JPS6341706A - Fluidized bed burning method - Google Patents
Fluidized bed burning methodInfo
- Publication number
- JPS6341706A JPS6341706A JP18598886A JP18598886A JPS6341706A JP S6341706 A JPS6341706 A JP S6341706A JP 18598886 A JP18598886 A JP 18598886A JP 18598886 A JP18598886 A JP 18598886A JP S6341706 A JPS6341706 A JP S6341706A
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- dead
- burnt
- temperature
- quick lime
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims description 9
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000000292 calcium oxide Substances 0.000 claims abstract description 28
- 235000012255 calcium oxide Nutrition 0.000 claims abstract description 28
- 239000003245 coal Substances 0.000 claims abstract description 15
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 13
- 230000023556 desulfurization Effects 0.000 claims abstract description 13
- 238000002485 combustion reaction Methods 0.000 claims abstract description 12
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 claims abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 239000000126 substance Substances 0.000 claims abstract description 4
- 238000009841 combustion method Methods 0.000 claims description 7
- 239000000571 coke Substances 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 30
- 239000004576 sand Substances 0.000 abstract description 10
- 239000000377 silicon dioxide Substances 0.000 abstract description 10
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract description 7
- 238000012546 transfer Methods 0.000 abstract description 7
- 239000012530 fluid Substances 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 235000019738 Limestone Nutrition 0.000 description 6
- 239000006028 limestone Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000010883 coal ash Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、流動層で石炭、オイルコークスなどの燃料（
以下、単に石炭という）を燃焼せしめて、運気を取り出
すようにした流動層燃焼ボイラの新規な燃焼方法、詳し
くは、粉化全敗が少なく、珪砂やアルミナよりも硬度が
小さい死焼した生石灰などの死焼したアルカリ土類金属
酸化物を流動物質とし、かつ実質的に脱硫反応を起こさ
ない高い温度の流動層で石炭を高い燃焼効率で燃焼する
方法に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention provides a method for producing fuels such as coal and oil coke in a fluidized bed.
A new combustion method for a fluidized bed combustion boiler that extracts good luck by burning coal (hereinafter simply referred to as coal).In detail, it uses dead-burned quicklime, which is less likely to be pulverized and has a lower hardness than silica sand or alumina. The present invention relates to a method of burning coal with high combustion efficiency in a high-temperature fluidized bed in which dead-burned alkaline earth metal oxide is used as a fluid material and substantially no desulfurization reaction occurs.
従来の流動層燃焼ボイラにおいては、炉内に石灰石を供
給して石炭中のイオウ分と反応せしめる、いわゆる炉内
脱硫を実施する場合が多い、脱硫には、８００〜９００
℃の範囲に最適温度があることもあって、炉内脱硫を実
施する場合には、９００℃よりも高い流動層温度は採用
されていない。In conventional fluidized bed combustion boilers, so-called in-furnace desulfurization is often carried out by supplying limestone into the furnace and reacting with the sulfur content in the coal.
Since there is an optimum temperature in the range of .degree. C., a fluidized bed temperature higher than 900.degree. C. is not used when performing in-furnace desulfurization.
このように、８００〜９００℃の低い流動層温度のため
に、燃焼効率が悪くなる。このため、未燃石炭を含む飛
散ダストを捕集して流動層に戻すＷｉ環方式を採用する
か、あるいは別に設けた再燃焼炉で燃焼する方法のいず
れかが採用されている。Thus, due to the low fluidized bed temperature of 800-900°C, the combustion efficiency becomes poor. For this reason, either a Wi-ring method is adopted in which scattered dust containing unburned coal is collected and returned to the fluidized bed, or a method in which the coal is combusted in a separately provided reburning furnace is adopted.
しかしながら、上記の従来の方法はいずれもシステムが
複雑で、設備費も高く、また運転操作も複流になるとい
う問題点を有している。However, all of the above conventional methods have problems in that the system is complicated, the equipment cost is high, and the operation requires double flow.
一方、高い燃焼効率を得るためには、流動層温度として
９００℃以上、好ましくは９５０℃以上が必要である。On the other hand, in order to obtain high combustion efficiency, the fluidized bed temperature needs to be 900°C or higher, preferably 950°C or higher.
この温度で使用できる流動物質として、珪砂（Ｓｉｎｇ
）、アルミナ（ＡｌｚＯｓ）などがあるが、珪砂のモー
ス硬度は６〜７、アルミナのモース硬度は１２と高＜、
流動層内の伝熱管の摩耗が大きく、これらは使用に適さ
ない。Silica sand (Sing) is a fluid material that can be used at this temperature.
), alumina (AlzOs), etc., but the Mohs hardness of silica sand is 6 to 7, and the Mohs hardness of alumina is as high as 12.
The heat exchanger tubes in the fluidized bed are severely worn out, making them unsuitable for use.
石灰石はモース硬度３と低く、伝熱管の摩耗は珪砂など
に比べて大幅に少ない。しかし石灰石は、流動層内で分
解してＣａＯになることもあって、粉化飛散性が大きく
、流動物質として使用するためには、大量供給する必要
があり、石炭供給量の数９ｉ〜１０数％も供給しなけれ
ばならず経済的でない。Limestone has a low Mohs hardness of 3, and the wear of heat transfer tubes is significantly less than that of silica sand. However, limestone can decompose into CaO in the fluidized bed, and has a high tendency to powder and scatter.In order to use it as a fluid material, it must be supplied in large quantities, which is approximately 9i to 10 times the amount of coal supplied. It is not economical to supply even several percent.
本発明者らは上記の問題点を解決すべく、鋭意研究を重
ねた結果、珪砂、アルミナよりも硬度が低（、それ自体
も粉化飛散し難い物質として、死焼生石灰などの死焼し
たアルカリ土類金属酸化物が流動物質として最適である
ことを見出した。In order to solve the above problems, the present inventors conducted extensive research and found that the hardness of silica sand and alumina is lower than that of silica sand and alumina. We have found that alkaline earth metal oxides are optimal as fluid materials.
本発明は上記の諸点に鑑みなされたもので、流動物質と
して死焼したアルカリ土類金属酸化物を用い、流動層ｌ
’７４度を高温に維持して、高い燃焼効率を得るように
した流動層燃焼方法の提供を目的とするものである。The present invention was made in view of the above points, and uses a dead-burned alkaline earth metal oxide as a fluid material, and uses a fluidized bed.
The object of the present invention is to provide a fluidized bed combustion method that maintains a high temperature of 74 degrees Celsius and obtains high combustion efficiency.
〔問題点を解決するための手段および作用〕本発明の流
動層燃焼方法は、流動層内に伝熱管を有する流動層で、
石炭、オイルコークスなどの燃料を燃焼する方法におい
て、流動物質として死焼したアルカリ土類金属酸化物を
供給し、流動層温度を死焼したアルカリ土類金属酸化物
が実質的に脱硫反応を起こさない９００℃以上にするこ
とを特徴としている。[Means and effects for solving the problems] The fluidized bed combustion method of the present invention uses a fluidized bed having heat transfer tubes in the fluidized bed,
In a method of burning fuel such as coal or oil coke, dead-burned alkaline earth metal oxide is supplied as a fluidized material, and the temperature of the fluidized bed is raised so that the dead-burned alkaline earth metal oxide does not substantially cause a desulfurization reaction. It is characterized by being heated to over 900°C.
石灰石は、分解に際してＣＯ２を放出するので、生成し
たＣａＯの結晶が細かく、比表面積および空隙率が大き
く、嵩比重が小さく、反応性が大きいなどの性質を有し
ている。このような状態の石灰石を軽焼生石灰と呼んで
いる。しかしながら、この軽焼生石灰は強度が弱く、流
動物質として使用すると、粉化飛散が多いため大量供給
が必要となり、灰量も多くなり経済的でない。Limestone releases CO2 when it decomposes, so the CaO produced has properties such as fine crystals, large specific surface area and porosity, small bulk specific gravity, and high reactivity. Limestone in this state is called lightly calcined quicklime. However, this lightly calcined quicklime has low strength, and when used as a fluid substance, it is often powdered and scattered, so a large amount of supply is required, and the amount of ash increases, making it uneconomical.
軽焼生石灰を高温で長時間焼成すると、細かい結晶は次
第に癒合し、全体の容積が収縮してくる。When lightly calcined quicklime is fired at high temperatures for a long period of time, the fine crystals gradually coalesce and the overall volume shrinks.
このような状態の生石灰を一般に死焼生石灰あるいは硬
焼生石灰と呼んでいる。死焼生石灰は軽焼生石灰に比べ
て、粉化飛散性が非常に少ない、しかし死焼生石灰も若
干の反応性を有しており、８００〜９００℃の流動層温
度では、脱硫反応が起こり、表面にＣａ５Ｏａを生成す
る０表面に生成したＣａ５Ｏａは柔かく次第に粉化飛散
し、繰り返しＣａＳＯ４の生成と粉化飛散が生じ、死焼
生石灰の補給が必要となる。Quicklime in this state is generally called dead-burned quicklime or hard-burned quicklime. Dead-burned quicklime has a very low pulverization and scattering property compared to light-burned quicklime, but dead-burned quicklime also has some reactivity, and at a fluidized bed temperature of 800 to 900°C, a desulfurization reaction occurs. Ca5Oa is generated on the surface. The Ca5Oa generated on the surface becomes soft and gradually powders and scatters, and CaSO4 is repeatedly produced and powders and scatters, necessitating replenishment of dead burnt lime.
このため本発明の方法においては、流動層温度を９００
℃以上、好ましくは９５０℃以上とし、実質的に脱硫反
応が起こらない温度にすることによって、死焼生石灰の
補給量を少なくする。このため、必要に応じて通常の排
ガス脱硫設備を設ける。Therefore, in the method of the present invention, the fluidized bed temperature is set to 900°C.
℃ or higher, preferably 950℃ or higher, at which the desulfurization reaction does not substantially occur, thereby reducing the amount of dead burnt lime to be replenished. For this reason, ordinary flue gas desulfurization equipment will be provided as necessary.
燃焼効率を高めるためには、可能な限り高い温度とする
のが好ましいが、最高温度は使用する石炭灰の軟化温度
で制限される。石炭灰の軟化温度は、−船釣に酸化雰囲
気に比べて、還元雰囲気では概略１００℃低くなるため
、単段燃焼として流動層内を酸化雰囲気にするのが好ま
しい。In order to increase combustion efficiency, it is preferable to set the temperature as high as possible, but the maximum temperature is limited by the softening temperature of the coal ash used. The softening temperature of coal ash is approximately 100° C. lower in a reducing atmosphere than in an oxidizing atmosphere, so it is preferable to use an oxidizing atmosphere in the fluidized bed as a single-stage combustion.
本発明の方法においては、死焼した生石灰の代りに、Ｍ
ｇ、Ｂａなどの他のアルカリ土類金属の化合物を死焼し
て得た酸化物、たとえば死焼ドロマイト、マグネシャク
リンカ−などを使用することができる。In the method of the present invention, M
It is possible to use oxides obtained by dead-burning compounds of other alkaline earth metals such as G, Ba, etc., such as dead-burning dolomite and magnesha clinker.
以下、図面を参照して、本発明の好適な実施例を例示的
に説明する。ただしこの実施例に記載されている構成機
器の形状、相対配置などは、と（に特定的な記載がない
限りは、本発明の範囲をそれらのみに限定する趣旨のも
のではな（、単なる説明例にすぎない。１は流動層炉で
、下部に風箱２を有し、この風箱２の上側に空気分散板
３を介して流動層４を有し、この流動層４の上側にフリ
ーボード５を有している。流動層４内には伝熱管６が設
けられ、石炭供給ロアから石炭を投入して燃焼させる。Hereinafter, preferred embodiments of the present invention will be exemplarily described with reference to the drawings. However, the shapes, relative arrangements, etc. of the components described in this example are not intended to limit the scope of the present invention to them unless specifically stated. This is just an example. 1 is a fluidized bed furnace, which has a wind box 2 at the bottom, a fluidized bed 4 above the wind box 2 via an air distribution plate 3, and a free space above the fluidized bed 4. It has a board 5. A heat transfer tube 6 is provided in the fluidized bed 4, and coal is introduced from a coal supply lower and combusted.
８は死焼生石灰供給口、９は温度計、１０は空気ブロワ
、１１は排ガス出口である。8 is a dead burnt lime supply port, 9 is a thermometer, 10 is an air blower, and 11 is an exhaust gas outlet.
流動層温度が、実質的に脱硫反応が起こらない９００℃
以上、好ましくは９５０℃以上の所定の温度になるよう
に、予め流動層の熱収支計算によって、伝熱管乙の量を
定める０石炭銘柄の変更などによって、流動１１７１度
が変化する場合には、必要に応して収熱量の調整を行う
、収熱量の増減は伝熱管乙の増加あるいは減少によって
可能であるが、−船釣には、伝熱管乙の表面に設ける低
面カバーの増減、あるいは流動高さを変更して有効な伝
熱管の量を変える方法が採用できる。The fluidized bed temperature is 900°C, where virtually no desulfurization reaction occurs.
As mentioned above, if the flow 1171 degrees changes by changing the coal brand, etc., which determines the amount of heat exchanger tubes by calculating the heat balance of the fluidized bed in advance so that the temperature is preferably 950 degrees Celsius or higher, Adjust the amount of heat absorption as necessary. Increase or decrease in the amount of heat absorption is possible by increasing or decreasing the number of heat transfer tubes. A method of changing the effective amount of heat transfer tubes by changing the flow height can be adopted.
つぎに電気炉加熱式の内径７０ｍ−の円筒形流動層炉を
用いて、粉化飛散性に関する試験を実施した結果を次表
に示す。この試験において、雰囲気ガスとして、Ｓｏｗ
Ｆ ２０００ｐｐｍ＋ 、Ｏｘ ： ２１％、残部Ｎ
２の組成のガスを用いた。Next, using an electric furnace heating type cylindrical fluidized bed furnace with an inner diameter of 70 m, a test regarding powdering and scattering properties was conducted, and the results are shown in the following table. In this test, Sow was used as the atmospheric gas.
F 2000ppm+, Ox: 21%, balance N
A gas having a composition of 2 was used.
（以下余白） （注） ＣａＯとして示している。(Margin below) (Note) Shown as CaO.
上表から明らかなように、流動層を維持するに必要な量
から判定すると、珪砂が最も少なく流動物質として優れ
ているが、硬度が大きいので、流動層内に伝面を設ける
場合には、伝熱管を摩耗するので好ましくない、珪砂に
ついで、死焼生石灰の９５０℃条件が優れていた。なお
死焼生石灰の９５０℃条件は、脱硫反応が生じる８００
℃条件よりも優れていた。As is clear from the table above, judging from the amount required to maintain a fluidized bed, silica sand has the lowest amount and is excellent as a fluid material, but since it has high hardness, when providing a transmission surface in a fluidized bed, Next to silica sand, which is unfavorable because it wears out the heat exchanger tubes, the 950°C condition of dead burnt lime was excellent. The 950°C condition for dead burnt lime is 800°C where the desulfurization reaction occurs.
It was better than the ℃ condition.
本発明は上記のように構成されているので、つぎのよう
に効果を有している。Since the present invention is configured as described above, it has the following effects.
（１） 死焼生石灰などの死焼したアルカリ土類金属
酸化物を用いるので、珪砂、アルミナよりも硬度が小さ
く、伝熱管の摩耗が少なく有利である。また石灰石、軽
焼生石灰と比べて、補給量が少なく経済的である。(1) Since a dead-burned alkaline earth metal oxide such as dead-burned quicklime is used, it has a lower hardness than silica sand or alumina, and is advantageous in that there is less wear on the heat exchanger tubes. Also, compared to limestone and light burnt lime, it requires less replenishment and is more economical.
（２） 流動層温度を実質的に脱硫反応が起こらない
９００℃以上、好ましくは９５０℃以上にすることによ
って、死焼生石灰の補給量を少なくすることができる。(2) By setting the fluidized bed temperature to 900° C. or higher, preferably 950° C. or higher, at which substantially no desulfurization reaction occurs, the amount of dead burnt lime to be replenished can be reduced.
また流動層を高温にすることによって、高い燃焼効率を
得ることができるとともに、高温の排ガスを得ることが
できる。Moreover, by heating the fluidized bed to a high temperature, high combustion efficiency can be obtained, and high-temperature exhaust gas can be obtained.
図面は本発明の流動層燃焼方法を実施する装置の一例を
示す説明図である。The drawing is an explanatory diagram showing an example of an apparatus for carrying out the fluidized bed combustion method of the present invention.
Claims (1)
コークスなどの燃料を燃焼する方法において、流動物質
として死焼したアルカリ土類金属酸化物を供給し、流動
層温度を死焼したアルカリ土類金属酸化物が実質的に脱
硫反応を起こさない９００℃以上にすることを特徴とす
る流動層燃焼方法。 ２ 流動物質が死焼した生石灰である特許請求の範囲第
１項記載の流動層燃焼方法。 ３ 単段燃焼で実施する特許請求の範囲第１項または第
２項記載の流動層燃焼方法。[Claims] 1. In a method of burning fuel such as coal or oil coke in a fluidized bed having heat exchanger tubes, a dead-burned alkaline earth metal oxide is supplied as a fluidized substance, and the fluidized bed is heated. A fluidized bed combustion method characterized in that the temperature is set to 900° C. or higher at which the dead-burned alkaline earth metal oxide substantially does not undergo a desulfurization reaction. 2. The fluidized bed combustion method according to claim 1, wherein the fluidized substance is dead-burned quicklime. 3. The fluidized bed combustion method according to claim 1 or 2, which is carried out by single-stage combustion.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18598886A JPS6341706A (en) | 1986-08-07 | 1986-08-07 | Fluidized bed burning method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18598886A JPS6341706A (en) | 1986-08-07 | 1986-08-07 | Fluidized bed burning method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6341706A true JPS6341706A (en) | 1988-02-23 |
| JPH0454127B2 JPH0454127B2 (en) | 1992-08-28 |
Family
ID=16180397
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP18598886A Granted JPS6341706A (en) | 1986-08-07 | 1986-08-07 | Fluidized bed burning method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6341706A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0493503A (en) * | 1990-08-07 | 1992-03-26 | Mitsubishi Heavy Ind Ltd | Method of operating fluidized bed combustion device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4994578A (en) * | 1973-01-16 | 1974-09-07 | ||
| JPS5821162A (en) * | 1981-07-29 | 1983-02-07 | Nippon Kokan Kk <Nkk> | Ultrasonic flaw detector |
| JPS6252306A (en) * | 1985-09-02 | 1987-03-07 | Aibii Keshohin:Kk | Method of burning oil coke in boiler |
-
1986
- 1986-08-07 JP JP18598886A patent/JPS6341706A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4994578A (en) * | 1973-01-16 | 1974-09-07 | ||
| JPS5821162A (en) * | 1981-07-29 | 1983-02-07 | Nippon Kokan Kk <Nkk> | Ultrasonic flaw detector |
| JPS6252306A (en) * | 1985-09-02 | 1987-03-07 | Aibii Keshohin:Kk | Method of burning oil coke in boiler |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0493503A (en) * | 1990-08-07 | 1992-03-26 | Mitsubishi Heavy Ind Ltd | Method of operating fluidized bed combustion device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0454127B2 (en) | 1992-08-28 |
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