JPS6241994B2 - - Google Patents
Info
- Publication number
- JPS6241994B2 JPS6241994B2 JP59117059A JP11705984A JPS6241994B2 JP S6241994 B2 JPS6241994 B2 JP S6241994B2 JP 59117059 A JP59117059 A JP 59117059A JP 11705984 A JP11705984 A JP 11705984A JP S6241994 B2 JPS6241994 B2 JP S6241994B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- heat exchanger
- deaerator
- gas
- recovery boiler
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 51
- 239000007789 gas Substances 0.000 claims description 22
- 239000000112 cooling gas Substances 0.000 claims description 14
- 238000011084 recovery Methods 0.000 claims description 14
- 239000000571 coke Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 description 7
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000007872 degassing Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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
Description
【発明の詳細な説明】
（産業上の利用分野）
この発明は赤熱コークスを乾式消火する際の排
熱回収ボイラからガス循環ブロワーによつて排出
された循環冷却ガスがまだ保有しているガス顕熱
を脱気前のボイラ給水に回収し、かつ給水温度を
循環冷却ガスの水露点以上に加熱する装置に関す
るものである。Detailed Description of the Invention (Industrial Field of Application) This invention is a method for dry-extinguishing red-hot coke, in which the circulating cooling gas discharged from the exhaust heat recovery boiler by the gas circulation blower is still retained. The present invention relates to a device that recovers heat to the boiler feed water before degassing and heats the feed water to a temperature higher than the water dew point of the circulating cooling gas.
（従来の技術）
排熱回収ボイラから排出した循環冷却ガスの保
有するガス顕熱を、ガス循環ブロワーの入側また
は出側において脱気前のボイラ給水に回収する技
術は既に公知である。(Prior Art) A technique is already known in which gas sensible heat possessed by circulating cooling gas discharged from an exhaust heat recovery boiler is recovered into boiler feed water before deaeration at the inlet or outlet side of a gas circulation blower.
たとえば日本動力協会会報「動力」159号
（S57―12―20）P.40、日本設計製図学会誌「設
計製図」VOL.18、No.99（S58―１―10）P.21に
紹介されているが、要約すれば第２図に示すごと
くになる。 For example, it was introduced in the Japan Power Association newsletter "Power" No. 159 (S57-12-20) P. 40 and the Japan Design and Drafting Society journal "Design Drafting" VOL. 18, No. 99 (S58-1-10) P. 21. However, it can be summarized as shown in Figure 2.
すなわちチヤンバー１に装入された赤熱コーク
スを消火して高温になつた循環冷却ガスは、ダス
トキヤツチヤー２を通つて排熱回収ボイラ３に導
かれる。ここにおいて循環冷却ガスの保有するガ
ス顕熱を水によつて回収し、ガス循環ブロワー４
およびその前後の間接熱交換器５を通り、再びチ
ヤンバー１に導入される。 That is, the circulating cooling gas that has reached a high temperature by extinguishing the red-hot coke charged in the chamber 1 is led to the exhaust heat recovery boiler 3 through the dust catcher 2. Here, the gas sensible heat possessed by the circulating cooling gas is recovered by water, and the gas circulation blower 4
The heat exchanger 5 passes through the indirect heat exchanger 5 before and after the heat exchanger 5, and is introduced into the chamber 1 again.
一方ボイラへの給水はボイラ給水タンク９から
脱気器給水ポンプ８によりガス循環ブロワー４の
入側と出側に設けた間接熱交換器５へ導入され、
循環冷却ガスと熱交換し、脱気器６にて脱気され
ボイラ給水ポンプ７により排熱回収ボイラ３へと
給水される。ここにおいて水は循環冷却ガスと熱
交換し、蒸気となつて蒸気管１１により系外に取
り出される。 On the other hand, the water supplied to the boiler is introduced from the boiler water supply tank 9 by the deaerator water supply pump 8 to the indirect heat exchanger 5 provided on the inlet and outlet sides of the gas circulation blower 4.
It exchanges heat with the circulating cooling gas, is degassed by a deaerator 6, and is supplied to the exhaust heat recovery boiler 3 by a boiler water supply pump 7. Here, the water exchanges heat with the circulating cooling gas, becomes steam, and is taken out of the system through the steam pipe 11.
なお蒸気管１１から脱気器６へ脱気用蒸気管１
２が分岐し、前述の蒸気の一部が水の加熱に用い
られる。 Note that the deaeration steam pipe 1 is connected from the steam pipe 11 to the deaerator 6.
2 is branched and a portion of the aforementioned steam is used to heat the water.
前記の循環冷却ガスは間接熱交換器５を介して
通常20℃前後のボイラ給水と熱交換させるため常
に間接熱交換器５の管壁温度はボイラ給水温度に
左右される。 The circulating cooling gas exchanges heat with the boiler feed water, which is usually around 20° C., through the indirect heat exchanger 5, so the temperature of the pipe wall of the indirect heat exchanger 5 always depends on the boiler feed water temperature.
従つて循環冷却ガスの接触する管の外壁近くで
はガス温度が水露点以上に降下するため、ガス中
の水分が間接熱交換器５の管外壁に結露すると共
に、この水適を媒体としてガス中の腐食成分およ
びダスト等が付着する現象を生ずる。 Therefore, near the outer wall of the pipe in contact with the circulating cooling gas, the gas temperature drops to above the water dew point, so that the moisture in the gas condenses on the outer wall of the pipe of the indirect heat exchanger 5, and the moisture in the gas is used as a medium to dew. This causes a phenomenon in which corrosive components and dust adhere to the surface.
この様な現象下では間接熱交換器５の管外壁の
腐食およびダスト堆積によるガス側抵抗の増加等
で安定した連続運転が困難となる。一方水露点対
策の１つとして間接熱交換器５の入側給水温度を
他の熱源で昇温する方法が考えられるが、この方
法では、間接熱交換器５の出側、つまり脱気器給
水温度が上昇し脱気器６内の熱バランスは一定で
あるため入熱増分だけ脱気用蒸気量が少くなり、
脱気性能を低下させることになる。 Under such a phenomenon, stable continuous operation becomes difficult due to corrosion of the tube outer wall of the indirect heat exchanger 5 and an increase in gas side resistance due to dust accumulation. On the other hand, one possible measure against water dew point is to raise the temperature of the water supply on the inlet side of the indirect heat exchanger 5 using another heat source. As the temperature rises and the heat balance inside the deaerator 6 remains constant, the amount of deaeration steam decreases by the amount of heat input.
This will reduce the degassing performance.
（発明が解決しようとする問題点）
本発明は従来の技術の欠点であつた間接熱交換
器の管外壁へのガス中の腐食成分およびダスト等
の付着が生じない装置を提供することにある。(Problems to be Solved by the Invention) An object of the present invention is to provide an apparatus in which corrosive components in gas, dust, etc. do not adhere to the outer wall of the pipes of an indirect heat exchanger, which was a drawback of the conventional technology. .
（問題点を解決するための手段・作用）
循環冷却ガスが赤熱コークスを装入するチヤン
バー１、排熱回収ボイラ３、ガス循環ブロワー
４、ガス循環ブロワー４の前および／または後に
設けた間接熱交換器５を経由してチヤンバー１に
循環するようにし、
排熱回収ボイラ３への給水が間接熱交換器５、
脱気器６、排熱回収ボイラ３を経由し、蒸気とし
て系外へ取り出される様にしたコークス乾式消火
設備において、間接熱交換器５入側の給水と脱気
器６入側の給水とを熱交換させる水対水熱交換器
１０を脱気器６の入側に設けたことを特徴とする
コークス乾式消火設備における給水加熱装置であ
つて、間接加熱装置５に給水される水温を循環冷
却ガスの水露点以上に上昇させるものである。(Means/effects for solving the problem) A chamber 1 in which circulating cooling gas is charged with red-hot coke, an exhaust heat recovery boiler 3, a gas circulation blower 4, and indirect heat provided before and/or after the gas circulation blower 4. The water is circulated to the chamber 1 via the exchanger 5, and the water supplied to the exhaust heat recovery boiler 3 is passed through the indirect heat exchanger 5,
In a coke dry extinguishing system in which the coke is taken out of the system as steam via a deaerator 6 and an exhaust heat recovery boiler 3, the water supply on the input side of the indirect heat exchanger 5 and the water supply on the input side of the deaerator 6 are separated. This is a feed water heating device for a coke dry fire extinguishing facility, characterized in that a water-to-water heat exchanger 10 for heat exchange is provided on the inlet side of the deaerator 6, and the water temperature of the water supplied to the indirect heating device 5 is circulated and cooled. This raises the temperature above the water dew point of the gas.
（実施例）
本発明の１実施例を示す第１図を用いて詳細に
説明する。(Example) An example of the present invention will be described in detail using FIG. 1.
循環冷却ガスの流れはチヤンバー１と排熱回収
ボイラ３の間を循環する従来設備と同じである。 The flow of the circulating cooling gas is the same as in conventional equipment where it circulates between the chamber 1 and the waste heat recovery boiler 3.
排熱回収ボイラ３への給水は、ボイラ給水タン
ク９から脱気器給水ポンプ８によつて水対水熱交
換器１０を経由してガス循環ブロワー４の入側と
出側に設けられた間接熱交換器５に給水される。 Water is supplied to the exhaust heat recovery boiler 3 from a boiler water supply tank 9 by a deaerator water supply pump 8, via a water-to-water heat exchanger 10, and then through an indirect pipe provided at the inlet and outlet sides of the gas circulation blower 4. Water is supplied to the heat exchanger 5.
この間接熱交換器５はガス循環ブロワー４の入
側または出側のいずれか１方に設置してもよい。
間接熱交換器５を経て循環冷却ガスにより加熱さ
れた給水は、水対水熱交換器１０において、間接
熱交換器５の入側の給水と熱交換された後脱気器
６に入り、別経路の脱気用蒸気管１２により供給
された蒸気と混合し昇温脱気される。その後ボイ
ラ給水ポンプ７によつて排熱回収ボイラ３に供給
され蒸気管１１により系外へ取り出される。 This indirect heat exchanger 5 may be installed on either the inlet side or the outlet side of the gas circulation blower 4.
The feed water heated by the circulating cooling gas via the indirect heat exchanger 5 undergoes heat exchange with the feed water on the inlet side of the indirect heat exchanger 5 in the water-to-water heat exchanger 10, and then enters the deaerator 6 and is separated from the water. It mixes with the steam supplied from the deaeration steam pipe 12 in the path and is degassed at elevated temperature. Thereafter, it is supplied to the exhaust heat recovery boiler 3 by the boiler feed water pump 7 and taken out of the system through the steam pipe 11.
従来法であると間接熱交換器５入側の給水温度
は20℃程度であるから間接熱交換器５の低温部管
外壁が水露点に達し、管壁外表面に循環ガス中の
水分の結露が生じ、循環ガス中の硫酸成分等の腐
蝕成分が付着して管壁の腐食がおこるとともに、
前記結露にダストが付着してガス側圧損の増大と
いう問題が発生する。 In the conventional method, the water supply temperature at the input side of the indirect heat exchanger 5 is about 20°C, so the outer wall of the low-temperature pipe of the indirect heat exchanger 5 reaches the water dew point, and moisture in the circulating gas condenses on the outer surface of the pipe wall. This causes corrosive components such as sulfuric acid components in the circulating gas to adhere, causing corrosion of the pipe walls.
Dust adheres to the dew condensation, causing a problem of increased gas side pressure loss.
本発明の装置では、間接熱交換器５から出た高
温の給水を水対水熱交換器１０において、間接熱
交換器５に入る前の低温の給水と熱交換し、間接
熱交換器５入側の給水を循環冷却ガスの水露点以
上に昇温させるものである。 In the apparatus of the present invention, the high temperature feed water coming out of the indirect heat exchanger 5 is heat exchanged with the low temperature feed water before entering the indirect heat exchanger 5 in the water-to-water heat exchanger 10. This is to raise the temperature of the water supply on the side above the water dew point of the circulating cooling gas.
（発明の効果）
以上詳述した如く、本発明を実施することによ
つて間接熱交換器５の低温部管外壁に結露を生じ
ないので、腐食およびダスト堆積の問題を解消す
ることが出来る。(Effects of the Invention) As described in detail above, by carrying out the present invention, no condensation occurs on the outer wall of the low-temperature section tube of the indirect heat exchanger 5, so the problems of corrosion and dust accumulation can be solved.
第１図は本発明の１実施例を示す説明図、第２
図は従来技術を示す説明図である。
１……チヤンバー、２……ダストキヤツチヤ
ー、３……排熱回収ボイラ、４……ガス循環ブロ
ワー、５……間接熱交換器、６……脱気器、７…
…ボイラ給水ポンプ、８……脱気器給水ポンプ、
９……ボイラ給水タンク、１０……水対水熱交換
器、１１……蒸気管、１２……脱気用蒸気管。
Figure 1 is an explanatory diagram showing one embodiment of the present invention, Figure 2 is an explanatory diagram showing one embodiment of the present invention.
The figure is an explanatory diagram showing a conventional technique. 1... Chamber, 2... Dust catcher, 3... Exhaust heat recovery boiler, 4... Gas circulation blower, 5... Indirect heat exchanger, 6... Deaerator, 7...
...Boiler feed water pump, 8...Deaerator water feed pump,
9...Boiler feed water tank, 10...Water-to-water heat exchanger, 11...Steam pipe, 12...Steam pipe for degassing.
Claims (1)
ンバー１、排熱回収ボイラ３、ガス循環ブロワー
４、ガス循環ブロワー４の前および／または後に
設けた間接熱交換器５を経由してチヤンバー１に
循環するようにし、 排熱回収ボイラ３への給水が間接熱交換器５、
脱気器６、排熱回収ボイラ３を経由して系外へ取
り出されるようにしたコークス乾式消火設備にお
いて、間接熱交換器５入側の給水と脱気器６入側
の給水とを熱交換させる水対水熱交換器１０を脱
気器入側に設けたことを特徴とするコークス乾式
消火設備における給水加熱装置。[Claims] 1. Circulating cooling gas passes through a chamber 1 into which red-hot coke is charged, an exhaust heat recovery boiler 3, a gas circulation blower 4, and an indirect heat exchanger 5 provided before and/or after the gas circulation blower 4. The water supplied to the exhaust heat recovery boiler 3 is circulated to the chamber 1 through the indirect heat exchanger 5,
In a coke dry extinguishing system in which coke is taken out of the system via a deaerator 6 and an exhaust heat recovery boiler 3, heat is exchanged between the water supply on the input side of the indirect heat exchanger 5 and the water supply on the input side of the deaerator 6. A feed water heating device in a coke dry fire extinguishing facility, characterized in that a water-to-water heat exchanger 10 is provided on the inlet side of a deaerator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59117059A JPS60260686A (en) | 1984-06-07 | 1984-06-07 | Feed water heater in dry-quenching installation for coke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59117059A JPS60260686A (en) | 1984-06-07 | 1984-06-07 | Feed water heater in dry-quenching installation for coke |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60260686A JPS60260686A (en) | 1985-12-23 |
| JPS6241994B2 true JPS6241994B2 (en) | 1987-09-05 |
Family
ID=14702407
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59117059A Granted JPS60260686A (en) | 1984-06-07 | 1984-06-07 | Feed water heater in dry-quenching installation for coke |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60260686A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| UA83983C2 (en) * | 2007-12-07 | 2008-08-26 | Общество С Ограниченной Ответственностью Научно-Техническое Предприятие "Котлоэнергопром" | Plant and method for dry coke quenching |
| JP2013040242A (en) * | 2011-08-12 | 2013-02-28 | Jp Steel Plantech Co | Coke dry quenching equipment |
-
1984
- 1984-06-07 JP JP59117059A patent/JPS60260686A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60260686A (en) | 1985-12-23 |
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