
coke oven
gas
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KR1020160144297A
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Korean (ko)
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KR101870710B1 (en
Inventor
박경태
김병일
이승재
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주식회사 포스코
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Priority to KR1020160144297A priority Critical patent/KR101870710B1/en
Publication of KR20180047688A publication Critical patent/KR20180047688A/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
    • C10B41/00—Safety devices, e.g. signalling or controlling devices for use in the discharge of coke
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B43/00—Preventing or removing incrustations
    • C10B43/02—Removing incrustations
    • 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
    • C10B45/00—Other details
    • 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
    • C10B5/00—Coke ovens with horizontal chambers
    • C10B5/10—Coke ovens with horizontal chambers with heat-exchange devices
    • C10B5/20—Coke ovens with horizontal chambers with heat-exchange devices with recuperators
    • 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Abstract

The present invention relates to a waste heat recovery device and a coke oven facility including the same and, more specifically, to a waste heat recovery device and a coke oven facility including the same, wherein the waste heat recovery device is capable of preventing excessive heat exchange during waste heat recovery of a gas passing through a rising pipe in a facility including a plurality of rising pipes. According to an embodiment of the present invention, the waste heat recovery device, which is installed at least partially in a facility including a plurality of rising pipes, comprises: a plurality of heat exchange units which have a path formed therein to allow a heat exchange medium capable of exchanging heat with a gas flowing in the rising pipes to pass therethrough, and are installed in the rising pipes, respectively; and a connection member which has an internal path through which the heat exchange medium can pass to form a movement line of the heat exchange medium and the heat exchange units, and connects the heat exchange units.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a coke oven,

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a heat recovery apparatus and a coke oven facility including the same, and more particularly, to a heat recovery apparatus capable of preventing excessive heat exchange at the time of recovery of gas passing through a riser, Device and a coke oven installation comprising the same.

Coal is the most important energy source of the steel industry and is mainly used in blast furnaces. In the early days, it was used as coal itself. However, since it is not efficient, coal is made into coke in almost all steel mills and put into blast furnace. In order to produce coke, coal for coke should be added to the coke oven. Coal imported from various countries has a different composition, so the composition is adjusted in the Blending Bin prior to injection into the coke oven. The coke oven consists of a number of independent combustion chambers and carbonization chambers, which supply energy to the carbonization chamber by combustion of the coke oven gas (COG) in the combustion chamber, and carbonification of the coal occurs in the carbonization chamber. When carbonization is carried out in the carbonization chamber, the volatile components contained in the coal escape through the rising pipe into the coke oven in the form of gas. It is called coke oven gas (COG) and is an important energy source for steelworks. Meanwhile, the crude coke oven gas (COG), which has not been refined yet, can be named as a crude coke oven gas (Crude COG), while the one-coke oven gas (Crude COG) (Coke oven gas) (COG) used in the steelworks.

The gas generated from the coke oven (Crude COG) is cooled by the ordination through the riser. In this process, the crude coke oven gas (Crude COG) at 600 to 800 ° C falls to 80 to 100 ° C, and Tar contained in the gas is removed. As a result of high temperature coke oven gas (COG) cooling, the Ordnance Temperature rises and at the same time the overall Ordnance Temperature circulating in the conversion process rises and the purification efficiency of coke oven gas (COG) declines. Therefore, efforts are needed to reduce the ordination temperature and simultaneously recover the heat.

To this end, attempts have been made to recover energy by installing a heat exchanger in a riser, but additional heat source supply and tar condensation have occurred due to excessive heat exchange. Further, the heat exchanger is arranged in a narrow space, which makes it difficult to maintain, and oven deformation occurs due to an increase in equipment load, thereby causing problems such as adhered substances to the heat exchanger.

Korean Patent Registration No. 10-0101833

The present invention provides a superheating and recovering device and a coke oven facility including the elevating and recovering device capable of obtaining high thermal energy while preventing excessive heat exchange at the time of recovering heat from the gas passing through the riser pipe.

The heat recovery / recovery device according to an embodiment of the present invention is a heat recovery / recovery device in which at least a part is installed in a facility including a plurality of uprising pipes, wherein a heat exchange medium capable of heat exchange with gas flowing in the uprising pipe A plurality of heat exchanging units each having a path formed therein and installed in the plurality of uprising pipes; And a connection member having an internal path through which the heat exchange medium can pass so as to form the moving lines of the plurality of heat exchange units and the heat exchange medium, and connecting the plurality of heat exchange units.

The heat exchanging part may be formed at least partially in a non-linear shape.

The heat exchanger may be located in a central region inside the riser pipe.

The heat exchanger may have a plurality of bent portions or bent portions.

The path length of the heat exchange unit located at one side of the movement line may be different from the path length of the heat exchange unit located at the other side of the movement line.

And a heat utilizing engine connected to a moving line of the heat exchange medium so as to utilize thermal energy transmitted from the heat exchange medium which has passed through the moving line of the heat exchange medium.

The heat utilization engine may be connected to both sides of the movement line of the heat exchange medium.

And a protection member disposed around the heat exchange unit to protect the heat exchange unit.

The protective member may include a chain sling on which the adhesive material is removed by shaking.

The heat exchange medium may include water, and the water may be converted into steam through a movement line of the heat exchange medium.

A coke oven facility according to another embodiment of the present invention comprises a coke oven for producing coke; And a superheating and recovering device installed in the carbonization chamber of the coke oven.

The plurality of heat exchanging units may be connected to the plurality of heat exchanging units and the plurality of heat exchanging units may be connected to the moving lines of the heat exchanging medium by connecting the plurality of heat exchanging units with the connecting members. Thus, since the heat exchange medium is passed through the plurality of risers, the heat exchange medium can be used to obtain high thermal energy even when excessive heat is not exchanged in each riser pipe during the recovery of the gas passing through the riser.

In addition, since only a moving line of the heat exchanging medium including a plurality of heat exchanging units and connecting members is installed in a facility including a plurality of uprising pipes, the load applied to the equipment can be minimized by the hot- In addition, the apparatus for recovering and recovering heat of the present invention can simplify the structure of the apparatus by a plurality of heat exchanging units and connecting members, thereby solving the difficulty of maintenance.

On the other hand, when at least a part of the heat exchanging part is non-linear, the heat exchanging time of the heat exchanging medium can be increased, so that the effective heat exchanging medium can be recovered through the heat exchanging medium. When water is used as a heat exchange medium, the water is converted into steam through a plurality of uprising pipes, so that the heat of the gas passing through the uprising pipe can be recovered and high temperature and high pressure steam can be obtained. Further, it is possible to prevent or suppress the contamination of the surface of the heat exchanging part due to the adhered material through the protective member, and thus the gas flowing in the inside of the uprising pipe can directly contact the surface of the heat exchanging part, Heat exchange of the heat exchange medium can be effectively performed.

FIG. 1 illustrates a facility including a plurality of risers according to an embodiment of the present invention. FIG.
FIG. 2 is a schematic view of a superheating and recovering apparatus according to an embodiment of the present invention; FIG.
3 is a view showing a modification of the heat exchanger according to the embodiment of the present invention.
4 is a schematic view showing a modified example of the heat recovery apparatus according to an embodiment of the present invention;
5 is a view illustrating a protective member according to an embodiment of the present invention.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. It will be apparent to those skilled in the art that the present invention may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, It is provided to let you know. In the description, the same components are denoted by the same reference numerals, and the drawings are partially exaggerated in size to accurately describe the embodiments of the present invention, and the same reference numerals denote the same elements in the drawings.

FIG. 1 is a view showing a facility including a plurality of uprising pipes according to an embodiment of the present invention, and FIG. 2 is a schematic view showing a boiler and a recovery apparatus according to an embodiment of the present invention.

1 and 2, a superheating and recovering apparatus 100 according to an embodiment of the present invention includes a superheating and recovering apparatus 100 having at least a part installed in a facility 200 including a plurality of ascending pipes 211, A plurality of heat exchange units 110 formed in the riser pipe 211 so as to pass therethrough a heat exchange medium capable of heat exchange with the gas flowing in the riser pipe 211; And a connection member (120) having an internal path through which the heat exchange medium can pass so as to form the plurality of heat exchange units (110) and the movement line (50) of the heat exchange medium, and connecting the plurality of heat exchange units .

The apparatus 200 may include a plurality of uprising pipes 211, and a high-temperature process may be performed. In this process, a high temperature gas can be generated, and the gas can pass through the uprising pipe 211. For example, the facility 200 can be a coke oven 200 that carries coal away. Hereinafter, the coke oven 200 will be described as an example.

The plurality of heat exchanging units 110 may be installed in each of the plurality of uprising pipes 211 and a path may be formed so that a heat exchange medium capable of heat exchange with the gas flowing in the uprising pipe 211 passes. Here, the gas flowing in the uprising pipe 211 may be a coke oven gas (COG), and more specifically, a crude coke oven gas (Crude COG) which is not purified. The plurality of heat exchanging units 110 may be installed in the uprising pipe 211 to recover the heat of the gas through the heat exchange medium and lower the temperature of the gas.

For example, the plurality of heat exchanging units 110 may be pipes passing through the plurality of uprising pipes 211. When the heat exchanging medium passes through the plurality of heat exchanging units 110, And heat exchange with the gas flowing through the inside of the pipe 211 can be recovered. The heat exchanging part 110 may be structured to enter the inside of the uprising pipe 211 from one side of the uprising pipe lid 211a and come out from the opposite side of the uprising pipe lid 211a, It may be a structure that enters the inside of the pipe 211 and goes out through the side wall of the opposite riser pipe 211.

The heat exchanging unit 110 may be installed along the inner wall of the uprising pipe 211 or may be installed so that the path inside the heat exchanging unit 110 passes through the center of the inner space of the uprising pipe 211. In this case, when the gas is installed along the inner wall of the uprising pipe 211, a hollow region through which the gas can pass may be formed, and it may be installed in contact with the inner wall of the uprising pipe 211 And may be installed apart from the inner wall of the uprising pipe 211. The pipe line may be inserted into the riser pipe 211 through one of the side walls of the riser pipe 211 and may be connected to the other pipe The piping lines may be installed outside the uprising pipe 211 without interfering with each other.

The connecting member 120 may have a plurality of heat exchanging units 110 and may have an internal path through which the heat exchanging medium can pass to form a moving line 50 of the heat exchanging medium together with the plurality of heat exchanging units 110. The connection member 120 may connect the plurality of heat exchange units 110 to move the heat exchange medium from one heat exchange unit 110 to the other heat exchange unit 110.

For example, the connecting member 120 may be a pipe that communicates with the plurality of heat exchanging units 110, and the heat exchanging medium may pass through the inner path to pass through one heat exchanging unit 110 to another heat exchanging unit 110, . ≪ / RTI >

The connecting member 120 may be located outside the uprising pipe 211 and may be exposed to the outside in order to connect the plurality of heat exchanging units 110. The connecting member 120 may be exposed to the outside, The member 120 may be subjected to a heat insulating treatment or a heat insulating treatment. In the method of the heat preservation treatment or the heat insulation treatment, the connection member 120 may be wrapped with a heat insulating material and subjected to a thermal insulation treatment or adiabatic treatment.

The plurality of heat exchanging units 110 and the connecting members 120 may constitute a moving line 50 of the heat exchanging medium. Here, the plurality of heat exchanging units 110 and the connecting member 120 may connect the plurality of heat exchanging units 110 through the connecting member 120 to form a single moving line 50 of the heat exchanging medium, At least two or more heat exchanging units 110 may be grouped and connected to each other through the connecting member 120 to form a plurality of the moving lines 50 of the heat exchanging medium.

Conventionally, the heat recovery / recovery device including the heat exchanger is provided in each of the plurality of uprising pipes 211. A plurality of heat recovery / recovery devices are installed on the upper part of the facility 200 including the plurality of uprising pipes 211, So that it was difficult to arrange the heating and recovering apparatus. In addition, the number of parts installed in the facility 200 among the hot-water collection devices increases, the load applied to the facility 200 increases due to the hot-water collection device, and the deformation of the facility 200 due to the large load applied to the facility 200 Lt; / RTI > Since each of the heat recovery and recovery devices in each riser 211 recovers the heat of the gas, the thermal energy that can be obtained through the recovery of the gas in one heat recovery and recovery device is not large. Therefore, there is a restriction in using the heat energy recovered from the heat of the gas, and the selection of the heat exchange medium has been limited in order to more effectively recover the heat of the gas. In case the facility 200 is the coke oven 200, in case of unreasonably recovering the heat of the gas in one riser 211 in order to increase the heat energy obtained by one heat recovery and recovery device, the coal 10 And Tar, which is to be removed separately, is condensed in the uprising pipe 211. In this case,

However, in the heat recovery apparatus 100 according to the present invention, a plurality of heat exchange units 110 are provided in a plurality of uprising pipes 211, and a plurality of heat exchange units 110 are connected to each other by a connection member 120, The heat exchanging unit 110 and the connecting member 120 may form the moving line 50 of the heat exchange medium. As a result, the heat exchange medium passes through the plurality of uprising pipes 211 and the heat exchange is performed for a long time. Therefore, when the gas passing through the uprising pipe 211 is recovered, excessive heat exchange is performed in each uprising pipe 211 (Or large) heat energy can be easily obtained by using the heat exchange medium even if the heat exchange medium is not used. Therefore, since the high heat energy can be obtained through the heat recovery apparatus 100, the use width of the heat energy recovered from the heat of the gas can be widened, and the selection width of the heat exchange medium can be widened.

The heat recovery apparatus 100 of the present invention includes a plurality of heat exchanging units 110 and a connecting member 120 disposed on a facility 200 including a plurality of uprising pipes 211, The load applied to the facility 200 can be minimized due to the heat recovery and recovery apparatus 100. [ In the present invention, not all of the heat recovery apparatus 100 is installed in a narrow space above the facility 200, but only a part of the heat recovery and recovery apparatus 100 is installed on the upper part of the facility 200 and a plurality of heat exchange units 110 And the connecting member 120, the arrangement of the apparatus is also simple and the difficulty of maintenance can be solved.

In the prior art, a method of collecting heat energy recovered through each of the heat recovery / recovery devices using an additional separate heat recovery medium was used because heat energy obtained through the heat recovery of the gas was not large in one heat recovery and recovery device. However, in the present invention, high heat energy can be obtained through the heat recovery apparatus 100, so that no additional heat recovery medium is required, and only one heat exchange medium can be used.

The heat exchange medium may be a liquid such as water that can easily recover the heat from the gas. The heat exchange medium may include water, and the water may be converted into steam through the movement line 50 of the heat exchange medium. The heat exchange medium may be supplied to one side of the movement line 50 of the heat exchange medium and recovered through the other side. When the heat exchange medium is water, liquid water is supplied to one side of the movement line (50) of the heat exchange medium and can exchange heat with the gas while passing through the movement line (50) of the heat exchange medium. It can be changed into a steam state through heat exchange. And the water in the steam state can be continuously recovered through the other of the transfer line 50 of the heat exchange medium through the transfer line 50 of the heat exchange medium.

In order to change the state of water to steam, latent heat is required. If the gas is separately recovered for each riser pipe 211 as in the prior art, water supplied to the heat exchanger can not obtain sufficient heat, It can not be changed into water of the state. When the facility 200 is the coke oven 200, if the gas is recovered and the water is changed into steam, the relatively large energy corresponding to the latent heat is lost in one carbon chamber 210 An additional heat source should be supplied for the coal 10 to flow and the tar to be removed separately due to excessive heat exchange can be condensed in the uprising pipe 211.

However, in the present invention, the water is passed through the plurality of heat exchanging units 110 and the connecting member 120 through the plurality of ascending pipes 211, (Or heat) corresponding to the heat (or heat) can be sufficiently recovered (or heat exchanged), so that steam can be easily obtained. Here, if the water passes through a plurality of (at least three or more) uprising pipes 211, high temperature and high pressure steam can be obtained. The high-temperature and high-pressure steam can be used variously in the conversion process of making a raw material (for example, coal) into a coke, and it is also easy to use it for power generation that generates electricity.

FIG. 3 is a view showing a modified example of the heat exchanger according to the embodiment of the present invention. FIG. 3 (a) shows a coil type heat exchanger and FIG. 3 (b) shows a multiphase horizontal rectangular wave heat exchanger.

Referring to FIG. 3, at least a part of the heat exchanging part 110 may be non-linearly formed. The non-linear shape may be a shape in which a line length between two points including a zigzag, a wave, a square wave, and a coil shape is made long. If at least a part of the heat exchanging part 110 is formed in a nonlinear shape, the path length of the heat exchanging part 110 installed in the uprising pipe 211 can be long and the heat exchanging medium can be stored in the uprising pipe 211 for a long time . Accordingly, the heat exchange time of the heat exchange medium can be increased, and the effective heat recovery can be performed through the heat exchange medium.

The heat exchanging part 110 may be formed in a coil shape. At this time, the heat exchanger 110 may be installed apart from the side wall of the uprising pipe 211. The coil type heat exchanging unit 110 can not only increase the path length of the heat exchanging unit 110 installed in the uprising pipe 211 but also allow the gas to pass through both the central hollow region and the outside region of the heat exchanging unit 110 And the area in contact with the gas flowing inside the uprising pipe 211 can be widened. Therefore, it is possible to more effectively recover the heat of the gas. Further, when the heat exchanging unit 110 is formed in a coil shape, the path length of the heat exchanging unit 110 can be easily adjusted.

And the heat exchange unit 110 may be located in a central region inside the uprising pipe 211. Since the amount of the gas flowing in the riser pipe 211 exceeds the outer area of the inside of the riser pipe 211 to the central area inside the riser pipe 211, The contact area with the gas can be widened, heat exchange with a large amount of the gas can be performed, and the heat generation of the gas can be effectively recovered.

Further, the heat exchanging unit 110 may have a plurality of bent portions or bent portions. That is, the heat exchanging unit 110 may have a bent portion or a bent portion, and the total number of bent portions or bent portions may be two or more. Here, the bent portion or the bent portion may be bent or bent in the vertical direction, or may be bent or bent in the horizontal direction. For example, as shown in FIG. 2, a plurality of bends may be formed in the vertical direction, and a plurality of bends may be formed in the horizontal direction as shown in FIG. 3 (b).

The heat exchange unit 110 may have a multi-stage structure. In the case where a plurality of bends are formed in the vertical direction, a multi-stage structure may be formed in the horizontal direction. In the case where a plurality of bends are formed in the horizontal direction, a multi-stage structure may be formed in the vertical direction. Direction and the direction in which the multistage structure is formed may be the same. The heat exchanging part 110 may include a plurality of bending parts and may have a multi-stage structure in both the horizontal direction and the vertical direction, and the direction in which the bending part is formed may be at least one of a horizontal direction and a vertical direction. For example, the heat exchanging unit 110 may be formed in a multi-stage horizontal rectangular wave shape in which horizontal rectangular waves having a plurality of bends in the horizontal direction are formed in multiple stages as shown in FIG. 3 (b). In this case, the path length of the heat exchange unit 110 installed in the uprising pipe 211 can be relatively long, the contact area with the gas can be increased, and heat exchange with a large amount of the gas can be achieved . Even in this case, heat exchange between the heat exchange medium and the gas can be performed for a sufficient time, and the heat generation of the gas can be sufficiently recovered.

When the heat exchanging part 110 is spaced from the inner wall of the uprising pipe 211 or the path of the heat exchanging part 110 passes the central part of the inner space of the uprising pipe 211, And the area of contact with the gas flowing inside the uprising pipe 211 can be widened. When the heat exchanging part 110 is formed along the inner wall of the uprising pipe 211, the path length of the heat exchanging part 110 installed in the uprising pipe 211 may be longer. In consideration of this, the shape of the heat exchanging part 110 can be appropriately selected.

The heat generating and recovering apparatus 100 of the present invention is characterized in that the path length of the heat exchanging unit 110 located at one side of the traveling line 50 and the path length of the heat exchanging unit 110 located at the other side of the traveling line 50 Can be different. One side of the movement line 50 may be closer to one side than the other side of the movement line 50 of the heat exchange medium and the other side of the movement line 50 may be located near the other side of the movement line 50 of the heat exchange medium. It may be closer to the other side than one side. On the other hand, when the heat exchange medium is water, the one side may be a place where liquid water passes, and the other side may be a place where water in a steam state passes. Even when the heat exchange medium is water, And the other side can be distinguished from each other. When the heat exchange medium is water, the water supplied to one side of the movement line 50 is in a liquid state and the water recovered to the other side of the movement line 50 is in a steam state. Therefore, The path length of the heat exchange unit 110 located at one side of the movement line 50 and the path length of the heat exchange unit 110 located at the other side of the movement line 50 may be different from each other . Since the latent heat is required to change the liquid state of the water in the steam state, the path length of the heat exchanging part 110 located at one side of the traveling line 50 is set to be shorter than the path length of the heat exchanging part 110 located at the other side of the traveling line 50 The water in the steam state is lower in thermal conductivity than the water in the liquid state and has a high specific heat so that the path of the heat exchange unit 110 located on the other side of the movement line 50 May be longer than the path length of the heat exchanging part (110) located at one side of the moving line (50). As described above, the latent heat, the heat conductivity, the specific heat or the heat exchange of the heat exchange medium may be determined in consideration of at least one of the latent heat of the heat exchange medium, the thermal conductivity, the specific heat, the thermal conductivity according to the state change of the heat exchange medium, The path lengths of the plurality of heat exchanging units 110 can be determined according to the thermal conductivity and / or the specific heat according to the state change of the medium.

The number of the heat exchanging units 110 may be controlled according to the heat recovery conditions such as the flow rate of the heat exchange medium and the number of the uprising pipes 211. In this case, The path length may be determined. The path lengths of the plurality of heat exchanging units 110 may vary depending on the type of the heat exchange medium.

4 is a schematic view showing a modified example of the heat recovery apparatus according to an embodiment of the present invention.

Referring to FIG. 4, the heating and recovering apparatus 100 according to the present invention is connected to the moving line 50 of the heat exchange medium so as to utilize the heat energy transmitted from the heat exchange medium passing through the moving line 50 of the heat exchange medium. And a heat utilization engine 130 which is connected to the heat exchanger.

The heat utilization engine 130 may be connected to at least one of the one side and the other side of the movement line 50 of the heat exchange medium and may be connected to the movement line 50 of the heat exchange medium, Heat (or heat) transferred from the heat exchange medium collected through the other side can be used. The heat utilization engine 130 may include a steam generator for generating electricity using high temperature and high pressure steam. Here, the steam generator 130 is exemplified as the heat utilization engine 130, but the present invention is not limited thereto, and any device that can utilize thermal energy is acceptable.

The heat recovery medium 100 of the present invention supplies the heat exchange medium from a heat exchange medium supply unit (not shown) to one side of a movement line 50 of the heat exchange medium, (Or recovering the heat of the gas) through the other side of the heat exchange medium 50. The heat exchange medium can be recovered and stored and / or used.

The heat utilization engine 130 may be connected to both sides of the movement line 50 of the heat exchange medium. The heat utilization engine 130 may be connected to one side and the other side of the movement line 50 of the heat exchange medium. The heat utilization engine 130 may be connected to the heat exchange orifice 130, The heat exchange medium which has received heat energy (or heat) from the medium and has been cooled down by the transfer of heat energy may be supplied to one side of the moving line 50 of the heat exchange medium again. Accordingly, a circulation line of the heat exchange medium can be formed to circulate the heat exchange medium.

FIG. 5 is a view showing a protection member according to an embodiment of the present invention, wherein FIG. 4 (a) shows a protection member provided in a rectangular wave heat exchanger, and FIG. 4 (b) .

5, the heat recovery apparatus 100 according to the present invention may further include a protection member 140 disposed around the heat exchange unit 110 to protect the heat exchange unit 110. Referring to FIG. The protection member 140 may be disposed around (or covering) the heat exchange unit 110 around the heat exchange unit 110 to physically protect the heat exchange unit 110. When the facility 200 is the coke oven 200, a large amount of viscous tar is contained in the one-coke oven gas (Crude COG) flowing in the uprising pipe 211. When there is no protective member 140, The viscous tar may cause piping damage to the heat exchange unit 110. [ However, in the present invention, piping damage to the heat exchange unit 110 due to a large amount of viscous tar can be prevented through the protection member 140. [ The protective member 140 may prevent or prevent contamination of the surface of the heat exchange unit 110 by attaching adhering substances such as particles (e.g., particles of carbon, tar, etc.) to the surface of the heat exchange unit 110 can do. If the surface of the heat exchange unit 110 is contaminated with the adhering substance, the adhering substance interferes with the heat exchange between the gas flowing inside the uprising pipe 211 and the heat exchange medium, so that the gas can not be effectively discharged. However, in the present invention, the contamination on the surface of the heat exchanging part 110 is prevented or suppressed, so that the gas flowing inside the uprising pipe 211 can directly contact the surface of the heat exchanging part 110, Heat exchange between the gas flowing through the heat exchange medium and the heat exchange medium can be effectively performed, and the heat generation of the gas can be effectively recovered through the heat exchange medium.

The heat exchanging part 110 may be coated with the protection member 140 when the heat exchanging part 110 is formed in contact with the inner wall of the uprising pipe 211 along the inner wall of the uprising pipe 211. [ In this case, the protection member 140 may be formed of a material having high thermal conductivity and high thermal conductivity (e.g., refractory, metal, etc.). When the heat exchanging part 110 is formed adjacent to the inner wall of the uprising pipe 211 along the inner wall of the uprising pipe 211, the protective member 140 is provided only on the front side (or inner side) of the heat exchanging part 110, When the heat exchanging part 110 is provided to be spaced from the inner wall of the uprising pipe 211, the protection member 140 may be provided on both sides (e.g., inside and outside) of the heat exchanging part 110 Can be provided.

And the protective member 140 may include a chain sling 140 in which the adhesive material is removed by shaking. The chain sling 140 can be easily removed by shaking (or through swinging) the attachment material attached to the surface. Here, the chain sling 140 can be connected to the lifting tube cover 211a, so that when the lifting tube cover 211a is opened, the chain sling 140 is shaken to naturally drop the bonding material. The deposited adhered material may fall down or be entrained by the gas below the uprising pipe 211 (for example, coal in a carbonization chamber).

Meanwhile, when the protection member 140 is installed in contact with the heat exchange unit 110, the protection member 140 may be formed of a material having a high thermal conductivity (for example, metal) so that the heat transfer to the heat exchange unit 110 can be performed well. When the protection member 140 is installed so as to be spaced apart from the heat exchange unit 110, the protection member 140 may be formed of a material having a low thermal conductivity so as to prevent the heat (or heat) of the gas from being lost.

Hereinafter, the coke oven system according to another embodiment of the present invention will be described in detail with reference to FIGS. 1 to 5. The elements overlapping with those described above with respect to the preheating and recovering apparatus according to an embodiment of the present invention Omit it.

The coke oven facility according to another embodiment of the present invention includes a coke oven 200 for manufacturing coke; And a superheating and recovering device 100 installed in the carbonization chamber 210 of the coke oven 200.

Coal imported from overseas is transferred from the yard to the blending bin through a conveyor belt after waiting for a certain period of time and blended to maintain a constant composition. The combined coal is conveyed to the charging car of the coke oven 200 through the conveyor belt and charged (or charged) into the carbonization chamber 210 of the coke oven 200 from the charging car.

The coke oven 200 can produce coke. The coke oven 200 can be manufactured by carburizing the coal 10 charged in the carbonization chamber 210 of the coke oven 200.

The heat recovery apparatus 100 may be installed in the carbonization chamber 210 of the coke oven 200 and may be the heat recovery apparatus 100 according to an embodiment of the present invention. The heat recovery and recovery apparatus 100 includes a plurality of heat exchanging units 110 and a plurality of heat exchanging units 110 connected to each other by a plurality of heat exchanging units 110, So that the connecting member 120 can form the moving line 50 of the heat exchange medium. Thus, the heat exchange medium passes through the plurality of uprising pipes 211. Therefore, even when excessive heat is not exchanged in each riser pipe 211 during the recovery of the gas passing through the uprising pipe 211, High thermal energy can be obtained.

The coke oven 200 may include a plurality of carbonization chambers 210 and a plurality of combustion chambers 220. The coke oven 200 may include a plurality of carbonization chambers 210 and a plurality of combustion chambers 220. Here, the charge 10 may include coal 10. A plurality of uprising pipes 211 can be connected to the plurality of carbonization chambers 210, and heating of the charge 10 can be performed. The combustion chamber 220 may be connected to a plurality of carbonization chambers 210 to supply heat to the plurality of carbonization chambers 210 to heat the charge 10. [ For example, in the combustion chamber 220, the fuel can be maintained in a hot state by burning, and in the carbonation chamber 210, the coal 10 can be carbonized in the absence of air. Carrying of the coal 10 in the coke oven 200 can proceed for about 18 to 24 hours, followed by a one-stroke coke oven gas (Crude COG). The pulverized coal 10 is converted into coke, cooled and then charged into the blast furnace. The crude coke oven gas (Crude COG) is passed through the uprising pipe 211 to remove sulfur, (Coke oven) gas (COG) that is refined through a scrubber and used in steel mills.

The coke oven 200 is a device that indirectly carries coal 10 in the absence of air with hot heat energy. The coal 10 for coke can be introduced into the carbonization chamber 210 of the coke oven 200 through the inlet port 212 by using a charging device (not shown) in the coke oven 200. Here, the entry port 212 may be closed (or covered) by the entry port cover 212a when the charge 10 is carbonized. In the airless carbonization chamber 210, the coal 10 is carbonized, and a crude coke oven gas (Crude COG) is generated and can escape through the uprising pipe 211 at the upper end of the carbonization chamber 210. Ordinance of significant pressure can be injected through an orifice inlet (not shown) through the riser pipe 211 or at the gas trap 20 to lower the temperature of the high temperature one coke oven gas (Crude COG). The Ordnance may fall to a down comer, and at the same time, tar contained in the one-coke oven gas (Crude COG) may be separated.

In the absence of the heat recovery apparatus 100, the Ordnance temperature rises due to the cooling of the high temperature one coke oven gas (Crude COG), and at the same time, the entire Ordnation temperature circulating in the conversion process also rises and the purification efficiency of the coke oven gas Can fall. However, in the present invention, the temperature of the first coke oven gas (Crude COG) can be lowered (or lowered) primarily through the recovery of the first coke oven gas (Crude COG) using the first heat recovery apparatus 100, The temperature can be lowered (or lowered), and the purification quality (or efficiency) of the coke oven gas (COG) can be improved.

The coke oven 200 may include a combustion chamber 220 and a carbonization chamber 210. In the combustion chamber 220, the by-product gas such as coke oven gas (COG) In the carbonization chamber 210, the coal 10 may be injected to cause the carbonization. A one-stroke coke oven gas (Crude COG) is generated during the progress of the carbonization process, and a one-stroke coke oven gas (Crude COG) is passed through the uprising pipe 211 of the carbonization chamber 210. The heat exchanging unit 210 may be installed inside the uprising pipe 211 so that the amount of heat of the one-coke oven gas (Crude COG) that escapes through the uprising pipe 211 can be taken away. The heat exchanging unit 110 of each riser 211 can be connected by the connecting member 120 and the temperature of the heat exchanging medium can be increased each time the heat exchanging medium passes through one riser 211. The heat exchange medium transfers heat energy to the heat utilization engine 130 and the temperature thereof is lowered. The heat utilization engine 130 may utilize thermal energy (or heat) transferred from the heat exchange medium. In the present invention, only the moving line 50 of the heat exchange medium, which is composed of the plurality of heat exchanging units 110 and the connecting member 120, is installed at the upper end of the coke oven 200, and other components such as the heat utilizing engine 130 It is possible to minimize the facility load applied to the coke oven 200 due to the heat recovery and recovery device 100 since the coke oven 200 can be installed outside the coke oven 200. Also, in the present invention, the configuration of the heat recovery and recovery apparatus 100 is simplified by the plurality of heat exchanging units 110 and the connecting member 120, thereby solving the difficulty of maintenance.

A combustion chamber 220 may be provided corresponding to each carbonization chamber 210, respectively. Here, the plurality of carbonization chambers 210 and the plurality of combustion chambers 220 may be arranged alternately. When each combustion chamber 220 corresponds to each of the carbonization chambers 210, each combustion chamber 220 can control each of the carbonization chambers 210, so that the control of each of the carbonization chambers 210 can be facilitated , It is possible to control the carbonization chambers 210 to maintain the same carbonization condition or carbonization condition for each carbonization chamber 210. As a result, the coke of the same quality can be produced by carbonizing the coal 10 in the plurality of carbonization chambers 210.

As described above, in the present invention, a plurality of heat exchanging units may be provided in each of the plurality of risers, and a plurality of heat exchanging units may be connected to the connecting members so that the plurality of heat exchanging units and the connecting members may form a moving line of the heat exchanging medium. Thus, since the heat exchange medium is passed through the plurality of risers, the heat exchange medium can be used to obtain high thermal energy even when excessive heat is not exchanged in each riser pipe during the recovery of the gas passing through the riser. In addition, since only a moving line of the heat exchanging medium including a plurality of heat exchanging units and connecting members is installed in a facility including a plurality of uprising pipes, the load applied to the equipment can be minimized by the hot- In addition, the apparatus for recovering and recovering heat of the present invention can simplify the structure of the apparatus by a plurality of heat exchanging units and connecting members, thereby solving the difficulty of maintenance. On the other hand, when at least a part of the heat exchanging part is non-linear, the heat exchanging time of the heat exchanging medium can be increased, so that the effective heat exchanging medium can be recovered through the heat exchanging medium. When water is used as a heat exchange medium, the water is converted into steam through a plurality of uprising pipes, so that the heat of the gas passing through the uprising pipe can be recovered and high temperature and high pressure steam can be obtained. In addition, it is possible to prevent or suppress contamination of the surface of the heat exchanging part due to the adhered material through the protective member, so that the gas passing through the uprising pipe can directly contact the surface of the heat exchanging part, Can be effectively performed.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is clearly understood that the same is by way of illustration and example only and is not to be construed as limited to the embodiments set forth herein. Those skilled in the art will appreciate that various modifications and equivalent embodiments may be possible. Accordingly, the technical scope of the present invention should be defined by the following claims.

10: charge (coal) 20: gas collecting part
50: transfer line of heat exchange medium 100:
110: heat exchanger 120: connecting member
130: Heat utilization engine 140: Protection member (chain sling)
200: Equipment (coke oven) 210: Carbon seal
211: rising pipe 211a: rising pipe cover
212: entry opening 212a: entry opening door
220: Combustion chamber

Claims (11)

In a super heat recovery apparatus in which at least a part is installed in a facility including a plurality of ascending pipes,
A plurality of heat exchanging units each having a path formed therein for allowing a heat exchange medium capable of heat exchange with gas flowing in the riser pipe to pass therethrough, And
And a connection member having an internal path through which the heat exchange medium can pass so as to form a moving line of the plurality of heat exchange units and the heat exchange medium, and connecting the plurality of heat exchange units. The method according to claim 1,
Wherein the heat exchanging part is formed at least partially in a non-linear shape. The method according to claim 1,
And the heat exchanger is located in a central region of the uprising pipe. The method according to claim 1,
Wherein the heat exchanging portion has a plurality of bent portions or bent portions. The method according to claim 1,
Wherein the path length of the heat exchange unit located at one side of the movement line is different from the path length of the heat exchange unit located at the other side of the movement line. The method according to claim 1,
And a heat utilization engine connected to a moving line of the heat exchange medium to utilize heat energy transferred from the heat exchange medium which has passed through the moving line of the heat exchange medium. The method of claim 6,
And the heat utilization engine is connected to both sides of the movement line of the heat exchange medium. The method according to claim 1,
And a protective member disposed around the heat exchange unit to protect the heat exchange unit. The method of claim 8,
Wherein the protective member comprises a chain sling in which the adhesive material is removed by shaking. The method according to claim 1,
Wherein the heat exchange medium comprises water,
And the water is converted into steam through the movement line of the heat exchange medium. A coke oven for producing coke; And
A coke oven plant as set forth in any one of claims 1 to 10, wherein the coke oven is installed in a carbonization chamber of the coke oven.
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20190143684A (en) * 2018-06-21 2019-12-31 주식회사 포스코 Apparatus for controlling pressure of gas in coke oven
KR20220122598A (en) 2019-12-25 2022-09-02 디아이씨 가부시끼가이샤 Positive photosensitive resin composition, cured film, and resist film

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5984975A (en) * 1982-11-05 1984-05-16 Kouritsu Kikai Kogyo Kk Heat exchanger for ascention pipe of coke oven
JPS6095472U (en) * 1983-12-08 1985-06-29 新日本製鐵株式会社 Rising tube heat exchanger cooling system for sensible heat recovery equipment for coke oven gas
KR101450849B1 (en) * 2013-04-29 2014-10-23 주식회사 포스코 Heat recovery device of waste gas from standpipe of coke oven, and method thereof

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5984975A (en) * 1982-11-05 1984-05-16 Kouritsu Kikai Kogyo Kk Heat exchanger for ascention pipe of coke oven
JPS6095472U (en) * 1983-12-08 1985-06-29 新日本製鐵株式会社 Rising tube heat exchanger cooling system for sensible heat recovery equipment for coke oven gas
KR101450849B1 (en) * 2013-04-29 2014-10-23 주식회사 포스코 Heat recovery device of waste gas from standpipe of coke oven, and method thereof

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20190143684A (en) * 2018-06-21 2019-12-31 주식회사 포스코 Apparatus for controlling pressure of gas in coke oven
KR20220122598A (en) 2019-12-25 2022-09-02 디아이씨 가부시끼가이샤 Positive photosensitive resin composition, cured film, and resist film

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