JP2889049B2 - Method for reducing N2O and NOx in fluidized bed combustion - Google Patents
Method for reducing N2O and NOx in fluidized bed combustionInfo
- Publication number
- JP2889049B2 JP2889049B2 JP4149367A JP14936792A JP2889049B2 JP 2889049 B2 JP2889049 B2 JP 2889049B2 JP 4149367 A JP4149367 A JP 4149367A JP 14936792 A JP14936792 A JP 14936792A JP 2889049 B2 JP2889049 B2 JP 2889049B2
- Authority
- JP
- Japan
- Prior art keywords
- combustion
- air
- fluidized bed
- stage
- 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 - Lifetime
Links
- 238000002485 combustion reaction Methods 0.000 title claims description 89
- 238000000034 method Methods 0.000 title claims description 6
- 239000003245 coal Substances 0.000 description 13
- 239000000446 fuel Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 4
- 239000006028 limestone Substances 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 102220579497 Macrophage scavenger receptor types I and II_F23C_mutation Human genes 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000010801 sewage sludge Substances 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
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
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)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、流動層ボイラや流動層
燃焼炉等の流動層燃焼におけるN2O, NOX の低減方法に
関するものである。The present invention relates relates to a method of reducing N 2 O, NO X in the fluidized bed combustion, such as fluidized bed boiler and the fluidized bed combustion furnace.
【０００２】[0002]
【従来の技術】石油危機を契機に石炭の利用拡大が推進
されてきている。しかしながら、石炭は灰分、窒素分を
多量に有し、また燃焼性が悪い固有の問題を有してい
る。このため、石炭を燃料とするには、煤塵およびN2O,
NOX の窒素酸化物に対する公害対策や省エネルギの面
から燃焼性改善策が必要となる。2. Description of the Related Art The use of coal has been expanded in the wake of the oil crisis. However, coal has a large amount of ash and nitrogen and has inherent problems of poor flammability. Therefore, to use coal as fuel, dust and N 2 O,
Flammability improvement from the standpoint of pollution control and energy saving for the nitrogen oxides NO X is required.
【０００３】石炭燃焼ボイラは従来はストーカ焚きが多
かったが、近年は大型化とボイラ効率の向上を目指して
微粉炭焚きが多くなってきた。しかしながら、微粉炭焚
きボイラでは、石炭の灰中未燃分の増加、燃焼室の肥大
化、高温の火炉壁へ灰が溶着、付着するスラッギング現
象や低温の熱交換器などへ堆積するファウリングなどの
問題を生じ使用石炭が限定されている。さらに加えて、
微粉炭燃焼では高温燃焼のためNOX が高く、また石灰石
噴射による直接脱硫も反応温度が高過ぎて採用できず、
高価で大型な脱硝装置や脱硫装置が必要となている。[0003] Conventionally, coal-fired boilers used to be stoker-fired, but in recent years pulverized-coal-fired fires have increased in order to increase the size and improve the boiler efficiency. However, in the pulverized coal-fired boiler, the unburned coal in the ash of the coal increases, the combustion chamber becomes larger, the ash adheres to the high-temperature furnace wall, the slagging phenomenon occurs, and fouling deposits on the low-temperature heat exchanger. And the use of coal is limited. In addition,
The pulverized coal combustion high NO X due to the high temperature combustion, also desulfurization is also not possible to employ the reaction temperature is too high directly by limestone injection,
Expensive and large-sized denitration equipment and desulfurization equipment are required.
【０００４】そこで、最近ではこれらの脱硝装置や脱硫
装置が不要であり、また幅広い石炭を高い燃焼率で燃焼
できる循環流動層ボイラが注目を集め、技術開発が盛ん
に行われつつある。In recent years, a circulating fluidized bed boiler that does not require such a denitration device or desulfurization device and can burn a wide range of coal at a high burning rate has attracted attention, and technical development has been actively carried out.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、近年、
地球温暖化の問題がクローズアップされ、CO2 ，メタ
ン，N2O の発生が問題となっている。特に循環流動層ボ
イラは低温燃焼のためN2Oの発生が問題となっている。However, in recent years,
The problem of global warming has been highlighted, and the generation of CO 2 , methane, and N 2 O has become a problem. Especially in a circulating fluidized bed boiler, the generation of N 2 O is a problem due to low temperature combustion.
【０００６】本発明は、上記の問題点を改善するべくな
したものであって、その目的は、元来NOX 濃度が低い流
動層燃焼において、さらにNOX を低減すると同時に、近
年地球温暖化ガスとして問題となっているN2O をも低減
する、流動層ボイラや流動層燃焼炉等の流動層燃焼にお
けるN2O, NOX の低減方法を提供することである。SUMMARY OF THE INVENTION The present invention has been made to solve the above problems, and it is an object of the present invention to further reduce NO X in a fluidized bed combustion which originally has a low NO X concentration, and simultaneously reduce global warming in recent years. An object of the present invention is to provide a method for reducing N 2 O and NO X in fluidized-bed combustion such as a fluidized-bed boiler and a fluidized-bed combustion furnace, which also reduces N 2 O which is a problem as a gas.
【０００７】[0007]
【課題を解決するための手段】上記目的を達成するため
に、本発明に係わる流動層燃焼におけるN2O, NOX の低
減方法は、１段目燃焼空気を燃焼室底部から、２段目燃
焼空気を燃焼室底部側壁からそれぞれ供給するととも
に、さらに３段目燃焼空気を燃焼室側壁の、燃焼室の高
さの0.25〜0.40の高さ位置から供給するものである。In order to achieve the above object, a method for reducing N 2 O and NO X in fluidized bed combustion according to the present invention is to reduce the first stage combustion air from the bottom of the combustion chamber to the second stage. The combustion air is supplied from the bottom wall of the combustion chamber, and the third stage combustion air is supplied from the side wall of the combustion chamber at a height of 0.25 to 0.40 of the height of the combustion chamber.
【０００８】そして、上記燃焼空気の供給において、１
段目燃焼空気の空気比が２段目燃焼空気の空気比より高
く、且つ両者の空気比の和がほぼ理論空気比となるよう
に１段目燃焼空気と２段目燃焼空気を供給するとよい。In the supply of the combustion air, 1
The first-stage combustion air and the second-stage combustion air may be supplied such that the air ratio of the second-stage combustion air is higher than the air ratio of the second-stage combustion air, and the sum of the two air ratios is substantially equal to the theoretical air ratio. .
【０００９】[0009]
【作用】次に、本発明の構成並びに作用について詳細に
説明する。本発明者が流動層燃焼におけるN2O, NOX 生
成特性について詳細に検討した結果、N2O, NOX の大部
分は燃焼室底部で発生していることが判明した。例え
ば、石炭燃焼におけるNOX は75％以上がフューエル（fu
el）NOX と言われており、さらにフューエルNOX は燃焼
初期に発生する揮発性（volatile）NOX と、主として燃
焼後期に発生するチャー中の残留窒素分によるチャー
（char）NOX とからなる。Next, the configuration and operation of the present invention will be described in detail. The present inventors have studied in detail N 2 O, NO X generation characteristics in fluidized bed combustion, the majority of N 2 O, NO X was found to have occurred in the combustion chamber bottom. For example, more than 75% of NO X in coal combustion is fuel (fu
el) is said to NO X, the more the fuel NO X is volatile occur initial combustion (volatile) NO X, mainly residual nitrogen content by char in the char generated in the combustion late (char) NO X Become.
【００１０】本発明者の調査結果によると、上記のよう
に燃焼室底部において揮発性NOX およびN2O を多量に発
生しており、この揮発性NOX およびN2O の発生を抑制す
ることにより、大幅に燃焼排ガス中のNOX ，N2O を低減
できることを見出した。[0010] According to the present inventors' findings, in the combustion chamber bottom as described above and the volatile NO X and N 2 O large amount generated, suppressing the generation of volatile NO X and N 2 O As a result, it has been found that NO X and N 2 O in the flue gas can be significantly reduced.
【００１１】特に、この揮発性NOX は燃焼空気と石炭か
ら発生する揮発分との混合が律速であり、混合速度を低
下させることによりNOX の発生を効果的に抑制できる。
すなわち、本発明は、多段燃焼を行うに際して、１段目
燃焼空気は石炭から発生する揮発分を燃料過濃状態で燃
焼させ、２段目燃焼空気でほぼ理論空気比で燃焼させ、
３段目燃焼空気で完全燃焼させる点に特徴がある。In particular, mixing of the volatile NO X with combustion air and volatile matter generated from coal is rate-determining, and the generation of NO X can be effectively suppressed by reducing the mixing speed.
That is, according to the present invention, when performing multi-stage combustion, the first-stage combustion air burns volatile components generated from coal in a fuel-rich state, and the second-stage combustion air burns at almost the theoretical air ratio,
It is characterized in that it is completely burned with the third stage combustion air.
【００１２】より具体的には、２段目燃焼空気の供給位
置はアンモニア、シアンなど窒素含有中間生成物の濃度
の高い領域に供給することが肝要であり、これにより、
N2OおよびNOX 低減効果はより顕著となることが明らか
になった。さらに３段目燃焼空気は未燃分を効果的に完
全燃焼させ、N2O, NOX の発生を抑制するように供給す
る点が重要であり、これには供給位置が燃焼室の高さの
0.25〜0.40範囲の高さの燃焼室側壁から供給する必要が
ある。実験によればこの範囲を外れると、適切な燃料過
濃域および完全燃焼域が実現できないことが判明した。More specifically, it is essential that the supply position of the second stage combustion air be supplied to a region where the concentration of nitrogen-containing intermediate products such as ammonia and cyan is high.
It was found that the N 2 O and NO X reduction effects became more significant. Furthermore, it is important that the third stage combustion air be supplied so as to effectively burn the unburned components completely and suppress the generation of N 2 O and NO X. The supply position is determined by the height of the combustion chamber. of
It is necessary to supply from the combustion chamber side wall with a height in the range of 0.25 to 0.40. Experiments have shown that outside of this range, an appropriate fuel rich region and a complete combustion region cannot be achieved.
【００１３】[0013]
【実施例】図１は、本発明に係わる循環流動層ボイラの
概念図である。この循環流動層ボイラでは、流動層燃焼
室１の底部から１段目燃焼空気２を供給し、底部側壁３
から石炭４および石灰石５を供給するとともに、石炭４
および石灰石５の供給位置より上方の底部側壁３から２
段目燃焼空気６を、さらに炉底からＬの高さ位置の燃焼
室側壁７から３段目燃焼空気８をそれぞれ供給して流動
層燃焼が行われるようになっている。なお、図中、９は
循環路に配設されたホットサイクロンを、Ｈは流動層燃
焼室１の高さをそれぞれ示す。1 is a conceptual diagram of a circulating fluidized bed boiler according to the present invention. In this circulating fluidized-bed boiler, first-stage combustion air 2 is supplied from the bottom of the fluidized-bed combustion chamber 1 and the bottom side wall 3 is formed.
Supplies coal 4 and limestone 5 from
And the bottom side walls 3 to 2 above the supply position of the limestone 5
The third stage combustion air 8 is supplied from the combustion chamber side wall 7 at a height L from the furnace bottom, and the third stage combustion air 8 is supplied to the stage combustion air 6 to perform fluidized bed combustion. In the drawing, reference numeral 9 denotes a hot cyclone provided in the circulation path, and H denotes the height of the fluidized bed combustion chamber 1.
【００１４】そして、流動層燃焼に際しては、先ず、１
段目燃焼空気２を空気比0.5 〜0.85の範囲で供給し、燃
料過濃状態で燃焼させ、アンモニア、シアンなどの窒素
含有中間生成物を多量に発生させ、一方NOなどの発生を
抑制する。In fluidized bed combustion, first, 1
The stage combustion air 2 is supplied at an air ratio in the range of 0.5 to 0.85 and burns in a fuel-rich state to generate a large amount of nitrogen-containing intermediate products such as ammonia and cyan while suppressing generation of NO and the like.
【００１５】次に、２段目燃焼空気６を、１段目燃焼空
気２と２段目燃焼空気６の合計空気比が1.05以下となる
ように空気比0.5 〜0.20の範囲で供給し、アンモニア、
シアンなどの窒素含有中間生成物をNOにならないように
反応させる。Next, the second stage combustion air 6 is supplied in an air ratio of 0.5 to 0.20 so that the total air ratio of the first stage combustion air 2 and the second stage combustion air 6 becomes 1.05 or less, and ammonia is supplied. ,
A nitrogen-containing intermediate such as cyan is reacted so as not to become NO.
【００１６】さらに、３段目燃焼空気８をＬの高さ位置
から供給しCO, H2などの未燃分を完全燃焼させ、さらに
その上部での未燃チャーの燃焼を促進する。この場合、
３段目燃焼空気８の供給高さ位置Ｌが重要であり、N2O
およびNOの発生に影響を及ぼす。Furthermore, CO supplies third-stage combustion air 8 from the height position of the L, is complete combustion of unburned such H 2, further promoting combustion of the unburned char in the upper portion thereof. in this case,
The supply height position L of the third stage combustion air 8 is important, and N 2 O
And NO generation.
【００１７】図２は、３段目燃焼空気８の供給位置Ｌの
N2O, NOに及ぼす影響を示す。３段目燃焼空気８の供給
位置Ｌは流動層燃焼室１の全高Ｈに対する無次元数で示
す。空気比は１段目空気比0.6 、２段目空気比0.4 、３
段目空気比0.2 である。FIG. 2 shows the state of the supply position L of the third stage combustion air 8.
The effect on N 2 O and NO is shown. The supply position L of the third stage combustion air 8 is indicated by a dimensionless number with respect to the total height H of the fluidized bed combustion chamber 1. The air ratio is 1st stage air ratio 0.6, 2nd stage air ratio 0.4, 3
The stage air ratio is 0.2.
【００１８】３段目燃焼空気８の供給位置Ｌを高くする
ほど、燃焼率は次第に低下し、0.4以上では空気不足の
燃焼域が広くなり過ぎ顕著に燃焼率が低下する。またN2
O およびNOX はＬ／Ｈが0.25〜0.4 の範囲で顕著に低下
する。この理由は、Ｌ／Ｈ＝0.25〜0.4 で適切な燃料過
濃域および完全燃焼域が実現され、燃焼率を低下させる
ことなくN2O, NOX を低減できるからである。As the supply position L of the third stage combustion air 8 is increased, the combustion rate gradually decreases. If the supply position L is 0.4 or more, the combustion area in which the air is insufficient becomes too wide, and the combustion rate decreases significantly. Also N 2
O and NO X is L / H is significantly decreased in the range of 0.25 to 0.4. The reason is that when L / H = 0.25 to 0.4, an appropriate fuel rich region and a complete combustion region are realized, and N 2 O and NO X can be reduced without lowering the combustion rate.
【００１９】このように、燃焼率をそれほど低下させる
ことなく、循環流動層ボイラで問題となるN2O,の発生を
抑制できるとともに、NOX も低下できる。As described above, the generation of N 2 O, which is a problem in the circulating fluidized bed boiler, can be suppressed without significantly lowering the combustion rate, and NO X can be reduced.
【００２０】本発明は、循環流動層ボイラの実施例で説
明したが、バブリング流動層ボイラや、都市ごみ、下水
汚泥、産業廃棄物の流動層燃焼炉にも応用できることは
言うまでもない。Although the present invention has been described in the embodiment of the circulating fluidized bed boiler, it is needless to say that the present invention can be applied to a bubbling fluidized bed boiler and a fluidized bed combustion furnace for municipal solid waste, sewage sludge, and industrial waste.
【００２１】[0021]
【発明の効果】以上説明したように、本発明にによれ
ば、元来NOX 濃度が低い流動層燃焼において、さらにNO
X を低減すると同時にN2O をも低減することができ、公
害対策や省エネルギの面は元より、近年問題となってい
る地球温暖化ガスの排出を低減することができ工業的価
値は極めて大きい。As described in the foregoing, according to the present invention, the original NO X concentration is lower fluidized bed combustion, further NO
X and N 2 O can be reduced at the same time, reducing pollution and energy savings, as well as global warming gas emissions, which have become a problem in recent years. large.
【図面の簡単な説明】[Brief description of the drawings]
【図１】本発明に係わる循環流動層ボイラの概念図であ
る。FIG. 1 is a conceptual diagram of a circulating fluidized bed boiler according to the present invention.
【図２】３段目燃焼空気の供給位置と煙道におけるN2O,
NOX および燃焼率との関係を示すグラフ図である。FIG. 2 The supply position of the third stage combustion air and N 2 O,
Is a graph showing the relationship between the NO X and the combustion rate.
１：流動層燃焼室 ２：１段目燃焼空気
３：底部側壁 ４：石炭 ５：石灰石
６：２段目燃焼空気 ７：燃焼室側壁 ８：３段目燃焼空気
９：ホットサイクロン Ｌ：３段目燃焼空気の供給位置までの炉底からの高さ Ｈ：流動層燃焼室の高さ1: Fluidized bed combustion chamber 2: First stage combustion air
3: Bottom side wall 4: Coal 5: Limestone
6: second stage combustion air 7: combustion chamber side wall 8: third stage combustion air
9: Hot cyclone L: Height from bottom of furnace to supply position of third stage combustion air H: Height of fluidized bed combustion chamber
───────────────────────────────────────────────────── フロントページの続き (58)調査した分野(Int.Cl.6，ＤＢ名) F23C 11/02 302 ──────────────────────────────────────────────────続 き Continued on front page (58) Field surveyed (Int.Cl. 6 , DB name) F23C 11/02 302
Claims (2)
目燃焼空気を燃焼室底部側壁からそれぞれ供給するとと
もに、さらに３段目燃焼空気を燃焼室側壁の、燃焼室の
高さの0.25〜0.40の高さ位置から供給することを特徴と
する流動層燃焼におけるN2O, NOX の低減方法。The first stage combustion air is supplied from the bottom of the combustion chamber from the bottom of the combustion chamber, and the second stage combustion air is supplied from the bottom wall of the combustion chamber. A method for reducing N 2 O and NO X in fluidized bed combustion, wherein the supply is performed from a height of 0.25 to 0.40.
気の空気比より高く、且つ両者の空気比の和がほぼ理論
空気比となるように１段目燃焼空気と２段目燃焼空気を
供給する請求項１記載の流動層燃焼におけるN2O, NOX
の低減方法。2. The first-stage combustion air and the second-stage combustion air such that the air ratio of the first-stage combustion air is higher than the air ratio of the second-stage combustion air, and the sum of the air ratios is substantially equal to the theoretical air ratio. 2. N 2 O, NO X in fluidized bed combustion according to claim 1, wherein combustion air is supplied.
Reduction method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4149367A JP2889049B2 (en) | 1992-06-09 | 1992-06-09 | Method for reducing N2O and NOx in fluidized bed combustion |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4149367A JP2889049B2 (en) | 1992-06-09 | 1992-06-09 | Method for reducing N2O and NOx in fluidized bed combustion |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05340509A JPH05340509A (en) | 1993-12-21 |
| JP2889049B2 true JP2889049B2 (en) | 1999-05-10 |
Family
ID=15473592
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4149367A Expired - Lifetime JP2889049B2 (en) | 1992-06-09 | 1992-06-09 | Method for reducing N2O and NOx in fluidized bed combustion |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2889049B2 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ATE228225T1 (en) * | 1996-12-30 | 2002-12-15 | Alstom Power Inc | METHOD FOR CONTROLLING NITROGEN OXIDES IN A CIRCULATING FLUIDIZED STEAM GENERATOR |
| JP3746751B2 (en) * | 2002-10-04 | 2006-02-15 | 三菱重工業株式会社 | Control method and control apparatus for sludge combustion furnace |
| MX2010004947A (en) * | 2007-11-07 | 2010-10-04 | Metawater Co Ltd | Fluidized-bed incinerator and method of fluidized-bed incineration of sludge with the same. |
| JP5525138B2 (en) * | 2008-03-26 | 2014-06-18 | メタウォーター株式会社 | Fluidized incinerator |
| JP5435973B2 (en) * | 2009-01-30 | 2014-03-05 | メタウォーター株式会社 | Fluidized incinerator |
| JP2016041990A (en) * | 2014-08-18 | 2016-03-31 | 東洋エンジニアリング株式会社 | Heating device including boiler |
| JP7075574B2 (en) * | 2017-05-29 | 2022-05-26 | 国立研究開発法人産業技術総合研究所 | Combustion furnace of organic waste and treatment system of organic waste using the combustion furnace |
-
1992
- 1992-06-09 JP JP4149367A patent/JP2889049B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH05340509A (en) | 1993-12-21 |
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