JPH0128286B2 - - Google Patents
Info
- Publication number
- JPH0128286B2 JPH0128286B2 JP54143841A JP14384179A JPH0128286B2 JP H0128286 B2 JPH0128286 B2 JP H0128286B2 JP 54143841 A JP54143841 A JP 54143841A JP 14384179 A JP14384179 A JP 14384179A JP H0128286 B2 JPH0128286 B2 JP H0128286B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- fluidized bed
- amount
- combustion
- air
- 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
- 238000002485 combustion reaction Methods 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 4
- 230000000717 retained effect Effects 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 25
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 17
- 229910052815 sulfur oxide Inorganic materials 0.000 description 7
- 239000003245 coal Substances 0.000 description 4
- 239000000446 fuel Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
- F23C2900/99006—Arrangements for starting combustion
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Feeding And Controlling Fuel (AREA)
- Control Of Steam Boilers And Waste-Gas Boilers (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Regulation And Control Of Combustion (AREA)
Description
【発明の詳細な説明】
この発明は流動層ボイラを起動する方法に関す
る。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for starting a fluidized bed boiler.
流動層炉を起動するには通常起動バーナにより
流動媒体を加熱するか、または熱風炉を別に設け
その炉からの熱風を流動層に供給する手段がとら
れている。前者の場合流動層上方に起動バーナを
位置させ、火炎を流動層に吹き付けするものが多
い。この場合従来は重油、軽油を燃焼するバーナ
が使用されている。しかし近時の石油事情よりし
て、石炭焚きの燃焼炉が見直しされ、その燃焼に
好適な流動層を使用する流動層ボイラが着目され
ている。この場合起動用バーナにも粉細粒炭を燃
焼させるバーナを使用する必要がある。しかし石
炭燃焼においてはNOx（窒素酸化物）、SOx（硫黄
酸化物）、粉じんが多いという問題がある。この
問題は起動バーナにおいても当然に生ずる問題で
あり、これらの排出を極力少ないものとする起動
手段が要望されるものである。 To start a fluidized bed furnace, the fluidized bed is usually heated by a startup burner, or a hot blast furnace is provided separately and hot air from the furnace is supplied to the fluidized bed. In the former case, a starting burner is often located above the fluidized bed and flame is sprayed onto the fluidized bed. In this case, burners that burn heavy oil or light oil have traditionally been used. However, due to the recent petroleum situation, coal-fired combustion furnaces have been reconsidered, and attention has been focused on fluidized bed boilers that use a fluidized bed suitable for combustion. In this case, it is necessary to use a burner that burns pulverized coal as the starting burner. However, coal combustion has the problem of producing a lot of NOx (nitrogen oxides), SOx (sulfur oxides), and dust. This problem naturally occurs in starting burners, and there is a need for a starting means that minimizes these emissions as much as possible.
この発明は流動層炉特に石炭焚きの流動層ボイ
ラにおいてSOx NOx粉じんの少ない起動の方法
を提案することを目的とする。 The purpose of this invention is to propose a method for starting a fluidized bed furnace, especially a coal-fired fluidized bed boiler, with less SOx NOx dust.
要するにこの発明は、起動バーナの点火と同時
に再循環フアンで排ガスを吸引して流動層ボイラ
の空気室に供給し、ボイラ装置外への排ガス量を
低減して粉じん、NOx、SOxの排出絶体量を低
減し、かつその排ガス保有熱を流動媒体加熱用熱
量の一部として流動層の昇温を早め、また排ガス
中のO2を計測して供給する燃焼用空気と排ガス
の混合気体の含有するO2を燃焼に適する量とす
るように排ガス再循環量を制御する流動層ボイラ
の起動方法であることを特徴とする。 In short, this invention sucks exhaust gas with a recirculation fan and supplies it to the air chamber of the fluidized bed boiler at the same time as the start-up burner ignites, reducing the amount of exhaust gas outside the boiler equipment and eliminating the exhaust gas of dust, NOx, and SOx. Contains a mixture of combustion air and exhaust gas that reduces the amount of combustion air and accelerates the temperature rise of the fluidized bed by using the heat retained in the exhaust gas as part of the heat amount for heating the fluidized medium, and also measures and supplies O 2 in the exhaust gas. The present invention is characterized in that it is a method for starting a fluidized bed boiler that controls the amount of exhaust gas recirculation so that the amount of O 2 is suitable for combustion.
この発明を以下図面により説明する。流動層ボ
イラ１内には流動層２が形成され、流動媒体はバ
ーナ３の燃料により加熱される。その燃焼により
生じた熱は蒸発管４、過熱器管５に伝えられ、最
終的にタービン（図示せず）に送られる。排ガス
は空塔部６を通り蒸発管群４ａ，４ｂに熱を与へ
発生した蒸気はドラム７に送られる。排ガスはさ
らに節炭器８を通りダクト９から図示しない脱硝
装置、集じん装置、脱硫装置、空気予熱器等を経
由して煙突より大気中に排出される。図示例にお
いては粉細粒炭を燃焼する起動用バーナ１０が空
塔部６に設けられその火炎は流動層上面に吹き付
けられ流動媒体を加熱し流動層を加熱する。起動
用バーナ１０からの粉細粒炭の供給量は制御弁１
０ａで制御される。 This invention will be explained below with reference to the drawings. A fluidized bed 2 is formed in the fluidized bed boiler 1 , and the fluidized medium is heated by fuel from a burner 3 . The heat generated by the combustion is transferred to the evaporator tube 4, the superheater tube 5, and finally sent to a turbine (not shown). The exhaust gas passes through the empty tower section 6 and imparts heat to the evaporator tube groups 4a and 4b, and the generated steam is sent to the drum 7. The exhaust gas further passes through the economizer 8, passes through a duct 9, passes through a denitrification device, a dust collector, a desulfurization device, an air preheater, etc. (not shown), and is discharged into the atmosphere from a chimney. In the illustrated example, a starting burner 10 for burning pulverized coal is provided in the empty column 6, and its flame is blown onto the upper surface of the fluidized bed to heat the fluidized medium and the fluidized bed. The supply amount of pulverized coal from the starting burner 10 is controlled by the control valve 1.
Controlled by 0a.
この場合、燃焼する燃料は少なく、排ガス温度
は低いものであつてもNOx SOx粉じんの発生は
まぬがれがたい。加えてこれら有害成分を除去す
る装置も充分に機能しにくいという状況にある。 In this case, even if the amount of fuel to be combusted is small and the exhaust gas temperature is low, the generation of NOx SOx dust is unavoidable. In addition, it is difficult for equipment to remove these harmful components to function satisfactorily.
起動に際して、酸素（O2）を充分に含む空気
をしかも流動層形成のために過多に供給すること
はNOxの発生をもまねくこととなる。そのため
排ガスの一部を流動層空気室に導入しO2低減を
しかつ排ガスの保有する熱を回収しながら充分に
流動層の流動化を確保しようというものである。
このため排ガスの流れる節炭器後流のダクト９と
流動層空気室１１とを管路１２で接続し、この管
路に昇圧をする再循環フアン１３と制御ダンパ１
４を設ける。この場合節炭器８の後流に排ガス中
のO2含有量を検知するO2メータ１５を設けその
信号を制御箱１６に送る。また更にO2量の制御
のため不活性ガス（N2ガス、CO2ガス等）を管
路１７、ダンパ１７ａを経由して流動層空気室１
１に補給することができる。O2メータ１５ａは
流動層空気室１１内に設け最終の流動用空気中の
O2量を検知しその信号を制御箱１６に送つて制
御することもできる。制御箱１６は記憶装置（図
示せず）の指令とO2メータ１５，１５ａの信号
とにより、指令信号を送風機１８の出口のダンパ
１９、燃料供給管路のダンパ１７ａ、ダンパ１
４、制御弁１０ａに送りこれ等を制御する。この
ため、送風機１８からの起動用空気量は再循環ガ
スが供給されることによりその量は少くてすみ、
NOx SOx粉じんをを含む排ガスの装置外排出は
少なく大部分は再循環され、かつその保有する熱
量は回収されて有効に利用されることとなる。 At startup, supplying too much air containing sufficient oxygen (O 2 ) to form a fluidized bed will also lead to the generation of NOx. Therefore, part of the exhaust gas is introduced into the fluidized bed air chamber to reduce O 2 and to recover the heat held in the exhaust gas while ensuring sufficient fluidization of the fluidized bed.
For this purpose, a duct 9 downstream of the economizer through which exhaust gas flows and a fluidized bed air chamber 11 are connected by a pipe 12, and a recirculation fan 13 and a control damper 1 are connected to this pipe to increase the pressure.
4 will be provided. In this case, an O 2 meter 15 for detecting the O 2 content in the exhaust gas is provided downstream of the economizer 8 and sends its signal to the control box 16 . Furthermore, in order to control the amount of O 2 , inert gas (N 2 gas, CO 2 gas, etc.) is supplied to the fluidized bed air chamber 1 via a pipe 17 and a damper 17a.
1 can be replenished. The O 2 meter 15a is installed in the fluidized bed air chamber 11 to measure the final fluidized air.
It is also possible to detect the amount of O 2 and send the signal to the control box 16 for control. The control box 16 sends command signals to the damper 19 at the outlet of the blower 18, the damper 17a of the fuel supply pipe, and the damper 1 based on the command from the storage device (not shown) and the signals from the O 2 meters 15 and 15a.
4. Send it to the control valve 10a to control these. Therefore, the amount of starting air from the blower 18 can be reduced due to the supply of recirculated gas.
Exhaust gas containing NOx SOx dust is not discharged outside the device, and most of it is recirculated, and its retained heat is recovered and used effectively.
この発明を実施することによりSOx NOx粉じ
んの排出が起動時に少なく、流動層に排ガスと空
気の混合気体を供給し流動化するので必要空気量
は少なくてすみ、バーナを小容量にしてもその排
ガスの全量を繰返し循環させるので小容量のバー
ナで起動できるので従来のような熱ガスを供給す
る起動用熱風炉を不用にでき、排ガス保有熱量も
回収され、かつ送風機動力も少くてすむなど種々
の効果を奏するものである。 By implementing this invention, less SOx NOx dust is emitted at startup, and since a mixed gas of exhaust gas and air is supplied to the fluidized bed and fluidized, the amount of air required is small, and even if the burner has a small capacity, the exhaust gas Since the entire amount of gas is repeatedly circulated, it can be started with a small-capacity burner, making it unnecessary to use a hot-blast furnace for starting up that supplies hot gas like in the past, and the amount of heat retained in the exhaust gas is recovered. It is effective.
第１図はこの発明の実施にかかる流動層ボイラ
の配管系統図である。
１……流動層ボイラ、１２……排ガス再循環の
管路、１３……再循環フアン、１５，１５ａ……
O2メータ、１６……制御箱。
FIG. 1 is a piping system diagram of a fluidized bed boiler according to the present invention. 1...Fluidized bed boiler, 12...Exhaust gas recirculation pipe, 13...Recirculation fan, 15, 15a...
O 2 meter, 16...control box.
Claims (1)
ガスを吸引して流動層ボイラの空気室に供給しボ
イラ装置外への排ガス量を低減して粉じん、
NOx、SOxの排出絶体量を低減し、かつその排
ガス保有熱を流動媒体加熱用熱量の一部として用
い流動層の昇温を早め、また排ガス中のO2を計
測して供給する燃焼用空気と排ガスの混合気体の
含有するO2を燃焼に適する量とするように排ガ
ス再循環を制御することを特徴とする流動層ボイ
ラの起動方法。1 Simultaneously with the ignition of the startup burner, exhaust gas is sucked in by a recirculation fan and supplied to the air chamber of the fluidized bed boiler to reduce the amount of exhaust gas outside the boiler equipment and eliminate dust.
For combustion, which reduces the absolute amount of NOx and SOx emissions, uses the heat retained in the exhaust gas as part of the heat amount for heating the fluidized bed, accelerates the temperature rise of the fluidized bed, and measures and supplies O 2 in the exhaust gas. A method for starting a fluidized bed boiler, comprising controlling exhaust gas recirculation so that O 2 contained in a mixture of air and exhaust gas is in an amount suitable for combustion.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14384179A JPS5668708A (en) | 1979-11-08 | 1979-11-08 | Method of starting fluidized boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14384179A JPS5668708A (en) | 1979-11-08 | 1979-11-08 | Method of starting fluidized boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5668708A JPS5668708A (en) | 1981-06-09 |
| JPH0128286B2 true JPH0128286B2 (en) | 1989-06-01 |
Family
ID=15348186
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14384179A Granted JPS5668708A (en) | 1979-11-08 | 1979-11-08 | Method of starting fluidized boiler |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5668708A (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4442795A (en) * | 1982-04-26 | 1984-04-17 | Electrodyne Research Corporation | Recirculating fluidized bed combustion system for a steam generator |
| JPS5995332A (en) * | 1982-11-25 | 1984-06-01 | Ishikawajima Harima Heavy Ind Co Ltd | Tubular heating furnace |
| FR2537701A1 (en) * | 1982-12-08 | 1984-06-15 | Creusot Loire | METHOD AND INSTALLATION FOR RECYCLING SOLID ENDS IN A FLUIDIZED BED |
| US4462341A (en) * | 1983-01-07 | 1984-07-31 | Strohmeyer Jr Charles | Circulating fluidized bed combustion system for a steam generator with provision for staged firing |
| US4454838A (en) * | 1983-03-07 | 1984-06-19 | Electrodyne Research Corporation | Steam generator having a circulating fluidized bed and a dense pack heat exchanger for cooling the recirculated solid materials |
| JPS60142101A (en) * | 1983-12-29 | 1985-07-27 | 川崎重工業株式会社 | Operation method in case of increase of load of fluidized bed boiler |
| JPS60142102A (en) * | 1983-12-29 | 1985-07-27 | 川崎重工業株式会社 | Operation method in case of reduction of load of fluidized bed boiler |
| CN101858691A (en) * | 2010-06-07 | 2010-10-13 | 中国铝业股份有限公司 | Circulating fluidized bed boiler hot state boiler starting method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50156727A (en) * | 1974-06-11 | 1975-12-18 | ||
| JPS5390672A (en) * | 1977-01-21 | 1978-08-09 | Babcock Hitachi Kk | Sluge incinerating method by controlling atmosphere and the system therefor |
-
1979
- 1979-11-08 JP JP14384179A patent/JPS5668708A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50156727A (en) * | 1974-06-11 | 1975-12-18 | ||
| JPS5390672A (en) * | 1977-01-21 | 1978-08-09 | Babcock Hitachi Kk | Sluge incinerating method by controlling atmosphere and the system therefor |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5668708A (en) | 1981-06-09 |
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