KR101764713B1 - System and method for sensible heat recovery from coke oven gas - Google Patents

System and method for sensible heat recovery from coke oven gas Download PDF

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Publication number
KR101764713B1
KR101764713B1 KR1020150186762A KR20150186762A KR101764713B1 KR 101764713 B1 KR101764713 B1 KR 101764713B1 KR 1020150186762 A KR1020150186762 A KR 1020150186762A KR 20150186762 A KR20150186762 A KR 20150186762A KR 101764713 B1 KR101764713 B1 KR 101764713B1
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South Korea
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heat medium
temperature
pipe
heat
heat exchanger
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KR1020150186762A
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Korean (ko)
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KR20170076962A (en
Inventor
이창훈
이준석
박해웅
Original Assignee
주식회사 포스코
재단법인 포항산업과학연구원
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Priority to KR1020150186762A priority Critical patent/KR101764713B1/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
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • C10B27/06—Conduit details, e.g. valves
    • 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
    • C10B41/08—Safety devices, e.g. signalling or controlling devices for use in the discharge of coke for the withdrawal of the distillation gases
    • 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
    • C10B43/04—Removing incrustations by mechanical means
    • 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
    • C10B43/14—Preventing 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Coke Industry (AREA)

Abstract

The COG sensible heat recovery system according to an embodiment of the present invention includes a heat exchanger installed in an uprising pipe installed in a carbonization chamber, a first heat medium supply unit connected to an inlet of a heat exchanger, an outlet of the heat exchanger, And a second conveyance pipe connecting the second heat medium supply unit, the first conveyance pipe or the second heat medium supply unit and the inside of the riser pipe connected to each other.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a system and method for recovering COG,

The present invention relates to a COG sensible heat recovery system and method.

Generally, coke ovens produce coke by drying raw materials such as coal at high temperature. In order to produce coke, the coke oven stores coal in a carbonization chamber and then maintains it at a high temperature (1,100 ° C. or more) for a certain period of time. To this end, air and fuel gas are supplied to the combustion chamber, .

The coke oven has a plurality of independent carbonization chambers, and each carbonization chamber is provided with a riser. In the coke oven, CO gas (COG), which is a volatile gas, is generated during the process of carbonizing the coal stored in each carbonization chamber. The COK oven gas (COG) is supplied through a rising pipe installed in the coke oven .

Since the gas discharged through the riser pipe of the coke oven may contain volatile substances and a large amount of pollutants such as dust and tar, the gas discharged from the riser pipe is collected in the gas collecting pipe and sent to the post-treatment process .

On the other hand, the temperature of the gas discharged through the riser pipe in the coke oven is about 600 ° C to 900 ° C, and a large amount of heat energy is discharged during the passage of such a high temperature gas through the riser pipe. Coke ovens are required to recover heat energy discharged through riser tubes and reuse them into steelmaking processes to reduce energy consumption.

For this purpose, there has been an attempt to install a heat exchanger on the rising outer wall for recovering the heat energy discharged to the riser. However, the excessive heat exchange on the inner wall surface of the riser causes condensation of tar on the inner wall of the riser, The sensible heat of most of the high-temperature COG flowing into the furnace is not effectively recovered.

Also, when the tar is condensed on the inner wall of the uprising pipe as described above, the uprising pipe is blocked and it is difficult to discharge the COG smoothly, which seriously affects the operation of the coke oven.

Accordingly, the present invention provides a COG sensible heat recovery system and method that easily removes tar or carbon adhered to the inner wall of the ascending tube, thereby minimizing the clogging of the ascending tube.

According to an aspect of the present invention, there is provided a COG sensible heat recovery system including a heat exchanger installed in an uprising pipe installed in a carbonization chamber, a first heat medium supply unit connected to an inlet of a heat exchanger, And a second conveyance pipe connecting the second heat medium supply unit, the first conveyance pipe or the second heat medium supply unit and the uprising pipe, which are connected to the outlet through the first conveyance pipe.

And a heat medium consuming unit connecting the first heat medium supply unit and the second heat medium supply unit.

The heat exchanger may be a tubular heat exchanger, and the heating medium flowing in the heat exchanger may be water, steam or carbon dioxide.

According to another aspect of the present invention, there is provided a COG sensible heat recovery method comprising the steps of: supplying a low-temperature heat medium to a heat exchanger installed in an uprising pipe provided in each of a plurality of carbonization chambers using a first heat medium supply unit; Wherein the high temperature heat medium produced by heat exchange between the coke oven gas in the riser and the temperature of the low temperature heat medium is stored is stored in the second heat medium supply section, the high temperature heat medium is transferred from the second heat medium supply section to the first transfer pipe and the second transfer Wherein the high temperature heat medium is cooled and stored in the first heat medium supply unit by being cooled by the heat medium exhaust unit in the heat medium exhaust unit and the riser pipe through the pipe, Temperature heating medium supplied to the reforming reactor reacts with carbon in the riser pipe to produce carbon monoxide The.

The low temperature heat medium may be a temperature ranging from room temperature to 200 ° C.

The high-temperature heat medium may be a temperature of 110 ° C to 300 ° C.

The low temperature heat medium and the high temperature heat medium may be any of water, steam, and carbon dioxide.

As in the present invention, by using the COG sensible heat recovery system, it is possible to minimize the tar and carbon adhering to the inside of the riser pipe, thereby preventing the rising pipe from being clogged.

Further, by circulating the heat recovered from the coke oven gas and effectively using it, it is possible to reduce the production cost of the coke.

1 is a schematic block diagram of a COG sensible heat recovery system according to an embodiment of the present invention.
Fig. 2 is an enlarged view of a part of Fig.

Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the invention. Wherever possible, the same or similar parts are denoted using the same reference numerals in the drawings.

All terms including technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the art to which the present invention belongs. 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.

The drawings are schematic and illustrate that they are not shown to scale. The relative dimensions and ratios of the parts in the figures are shown exaggerated or reduced in size for clarity and convenience in the figures, and any dimensions are merely illustrative and not restrictive.

Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.

FIG. 1 is a schematic configuration diagram of a COG sensible heat recovery system according to an embodiment of the present invention, and FIG. 2 is an enlarged view of a portion of FIG.

1, a COG sensible heat recovery system according to an embodiment of the present invention includes a riser pipe 100 connected to a plurality of carbonization chambers, a heat exchanger 200 installed in each riser pipe 100, And a heating medium consuming part 500 connected to the first heat medium supplying part 300 and the second heating medium supplying part 400 and the second heating medium supplying part 400 connected to the heat exchanger 200.

The uprising pipe 100 is connected to the inside of the carbonization chamber and the carbonization chamber may be a coke oven. In the uprising pipe 100, coke oven gas (COG) generated in the carbonization chamber moves.

The heat exchanger 200 may be installed in the riser pipe 100 in the form of a tubular heat exchanger and may be installed in the riser pipe in a repeatedly bent form in order to increase the contact area and effect heat exchange.

The first heat medium supply unit 300 supplies the low temperature heat medium to the heat exchanger 200 and supplies the low temperature heat medium to the heat exchanger 200. The heating medium may include water, water vapor, carbon dioxide, and the like. The temperature of the low temperature heat medium may be supplied from room temperature to 200 DEG C lower than the temperature of the coke oven gas flowing into the riser pipe.

The second heat medium supply unit 400 is connected to the outlet of the heat exchanger 200 and stores a high temperature heat medium whose temperature has been increased by heat exchange and supplies a high temperature heat medium to the heat medium dissipation unit when necessary. The low-temperature heat medium injected into the heat exchanger 200 is heat-exchanged with the coke oven gas passing through the riser, and the temperature of the heat medium can be raised to 110 ° C to 300 ° C.

The heating medium consuming unit 500 may be a radiator such as a radiator, a steam drier, or the like, which utilizes the heat of the high-temperature heating medium discharged from the heat exchanger 200.

The heating medium consuming part 500 and the second heating medium supplying part 400 are connected to each other by a first conveyance pipe 51 to receive a high temperature heating medium. The heat medium consuming part 500 may be connected to the first heat medium supplying part 300 through the second conveying pipe 52. When the heat is consumed by the heat medium consuming part 500, the temperature of the high temperature heat medium is lowered and it is transferred to the first heat medium supplying part 300 through the second conveying pipe 52 and can be used as a low temperature heat medium.

The second heating medium supply part 400 may be connected to the inside of the uprising pipe and the third conveyance pipe 53. The high-temperature heating medium stored in the second heating medium supply unit 400 may be transferred to the inside of the uprising pipe through the fourth feeding pipe 54 branched from the third feeding pipe 53. Further, the high temperature heat medium can be supplied into the uprising pipe through the fifth conveyance pipe 55 directly connected to the second heat medium supplier 400. The fourth conveyance pipe (54) and the fifth conveyance pipe (55) can be selectively installed as required.

A valve and a flow meter may be installed in each of the first to fifth transfer pipes (51) to (55), and the flow rate is adjusted according to the required amount and temperature.

When the heat exchanger is installed in each of the plurality of uprising pipes, the low-temperature heat medium transferred from the first heat medium supplier 300 can be connected to the respective heat exchangers by using the branched sixth transfer pipe 56. A valve and a flow meter are also provided on each branch of the branched sixth conveyance pipe (56), and the flow rate can be adjusted in accordance with each rising pipe condition.

The COG sensible heat recovery method using the above sensible heat recovery system will be described in detail.

The method for recovering COG sensible heat comprises the steps of supplying a low-temperature heat medium to a heat exchanger provided in an uprising pipe provided in each of a plurality of carbonization chambers by using a first heat medium supply unit, heat exchange between the heat exchanger and the coke oven gas in the uprising pipe, Storing the generated high-temperature heat medium in the second heat medium supply unit, supplying the high-temperature heat medium from the second heat medium supply unit to the heat medium exhaust unit and the uprising pipe through the first transfer pipe and the second transfer pipe, respectively , The high temperature heat medium is cooled in the heat medium consuming part to generate the low temperature heat medium and stored in the first heat medium supply part, and the high temperature heat medium supplied to the uprising pipe through the second conveyance pipe reacts with carbon in the uprising pipe, .

The coke oven gas generated in the coke oven is introduced into the uprising pipe from the lower part of the uprising pipe and moves upward toward the upper part of the uprising pipe. The main components of the Kosc oven may be hydrogen, methane, carbon monoxide, and may also include other components such as tar, vegetable oil, ammonia, hydrogen sulfide, hydrogen cyanide, and the like.

At this time, the temperature of the coke oven gas flowing into the uprising pipe is 600 ° C to 900 ° C.

On the other hand, a low-temperature heating medium supplied from the first heating medium supply unit 300 flows into the inside of the tube of the heat exchanger 200 installed inside the uprising pipe. At this time, the low temperature heat medium temperature is supplied at a temperature lower than the temperature of the coke oven gas, for example, 200 ° C or lower.

When the low-temperature heat medium is supplied into the heat exchanger 200, heat exchange occurs between the high-temperature coke oven gas flowing outside the heat exchanger 200 and the low-temperature heat medium. Accordingly, the temperature of the heating medium inside the heat exchanger 200 increases and the temperature of the coke oven gas outside the heat exchanger 200 decreases.

Thereafter, the heat medium flowing in the heat exchanger 200 is transferred to the second heat medium supplier 400 after the temperature rises. At this time, the temperature of the heating medium transferred to the second heating medium supply part 400 may be higher than the temperature of the low-temperature heating medium, and may be approximately 300 ° C or less.

The high temperature heat medium transferred to the second heat medium supplier 400 may be transferred to the heat medium consuming unit 500 requiring heat energy or may be supplied again to the riser through the fourth transfer pipe 54 or the fifth transfer pipe 55 have.

The temperature of the heating medium is lowered by the heating medium consuming part and then transmitted to the first heating medium supplying part 300 and used as a low temperature heating medium to be injected into the heat exchanger.

On the other hand, the heating medium re-supplied to the uprising pipe through the fourth conveyance pipe 54 or the fifth conveyance pipe 55 reacts with tar or attached carbon adhered to the inner wall of the re-supply pipe as shown in the following reaction formulas 1 and 2 .

[Reaction Scheme 1]

C + H 2 O? CO + H 2 (? H = + 131.4 kJ / mol)

[Reaction Scheme 2]

C + CO 2 ? 2CO (? H = + 172.6 kJ / mol)

The high-temperature heat medium can be supplied to uniformly diffuse into the riser by spraying at a constant pressure using a nozzle or the like.

As described above, by injecting the high-temperature heating medium into the re-supply pipe, it is possible to easily remove tar or carbon adhering to the re-supply inner wall. A valve and a flow meter may be installed in the fourth conveyance pipe 54 and the fifth conveyance pipe 55 to adjust the amount of the heating medium to be supplied depending on the amount of tar or carbon to be removed.

Using the COG sensible heat recovery system as in the embodiment of the present invention, the sensible heat of the COG can be circulated continuously and the tar or carbon can be easily removed without any additional apparatus and process.

While the present invention has been described in connection with what is presently considered to be practical exemplary embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, Of course.

51: first conveyance pipe 52: second conveyance pipe
53: Third conveying pipe 54: Fourth conveying pipe
55: fifth conveying pipe 56: sixth conveying pipe
100: riser 200: heat exchanger
300: first heating medium supply part
400: second heating medium supply part

Claims (7)

A heat exchanger installed inside the uprising pipe provided in the carbonization chamber,
A first heat medium supply unit connected to an inlet of the heat exchanger,
A second heat medium supply unit connected to the outlet of the heat exchanger through a first transfer pipe,
A second conveyance pipe connecting the first conveyance pipe or the second heating medium supply unit to the inside of the uprising pipe,
And a heat medium consuming unit (120) for connecting the first heat medium supply unit
The COG sensible heat recovery system. delete The method of claim 1,
The heat exchanger is a tubular heat exchanger,
Wherein the heat medium flowing in the heat exchanger is water, steam or carbon dioxide. Supplying a low-temperature heating medium to the heat exchanger provided in the uprising pipe provided in each of the plurality of carbonization chambers by using the first heat medium supply unit,
Heat exchange occurs between the heat exchanger and the coke oven gas in the uprising pipe, the high temperature heat medium generated by the temperature rise of the low temperature heat medium is stored in the second heat medium supplier,
Supplying the high-temperature heat medium from the second heat medium supply unit to the heat medium consuming unit and the uprising pipe through the first conveyance pipe and the second conveyance pipe, respectively,
Wherein the high-temperature heat medium is cooled in the heat medium exhaust part, and the low-temperature heat medium is generated and stored in the first heat medium supply part; and
Wherein the high temperature heat medium supplied to the uprising pipe through the second feed pipe reacts with carbon in the uprising pipe to produce carbon monoxide
And the COG sensible heat recovery method. 5. The method of claim 4,
Wherein the low-temperature heat medium is a temperature of room temperature to 200 ° C. 5. The method of claim 4,
Wherein the high-temperature heat medium is at a temperature of 110 ° C to 300 ° C. 5. The method of claim 4,
Wherein the low temperature heat medium and the high temperature heat medium are any one of water, steam, and carbon dioxide.
KR1020150186762A 2015-12-24 2015-12-24 System and method for sensible heat recovery from coke oven gas KR101764713B1 (en)

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KR101764713B1 true KR101764713B1 (en) 2017-08-04

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3055405B2 (en) 1994-11-07 2000-06-26 日本鋼管株式会社 Sensible heat recovery method for crude coke oven gas
KR101104350B1 (en) 2009-05-27 2012-01-16 신한열기 주식회사 System for Reclaiming Waste Heat From Boiler
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
JP3055405B2 (en) 1994-11-07 2000-06-26 日本鋼管株式会社 Sensible heat recovery method for crude coke oven gas
KR101104350B1 (en) 2009-05-27 2012-01-16 신한열기 주식회사 System for Reclaiming Waste Heat From Boiler
KR101450849B1 (en) * 2013-04-29 2014-10-23 주식회사 포스코 Heat recovery device of waste gas from standpipe of coke oven, and method thereof

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