JPS6129601A - Fluidized-bed combustion apparatus - Google Patents
Fluidized-bed combustion apparatusInfo
- Publication number
- JPS6129601A JPS6129601A JP14935084A JP14935084A JPS6129601A JP S6129601 A JPS6129601 A JP S6129601A JP 14935084 A JP14935084 A JP 14935084A JP 14935084 A JP14935084 A JP 14935084A JP S6129601 A JPS6129601 A JP S6129601A
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- fluidized
- operating
- coal
- limestone
- 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.)
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
〔発明の利用分野〕
この発明は流動層燃焼装置に係り、特に、伝熱管の腐蝕
および摩耗を防止することができる流動層燃焼ボイラに
関するもの（アル。DETAILED DESCRIPTION OF THE INVENTION [Field of Application of the Invention] The present invention relates to a fluidized bed combustion apparatus, and particularly to a fluidized bed combustion boiler that can prevent corrosion and wear of heat exchanger tubes (Al.
流動層燃焼ボイラは、熱容量が大きいために、石炭鉱山
のぼた山に野積みされている低品位炭を燃焼して、燃料
として有効に利用することができる特徴をもっている。Fluidized bed combustion boilers have a large heat capacity, so they can burn low-grade coal piled up in the heaps of coal mines and use it effectively as fuel.
流動層燃焼ボイラの流動層内に配設した伝熱管の伝熱量
（熱伝達率）は、従来形のボイラにおける燃料の燃焼カ
ス流のみから伝達される伝熱量に比べて大きく、５〜１
０倍程度程度るので、燃料を有効に利用できる流動層燃
焼ボイラは、省エネルギー化の進む近年脚光を浴びてい
る。The amount of heat transfer (heat transfer coefficient) of the heat transfer tubes arranged in the fluidized bed of a fluidized bed combustion boiler is larger than the amount of heat transferred only from the combustion residue flow of fuel in a conventional boiler, and is 5 to 1
Fluidized bed combustion boilers, which can effectively utilize fuel, have been in the spotlight in recent years as energy saving progresses.
流動層燃焼ボイラは、流動層内において、１〜１０ｒｒ
Ｖ′′の粒径の石炭を８００〜９００°Ｃの比較的低温
度域で燃焼させるものである。そして、流動媒体として
、燃料となる石炭と脱硫作用をする石灰石とメー用いて
いるので、流動層内において石炭の燃焼ガスの脱硫が容
易に行われると七もに、石炭の燃焼が８００〜９００℃
程度の比較的低温度域での燃焼であるため、窒素酸化物
の発生量が従来の微粉炭燃焼ボイラに比べて少ない。The fluidized bed combustion boiler has a combustion rate of 1 to 10 rr in the fluidized bed.
Coal having a particle size of V'' is burned at a relatively low temperature range of 800 to 900°C. Since coal as a fuel and limestone as a desulfurizing agent are used as fluidized media, desulfurization of coal combustion gas is easily carried out in the fluidized bed, and the coal combustion rate is 800 to 900%. ℃
Because the combustion occurs in a relatively low temperature range, the amount of nitrogen oxides generated is lower than that of conventional pulverized coal combustion boilers.
第３図は従来の流動層燃焼装置の概略を示す図である。FIG. 3 is a diagram schematically showing a conventional fluidized bed combustion apparatus.
第３図において、流動層燃焼ボイラ１は、空気分散板２
によって流動層３と空気室４とに仕切られ、石炭、石灰
石、燃焼灰等が混合している流動層３内に伝熱管５が配
設されている。石炭および石灰石は、燃料供給管６によ
って搬送用空気とともに、流動層燃焼ボイラ１の底部か
ら流動層３内に供給される。燃焼用空気は、空気供給管
７によって空気室４に供給され、空気分散板２の空気供
給ノズル２２を通って流動層３に供給される。In FIG. 3, a fluidized bed combustion boiler 1 includes an air distribution plate 2
The fluidized bed 3 is partitioned into a fluidized bed 3 and an air chamber 4 by a heat exchanger tube 5, and a heat transfer tube 5 is disposed within the fluidized bed 3 in which coal, limestone, combustion ash, etc. are mixed. Coal and limestone are supplied from the bottom of the fluidized bed combustion boiler 1 into the fluidized bed 3 along with conveying air by a fuel supply pipe 6 . Combustion air is supplied to the air chamber 4 by an air supply pipe 7 and is supplied to the fluidized bed 3 through an air supply nozzle 22 of the air distribution plate 2 .
燃料供給管６によって流動層３に供給される１〜１０胴
の粒径の石炭は、流動層３内における燃焼によって粒径
が徐々に小さくなり、ある粒径以下になると流動層３内
に留まることができず、石炭の燃焼排ガスとともに、流
動層３の上方の空間ｍ５すなわちフリーボード部８に排
出される。石炭の燃焼排ガスとともに流動層３からフリ
ーホード部８に排出される粒径の小さな石炭は、揮発分
力（少なく炭素分が多（て燃焼しにくいので、一部の石
炭はフリーボード部８において燃焼するが完全（こは燃
焼せず、通常１０係程度の未燃石炭が排ガス出口管９か
ら排出される。Coal having a grain size of 1 to 10 grains is supplied to the fluidized bed 3 through the fuel supply pipe 6, and its grain size gradually decreases through combustion within the fluidized bed 3, and remains within the fluidized bed 3 when it reaches a certain grain size or less. Therefore, it is discharged into the space m5 above the fluidized bed 3, that is, into the freeboard section 8 together with the coal combustion exhaust gas. Coal with a small particle size discharged from the fluidized bed 3 to the freehold section 8 together with coal combustion exhaust gas is difficult to burn due to its low volatile content (low volatile content) and high carbon content. Although it burns completely, it does not burn completely, and usually about 10 units of unburned coal is discharged from the exhaust gas outlet pipe 9.
排ガス出口管９から排出される石灰石および未燃石炭な
どは、灰捕集装置１０によって捕集さ第１、捕集灰出口
管１１を経て混合ホ・ンノク１２に供給される。Limestone, unburned coal, etc. discharged from the exhaust gas outlet pipe 9 are collected by an ash collector 10 and supplied to a mixing hole 12 via a first collected ash outlet pipe 11.
混合ホッパ１２には、石炭が石炭貯蔵ホッパ１３から石
炭供給管１４を経て、また、石灰石が石灰石貯蔵ホッパ
１５から石灰石供給管１６を経て、夫々供給されている
。そして、灰捕集装置１０によって捕集された石灰石や
未燃石炭は、上記の石炭および石灰石と共に燃料供給管
６を経て流動層燃焼ボイラ１内に戻される。灰捕集装置
１０によって石灰石および未燃石炭等が捕集されて清浄
になった燃焼排ガスは、排ガス出口管１７から大気に放
出される。Coal is supplied to the mixing hopper 12 from a coal storage hopper 13 through a coal supply pipe 14, and limestone is supplied from a limestone storage hopper 15 through a limestone supply pipe 16, respectively. The limestone and unburned coal collected by the ash collecting device 10 are returned to the fluidized bed combustion boiler 1 through the fuel supply pipe 6 together with the above-mentioned coal and limestone. The combustion exhaust gas, which is purified by collecting limestone, unburned coal, etc., by the ash collector 10, is discharged into the atmosphere from the exhaust gas outlet pipe 17.
第４図は、モデル試験装置の流動層内における各種材質
の伝熱管の摩耗試験後の外径減少量と、空気分散板から
の高さとの関係を示す図である。FIG. 4 is a diagram showing the relationship between the amount of reduction in the outer diameter of heat transfer tubes made of various materials after an abrasion test in the fluidized bed of the model test device and the height from the air distribution plate.
既に説明した第３図における燃料供給管６から搬送用空
気によって石炭および石灰石が供給されず、そして、空
気供給管７から燃焼用空気が供給されないときの流動層
すなわち静止流動層の上面１８は、空気分散板２から高
さＨ２の位置にある。また、燃料供給管６から搬送用空
気によって石炭および宕灰石が供給されており、そして
、空気供給管７から燃焼用空気が供給されているときの
流動層すなわち運転流動層は体積が増加するので、運転
流動層の上面１９は静止流動層の上面１８よりも高さＨ
。The upper surface 18 of the fluidized bed, that is, the stationary fluidized bed when coal and limestone are not supplied by conveying air from the fuel supply pipe 6 in FIG. 3 already explained, and when combustion air is not supplied from the air supply pipe 7, It is located at a height H2 from the air distribution plate 2. Further, when coal and mauvestone are supplied by conveying air from the fuel supply pipe 6 and combustion air is supplied from the air supply pipe 7, the volume of the fluidized bed, that is, the operating fluidized bed increases. Therefore, the top surface 19 of the operating fluidized bed is higher than the top surface 18 of the stationary fluidized bed by a height H.
.
だけ高い位置にある。運転流動層の上面１９と静止流動
層の上面１８との間の厚さＨ，の層はスプラッシュゾー
ン２０と、また、空気分散板２と静止流動層の上面１８
との間の厚さＨ２の層はバブルゾーン２１と、夫々呼ば
れている。ＳＴＢ、 ＳＵＳ等の各種材質の伝熱管の外
径減少量の説明は、後述の第５図および第６図の説明と
ともに行う。only in a high position. A layer of thickness H, between the top surface 19 of the operating fluidized bed and the top surface 18 of the static fluidized bed forms a splash zone 20 and also the air distribution plate 2 and the top surface 18 of the static fluidized bed.
A layer having a thickness of H2 between the two is called a bubble zone 21, respectively. The amount of reduction in the outer diameter of heat transfer tubes made of various materials such as STB and SUS will be explained together with the explanation of FIGS. 5 and 6, which will be described later.
第５図は流動層内の石炭、石灰石、空気等の状況を示す
図、第６図は流動層内の流動媒体すなわち石炭および石
灰石のかさ密度および流動速度と空気分散板からの高訴
との関係を示す図である。Figure 5 is a diagram showing the conditions of coal, limestone, air, etc. in the fluidized bed, and Figure 6 is a diagram showing the bulk density and flow velocity of the fluidized medium, that is, coal and limestone, in the fluidized bed and the high complaints from the air dispersion plate. It is a figure showing a relationship.
第５図および第６図において、空気分散板２の空気供給
ノズル２２から供給される燃焼用空気と、図示しない燃
料供給管６によって供給される石炭および石灰石を搬送
する搬送用空気とは、石炭に燃焼用酸素を供給しつつ、
石炭、石灰石、燃焼灰等を押し上げながら気泡２３とな
って、バブルゾーン２１内を上昇する。気泡２３は、バ
ブルゾーン２１内を上昇しながら合体、成長し、スプラ
ッシュゾーン２０内において瞬時に爆発的に膨張する。In FIG. 5 and FIG. 6, the combustion air supplied from the air supply nozzle 22 of the air distribution plate 2 and the conveying air for conveying coal and limestone supplied by the fuel supply pipe 6 (not shown) are while supplying combustion oxygen to
It becomes bubbles 23 while pushing up coal, limestone, combustion ash, etc., and rises in the bubble zone 21. The bubbles 23 coalesce and grow while rising within the bubble zone 21, and instantly expand explosively within the splash zone 20.
したがって、バブルゾーン２１内の流動媒体すなわち石
炭および石灰石のかさ密度は、点線２５′で示すように
一定であるが、スプラッシュゾーン２０内の流動媒体す
なわち石炭および石灰石のかさ密度は、点線２５で示す
ように静止流動層の上面１８から運転流動層の上面１９
に向って低下する。また、バブルゾーン２１内の流動媒
体すなわち石炭および石灰石の流動速度は、実線２４′
で示すように低くて一定であるが、スプラッシュゾーン
２０内の流動媒体すなわち石炭および石灰石の流動速度
は、実線２４で示すように静止流動層の上面１８から運
転流動層の上面１９に向って急激に上昇する。Therefore, the bulk density of the flowing medium, i.e. coal and limestone, in the bubble zone 21 is constant, as indicated by the dotted line 25', whereas the bulk density of the flowing medium, i.e. coal and limestone, in the splash zone 20, is indicated by the dotted line 25'. from the top surface 18 of the stationary fluidized bed to the top surface 19 of the operating fluidized bed.
decreases towards Further, the flow velocity of the fluid medium, that is, coal and limestone in the bubble zone 21 is represented by the solid line 24'
Although the flow rate of the fluidized media, namely coal and limestone, in the splash zone 20 is low and constant as shown by , the flow velocity of the fluidized media, namely coal and limestone, in the splash zone 20 suddenly increases from the top surface 18 of the stationary fluidized bed to the top surface 19 of the operating fluidized bed, as shown by the solid line 24. rise to
バブルゾーン２１内の流動媒体すなわち石炭および石灰
石の実線２４′で示す流動速度と、スプラッシュゾーン
２０内の流動媒体すなわち石炭および石灰石の実線２４
で示す流動速度との相違によって、バブルゾーン２１内
の図示しない伝熱管の摩耗による外径減少量と、スプラ
ッシュゾーン２０内の図示−しない伝熱管の摩耗による
外径減少量とが相違して（る。すなわち、第４図におい
て、スプラッシュゾーン２０内では、流動媒体すなわち
石炭お崖び石灰石の流動速度は第６図の実線２４で示す
ように急激に上昇するので、ＳＴＢ、ＳＵＳ等の耐蝕性
を有する材質の伝熱管であっても摩耗による外径減少量
は多いが、バブルゾーン２１内では、流動媒体すなわち
石炭および石灰石の流動速度は第６図の実線２４′で示
すように低いので、ＳＴＢ、ＳＵＳ等の耐蝕性を有する
伝熱管の摩耗による外径減少量は少ない。The flow velocity shown by the solid line 24' for the fluidized media, coal and limestone, in the bubble zone 21 and the solid line 24 for the fluidized media, coal and limestone in the splash zone 20.
Due to the difference from the flow velocity shown in ( In other words, in the splash zone 20 in FIG. 4, the flow rate of the fluid medium, that is, coal, limestone, etc., increases rapidly as shown by the solid line 24 in FIG. Even if the heat exchanger tube is made of a material with The amount of decrease in outer diameter due to wear of corrosion-resistant heat transfer tubes such as STB and SUS is small.
また、空気分散板２の空気供給ノズル２２から供給され
る燃焼用空気中の酸素は、流動層３内での石炭の燃焼に
よって徐々に消費されるため、流動層３内の高さ方向の
酸素濃度は、流動層３の底部ちなわち空気分散板２の近
傍では高く、流動層３の頂部すなわちスプラッシュゾー
ン２０では低い。In addition, since the oxygen in the combustion air supplied from the air supply nozzle 22 of the air distribution plate 2 is gradually consumed by the combustion of coal within the fluidized bed 3, the oxygen in the height direction within the fluidized bed 3 is The concentration is high at the bottom of the fluidized bed 3, ie near the air distribution plate 2, and low at the top of the fluidized bed 3, ie the splash zone 20.
したがって、スプラッシュゾーン２０内に伝熱管を配設
した場合、伝熱管は、流動速度の速い高温の流動媒体す
なわち石炭および石灰石と接触するととによって摩耗す
るとともに、流動層３内全体が石炭中の硫黄分によって
還元雰囲気であることと、特に、スプラッシュゾーン２
０内は酸素濃度が低いことによって還元雰囲気であるこ
ととか加わって、摩耗が加速されるので従来から問題と
なっていた。Therefore, when a heat exchanger tube is disposed in the splash zone 20, the heat exchanger tube is worn out when it comes into contact with a high-temperature fluid medium having a high flow rate, that is, coal and limestone, and the entire inside of the fluidized bed 3 is covered with sulfur contained in the coal. Particularly in the splash zone 2, which is a reducing atmosphere by the minute.
This has been a problem in the past since wear is accelerated in the 0 zone due to the low oxygen concentration, which creates a reducing atmosphere.
この発明は、上記の問題を解決するためになされたもの
で、流動層燃焼ボイラの流動層のスプラッシュゾーンに
おける伝熱管の摩耗を無くすことのできる流動層燃焼装
置を提供することを目的とするものである。This invention was made in order to solve the above-mentioned problem, and an object thereof is to provide a fluidized bed combustion apparatus that can eliminate wear of heat transfer tubes in the splash zone of the fluidized bed of a fluidized bed combustion boiler. It is.
この発明は、流動層燃焼ボイラの流動層のスプラソンユ
ゾーン内以外の部分、すなわち、バブルゾーン内および
流動層の上部のフリーボード部内に伝熱管を配設する。According to the present invention, heat transfer tubes are disposed in a portion of the fluidized bed of a fluidized bed combustion boiler other than the spratly zone, that is, in the bubble zone and in the freeboard portion above the fluidized bed.
そして、流動層底部とフリーボード部とに圧力計を設け
て、これら２個の圧力計の圧力の差圧に曖よってスプラ
ッンユゾーンの位置を検出し、流動層底部から流動媒体
！なわち石炭および石灰石を抽出したり、あるいは、流
動一層上部から流動媒体すなわち石炭および石灰石を補
給したりして、スプラッシュゾーンの位置を制御するこ
とにより、スプラッシュゾーンが上昇あるいは下降′し
てバブルゾーン内およびフリーホード部内に配設した伝
熱管に到達しないようにすることを特徴とするものであ
る。Then, pressure gauges are installed at the bottom of the fluidized bed and the freeboard section, and the position of the spatter zone is detected based on the difference in pressure between these two pressure gauges, and the fluidized medium is removed from the bottom of the fluidized bed. By controlling the position of the splash zone by extracting coal and limestone or by replenishing the fluidized medium, i.e. coal and limestone, from the top of the fluidized layer, the splash zone can be raised or lowered to create a bubble zone. It is characterized by preventing the heat transfer tubes from reaching the heat exchanger tubes disposed inside the inner and freehold parts.
この発明に係る実施例を図に基づいて説明する。 Embodiments of the invention will be described based on the drawings.
第１図はこの発明の流動層燃焼ボイラの概略構造を示す
図、第２図はこの発明の流動層燃焼ボイラの流動層の底
部とフリーボード部との差圧と、流動層の上面の高さと
の関係を示す図である。Figure 1 shows the schematic structure of the fluidized bed combustion boiler of the present invention, and Figure 2 shows the differential pressure between the bottom of the fluidized bed and the freeboard section of the fluidized bed combustion boiler of the present invention, and the height of the top surface of the fluidized bed. FIG.
第１図番こおいて、伝熱管群２９ａが流動層燃焼ボイラ
１のフリーボード部８内に、また、伝熱管群２９ｂが流
動層燃焼ボイラ１の流動層３のバブルゾーン２１内に、
夫々配設されており、スプラッシュ流動層３内において
スプラッシュゾーンｉｏが空気分散板２の上方のどの位
置にくるかによって決定される。スプラッシュゾーン２
０の位置は、流動層燃焼ボイラ１を設計する際、燃料供
給管６によって石炭と石灰石とを搬送する搬送用空気お
よび空気供給管７から供給される燃焼用空気等の供給空
気量から決定することができる。（Ｒｅｆ ； Ｓ、
Ｐ。In Figure 1, the heat transfer tube group 29a is placed in the freeboard section 8 of the fluidized bed combustion boiler 1, and the heat transfer tube group 29b is placed in the bubble zone 21 of the fluidized bed 3 of the fluidized bed combustion boiler 1.
The splash zone io is determined by the position above the air distribution plate 2 in the splash fluidized bed 3. splash zone 2
The position of 0 is determined when designing the fluidized bed combustion boiler 1 based on the amount of air to be supplied such as the conveying air for conveying coal and limestone through the fuel supply pipe 6 and the combustion air supplied from the air supply pipe 7. be able to. (Ref; S,
P.
Ｂａｂｕ他２． ＡＩＣｈＥ’ＳＹＭＰＯ３ＩＵＭ ５
ＥＲＩＥＳＮｏ、 １７６、’７４．１７６〜１８６．
１９７８ ）スプラッシュゾーン２０の厚さＨ，は、通
常、バブルゾーン２１の厚さＨ２の０．２倍以上の厚さ
であるので、伝熱管群２９ａと伝熱管群２９ｂとの間隔
Ｈもバブルゾーン２１の厚さＨ２の０２倍以上の間隔ニ
しである。既に説明した第４図において、スプラッシュ
ゾーン２０の厚さＨｌはバブルゾーン２１の厚すＨ２の
０．３倍の厚さであり、スプラッシュゾーン２０の頂部
すなわち運転流動層の上面１９の近傍では、伝熱管の外
径減少量が急激に減少している。Babu et al. 2. AIChE'SYMPO3IUM 5
ERIES No. 176, '74.176-186.
1978) Since the thickness H of the splash zone 20 is usually 0.2 times or more the thickness H2 of the bubble zone 21, the distance H between the heat exchanger tube group 29a and the heat exchanger tube group 29b is also equal to the bubble zone. The distance is 02 times or more the thickness H2 of 21. In FIG. 4 already explained, the thickness Hl of the splash zone 20 is 0.3 times the thickness H2 of the bubble zone 21, and at the top of the splash zone 20, that is, near the upper surface 19 of the operating fluidized bed, The amount of reduction in the outer diameter of the heat exchanger tube is rapidly decreasing.
空気分散板２の近傍には、流動層燃焼ボイラｌの運転中
にスプラッシュゾーン２０の位置を下降させるために、
流動媒体すなわち石炭および石灰石を抽出する流動媒体
抽出管２６が配設されている。In the vicinity of the air distribution plate 2, in order to lower the position of the splash zone 20 during operation of the fluidized bed combustion boiler l,
A fluidized media extraction tube 26 is provided for extracting fluidized media, namely coal and limestone.
また、流動層燃焼ボイラ１の運転中にスプラッシュゾー
ン２０の位置を上イ昇させるために、フリーボード部８
から流動媒体すなわち石炭および石灰石を補給する流動
媒体貯蔵ホ・ツバ２８が配設されている。In addition, in order to raise the position of the splash zone 20 during operation of the fluidized bed combustion boiler 1, the freeboard section 8
A fluidized media storage tank 28 is provided for replenishing fluidized media, namely coal and limestone.
スプラッシュマ゛−ン２０の位置すなわち運転流動層の
上面１９の高さを検出するために、圧力計３０２がフリ
ーボード部８に、また、圧力計３０ｂが空気分散板２の
直上部に、夫々設けられており、圧力計３０ａの指示圧
力と圧力計３０ｂの指示圧力との差圧ΔＰ１〜ΔＰ３を
用いて、第２図に示す関係によって、運転流動層の上面
１９の高さり、−ｈ３を算出する流動層上面高演算装置
３１が設けられている。In order to detect the position of the splash man 20, that is, the height of the upper surface 19 of the operating fluidized bed, a pressure gauge 302 is installed in the freeboard section 8, and a pressure gauge 30b is installed directly above the air distribution plate 2, respectively. The height of the upper surface 19 of the operating fluidized bed, -h3, is determined by the relationship shown in FIG. A fluidized bed top surface height calculation device 31 is provided to calculate the fluidized bed top surface height.
流動層上面高演算装置３１によって算出される運転流動
層の上面１９の高さは、予め定められた高さになるよう
に流動層上面高制御装置３２によって制御される。すな
わち、流動層上面高演算装置３１によって算出される運
転流動層の上面１９の高さが予め定められた高さより低
い場合、流動層上面高制御装置３２によって、燃料供給
管６あるいは流動媒体貯蔵ホッパ２８から流動媒体すな
わち石炭および石灰石が供給され、運転流動層の上面１
９の高さは予め定められた高さまで上昇する。逆に、運
転流動層の上面１９の高さが予め定められた高さより高
い場合、流動層上面高制御装置３２によって、流動媒体
抽出管２６から流動媒体すなわち石炭および石灰石が抽
出され、あるいは、燃料供給管６によっ゛ て供給
される石炭および石灰石の供給量が減少させられ、また
は、空気供給管７によって供給される燃焼用空気の供給
量が減少させられて、運転流動層の上面１９の高さは予
め定められた高さまで下降する。The height of the top surface 19 of the operating fluidized bed calculated by the fluidized bed top surface height calculation device 31 is controlled by the fluidized bed top surface height control device 32 so that it becomes a predetermined height. That is, when the height of the top surface 19 of the operating fluidized bed calculated by the fluidized bed top surface height calculation device 31 is lower than a predetermined height, the fluidized bed top surface height control device 32 controls the fuel supply pipe 6 or the fluidized medium storage hopper. From 28 fluidized media, i.e. coal and limestone, are supplied from the upper surface 1 of the working fluidized bed.
The height of 9 rises to a predetermined height. Conversely, when the height of the top surface 19 of the operating fluidized bed is higher than the predetermined height, the fluidized bed top height control device 32 extracts the fluidized medium, ie, coal and limestone, from the fluidized medium extraction pipe 26, or extracts the fuel The supply of coal and limestone supplied by the supply pipe 6 is reduced, or the supply of combustion air supplied by the air supply pipe 7 is reduced, so that the upper surface 19 of the operating fluidized bed is reduced. The height is lowered to a predetermined height.
流動層上面高制御装置３２によって運転流動層の上面１
９の高さを予め定められた高さに制御する場合、流動層
上面高制御装置３２と流動媒体抽出弁２７ａ、流動媒体
補給弁２７ｂ、燃料供給弁２７Ｃ１燃焼用空気供給弁２
７ｄとを連結して自動的に制御することができるが、流
動層上面高制御装置３２から警報を出して流動媒体抽出
弁２７ａ、流動媒体補給弁２７ｂ、燃料供給弁２７Ｃ１
燃焼用空気供給弁２７ｄを手−動で制御することもでき
る。The upper surface 1 of the fluidized bed is operated by the fluidized bed upper surface height controller 32.
9 to a predetermined height, the fluidized bed top surface height control device 32, the fluidized medium extraction valve 27a, the fluidized medium replenishment valve 27b, the fuel supply valve 27C1, the combustion air supply valve 2
7d and can be automatically controlled by issuing an alarm from the fluidized bed top surface height control device 32 to control the fluidic medium extraction valve 27a, fluidic medium replenishment valve 27b, and fuel supply valve 27C1.
The combustion air supply valve 27d can also be controlled manually.
なお、伝熱管群２９ａが流動層燃焼ボイラ１のフリーボ
ード部８（ζ、また、伝熱管群２９ｂが流動層燃焼ボイ
ラｌの流動層３のバブルゾーン２１内に、夫々設けられ
ていると説明したが、流動層燃焼ボイラｌの負荷の容量
によっては、伝熱管群２９ａをフリーボード部８に設け
るだけにするか、または、伝熱管群２９ｂをバブルゾー
ン２１内に設けるだけにするか、何れでもよい。Note that the heat transfer tube group 29a is provided in the freeboard section 8 (ζ) of the fluidized bed combustion boiler 1, and the heat transfer tube group 29b is provided in the bubble zone 21 of the fluidized bed 3 of the fluidized bed combustion boiler l. However, depending on the load capacity of the fluidized bed combustion boiler l, the heat transfer tube group 29a may be provided only in the freeboard section 8, or the heat transfer tube group 29b may be provided only within the bubble zone 21. But that's fine.
さらに、伝熱管群２９ａおよび伝熱管２９ｂの伝熱管の
配列は、縦型、横型、傾斜型の何れであっても、流動層
３内の流動媒体すなわち石炭および石灰石による摩耗は
同等である。Further, regardless of whether the heat exchanger tubes of the heat exchanger tube group 29a and the heat exchanger tubes 29b are arranged vertically, horizontally, or inclined, wear caused by the fluidized medium in the fluidized bed 3, that is, coal and limestone, is the same.
また、運転流動層の上面１９の高さを検出するために、
フリーホード部８と空気分散板２の直上部との２個所に
圧力計を設けると説明したが、圧力計を３個所以上に設
ければ、運転流動層の上面１９の高さの検出精度はさら
に向上する。Moreover, in order to detect the height of the upper surface 19 of the operating fluidized bed,
Although it has been explained that pressure gauges are provided at two locations, the freehold section 8 and directly above the air distribution plate 2, if pressure gauges are provided at three or more locations, the detection accuracy of the height of the upper surface 19 of the operating fluidized bed will be improved. Further improvement.
５発明の効果〕
この発明は、以上説明したように、スプラッンュゾーン
内以外の部分、すなわち、バブルゾーン内およびフリー
ボード部内に伝熱管を配設している。そして、スプラッ
ンユゾーンが上昇または下降して伝熱管に到達しないよ
うにスプラッシュゾーンの位置を制御している。したが
って、伝熱管が、スプラッシュゾーン内の流動速度の速
い高温の流動媒体すなわち石炭および石灰石と接触しな
いので、摩耗しない効果がある。また、スプラッンユゾ
ーンの還元雰囲気によって摩耗が加速されない効果があ
る。5. Effects of the Invention] As explained above, in the present invention, heat transfer tubes are disposed in a portion other than the splatter zone, that is, the bubble zone and the freeboard portion. The position of the splash zone is controlled so that the splash zone does not rise or fall and reach the heat transfer tubes. Therefore, the heat exchanger tubes do not come into contact with the high-temperature fluidized medium with a high flow rate in the splash zone, ie, coal and limestone, so there is an effect of preventing wear. In addition, there is an effect that wear is not accelerated by the reducing atmosphere in the splash zone.
第１図はこの発明の流動層燃焼ボイラの概略構造を示す
図、第２図はこの発明の流動層燃焼ボイラの流動層の底
部とフリーボード部との差圧と、流動層の上面の高さと
の関係を示す図、第３図は従来の流動層燃焼装置の概略
を示す図、第４図は、モデル試験装置の流動層内におけ
る各種材質の伝熱管の摩耗試験後の外径減少量と、空気
分散板がらの高さとの関係を示す図、第５図は流動層内
の石炭、石灰石、空気等の状況を示す図、第６図は流動
層内の流動媒体すなわち石炭および石灰石のかさ密度お
よび流動速度と空気分散板からの高さとの関係を示す図
である。
１・・流動層燃焼ボイラ ２・・・空気分散板３・・・
流動層 ４・・・空気室５・・・伝熱管
６・・燃料供給管７・・・空気供給管 ８・
・・フリーボード部９・・・排ガス出口管 １０・・
・灰捕集装置１１・・捕集灰出口管 １２・・・混合
ホッパ１３・・石炭貯蔵ホッパ １４・・・石炭供給管
１５・・・石灰石貯蔵ホッパ１６・・・石灰石供給管１
７・・排カス出口管 ］８・・静止流動層上面１９・
・運転流動層上面
２０・・・スプラッンユゾーン
２１・・バブルゾーン ２２・・・空気供給ノズル２
３・・気泡 ２４・・・流動速度２５・・・
かさ密度 ２６・・・抽出管２７ａ 〜２７ｄ
−・弁
２８・・流動媒体貯蔵ホッパFigure 1 shows the schematic structure of the fluidized bed combustion boiler of the present invention, and Figure 2 shows the differential pressure between the bottom of the fluidized bed and the freeboard section of the fluidized bed combustion boiler of the present invention, and the height of the top surface of the fluidized bed. Figure 3 is a diagram showing the outline of a conventional fluidized bed combustion apparatus, Figure 4 is a diagram showing the amount of outer diameter reduction after wear tests of heat transfer tubes made of various materials in the fluidized bed of a model test equipment. Figure 5 is a diagram showing the relationship between the height of the air distribution plate and the height of the air distribution plate, Figure 5 is a diagram showing the situation of coal, limestone, air, etc. in the fluidized bed, and Figure 6 is a diagram showing the relationship between the fluidized medium in the fluidized bed, that is, coal and limestone. FIG. 3 is a diagram showing the relationship between the density and flow velocity and the height from the air distribution plate. 1...Fluidized bed combustion boiler 2...Air distribution plate 3...
Fluidized bed 4...Air chamber 5...Heat transfer tube
6.Fuel supply pipe 7.Air supply pipe 8.
...Freeboard part 9...Exhaust gas outlet pipe 10...
-Ash collection device 11...Collected ash outlet pipe 12...Mixing hopper 13...Coal storage hopper 14...Coal supply pipe 15...Limestone storage hopper 16...Limestone supply pipe 1
7. Exhaust waste outlet pipe] 8. Stationary fluidized bed top surface 19.
・Operating fluidized bed upper surface 20... Splash zone 21... Bubble zone 22... Air supply nozzle 2
3... Air bubbles 24... Flow rate 25...
Bulk density 26...Extraction tubes 27a to 27d
-・Valve 28・・Fluid medium storage hopper
Claims (4)
層内の燃料の燃焼熱量を伝達する流動層燃焼装置におい
て、前記流動層内の燃料を燃焼していないときの静止流
動層内と、前記流動層内の燃料を燃焼しているときの運
転流動層の上部の空間部分とに、夫々前記伝熱管を配設
することを特徴とする流動層燃焼装置。(1) In a fluidized bed combustion apparatus that transfers the amount of combustion heat of fuel in the fluidized bed to a fluid in a heat transfer tube arranged in the fluidized bed, static flow occurs when the fuel in the fluidized bed is not being combusted. A fluidized bed combustion apparatus characterized in that the heat transfer tubes are disposed within the bed and in a space above the operating fluidized bed when fuel in the fluidized bed is being combusted.
運転流動層の上部の空間部分に配設する前記伝熱管との
間の距離は、前記静止流動層の鉛直方向の厚さの０．２
倍以上の距離であることを特徴とする特許請求の範囲第
１項記載の流動層燃焼装置。(2) The distance between the heat transfer tubes disposed in the stationary fluidized bed and the heat transfer tubes disposed in the upper space of the operating fluidized bed is equal to the vertical thickness of the stationary fluidized bed. 0.2 of
The fluidized bed combustion apparatus according to claim 1, wherein the distance is at least twice as long.
の上部の前記空間部分との２個所に圧力計を設け、前記
２個所に設けた前記圧力計の指示圧力の差圧によって、
前記運転流動層の上面の高さを検出することを特徴とす
る特許請求の範囲第１項記載の流動層燃焼装置。(3) Pressure gauges are provided at least at two locations, the bottom of the operating fluidized bed and the space above the operating fluidized bed, and the pressure difference between the indicated pressures of the pressure gauges provided at the two locations is used to
The fluidized bed combustion apparatus according to claim 1, wherein the height of the upper surface of the operating fluidized bed is detected.
の流動媒体を抽出する流動媒体抽出管と、前記運転流動
層の上部の前記空間部分から前記運転流動層の流動媒体
を補給する流動媒体貯蔵ホッパとを設け、前記運転流動
層の上面の高さが予め定められた高さになるように、前
記運転流動層の上面の上昇および下降を制御することを
特徴とする特許請求の範囲第１項記載の流動層燃焼装置
。(4) A fluidized medium extraction pipe that extracts the fluidized medium in the operating fluidized bed from the bottom of the operating fluidized bed, and a fluidized medium that replenishes the fluidized medium of the operating fluidized bed from the space above the operating fluidized bed. A medium storage hopper is provided, and the raising and lowering of the upper surface of the operating fluidized bed is controlled so that the height of the upper surface of the operating fluidized bed becomes a predetermined height. The fluidized bed combustion apparatus according to item 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14935084A JPS6129601A (en) | 1984-07-20 | 1984-07-20 | Fluidized-bed combustion apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14935084A JPS6129601A (en) | 1984-07-20 | 1984-07-20 | Fluidized-bed combustion apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6129601A true JPS6129601A (en) | 1986-02-10 |
Family
ID=15473199
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14935084A Pending JPS6129601A (en) | 1984-07-20 | 1984-07-20 | Fluidized-bed combustion apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6129601A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61173011A (en) * | 1985-01-28 | 1986-08-04 | Babcock Hitachi Kk | Fluidized bed combustion equipment |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5512336A (en) * | 1978-07-10 | 1980-01-28 | Mitsubishi Heavy Ind Ltd | Fluid bed boiler |
| JPS57192713A (en) * | 1981-04-09 | 1982-11-26 | Foster Wheeler Corp | Fluid bed type heat exchanger with controller for responding change of quantity required |
| JPS5824710A (en) * | 1981-08-05 | 1983-02-14 | Kawasaki Heavy Ind Ltd | Height control of static bed of fluidized medium in boiler of fluidized-bed combustion type |
-
1984
- 1984-07-20 JP JP14935084A patent/JPS6129601A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5512336A (en) * | 1978-07-10 | 1980-01-28 | Mitsubishi Heavy Ind Ltd | Fluid bed boiler |
| JPS57192713A (en) * | 1981-04-09 | 1982-11-26 | Foster Wheeler Corp | Fluid bed type heat exchanger with controller for responding change of quantity required |
| JPS5824710A (en) * | 1981-08-05 | 1983-02-14 | Kawasaki Heavy Ind Ltd | Height control of static bed of fluidized medium in boiler of fluidized-bed combustion type |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61173011A (en) * | 1985-01-28 | 1986-08-04 | Babcock Hitachi Kk | Fluidized bed combustion equipment |
| JPH0522806B2 (en) * | 1985-01-28 | 1993-03-30 | Babcock Hitachi Kk |
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