JPS6125861Y2 - - Google Patents
Info
- Publication number
- JPS6125861Y2 JPS6125861Y2 JP6551380U JP6551380U JPS6125861Y2 JP S6125861 Y2 JPS6125861 Y2 JP S6125861Y2 JP 6551380 U JP6551380 U JP 6551380U JP 6551380 U JP6551380 U JP 6551380U JP S6125861 Y2 JPS6125861 Y2 JP S6125861Y2
- Authority
- JP
- Japan
- Prior art keywords
- furnace
- fluidized bed
- regeneration
- coal
- fuel
- 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
- 230000008929 regeneration Effects 0.000 claims description 31
- 238000011069 regeneration method Methods 0.000 claims description 31
- 239000003795 chemical substances by application Substances 0.000 claims description 28
- 239000000446 fuel Substances 0.000 claims description 20
- 238000006477 desulfuration reaction Methods 0.000 claims description 17
- 230000023556 desulfurization Effects 0.000 claims description 17
- 238000002309 gasification Methods 0.000 claims description 15
- 239000003245 coal Substances 0.000 claims description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims 3
- 230000001172 regenerating effect Effects 0.000 claims 1
- 239000004576 sand Substances 0.000 claims 1
- 239000000377 silicon dioxide Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 description 18
- 239000010410 layer Substances 0.000 description 17
- 230000003009 desulfurizing effect Effects 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 9
- 238000009826 distribution Methods 0.000 description 7
- 239000000295 fuel oil Substances 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 239000010742 number 1 fuel oil Substances 0.000 description 4
- 239000002956 ash Substances 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000010459 dolomite Substances 0.000 description 2
- 229910000514 dolomite Inorganic materials 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
【考案の詳細な説明】
本考案は、主として石炭、重油などの燃料の部
分酸化反応により生成する還元ガスによつて、亜
硫酸ガスを吸収したCaSO4（石こう）を含む脱硫
剤を再生する２層式の流動床再生炉に関するもの
である。[Detailed description of the invention] This invention is a two-layer system that regenerates a desulfurization agent containing CaSO 4 (gypsum) that has absorbed sulfur dioxide gas using a reducing gas generated by a partial oxidation reaction of fuels such as coal and heavy oil. This relates to a fluidized bed regeneration furnace of the type.
従来から、石炭、重油などの燃料と石灰石
（CaCO3）、ドロマイト（MgCO3とCaCO3とから
なる）などの脱硫剤とで形成される流動床内に伝
熱管を挿入して熱回収をはかるようにした流動床
ボイラが既に知られている。またこの流動床ボイ
ラから抜き出される使用済の脱硫剤と、石炭、重
油などの燃料を燃焼させて発生させた水素、一酸
化炭素などの還元ガスとを反応せしめて使用済の
脱硫剤を再生させる流動床再生炉も既に知られて
いる。従来の流動床再生炉は、１層の流動床に石
炭などの燃料とCaSO4を含む使用済の脱硫剤を投
入し、石炭などの燃料のガス化とともに、同一炉
内にて脱硫剤を再生するものである。石炭などの
燃料のガス化は常圧では900〜1050℃の範囲内が
望ましく、1050℃以上になると、石炭などの燃料
の酸化反応においてヒートスポツト部が生じ石炭
灰と脱硫剤とがアグロメレーシヨン（焼結）現象
が起こり、塊状の固形物が生成して操業が困難な
事態になるおそれがある。しかし脱硫剤の再生反
応については1050〜1150℃の範囲内にて行なうの
が望ましく、1050℃以下では副反応が起こる。し
たがつて石炭と脱硫剤の共存下でのアグロメレー
シヨンがあることおよびガス化反応と再生反応の
望ましい温度領域が必ずしも一致しないことのた
め１層の流動床を有する同一炉にてガス化反応と
再生反応とを行なうことは得策でない。 Conventionally, heat recovery has been achieved by inserting heat transfer tubes into a fluidized bed formed by fuels such as coal and heavy oil and desulfurizing agents such as limestone (CaCO 3 ) and dolomite (consisting of MgCO 3 and CaCO 3 ). Such a fluidized bed boiler is already known. In addition, the used desulfurizing agent extracted from this fluidized bed boiler is reacted with reducing gases such as hydrogen and carbon monoxide generated by burning fuels such as coal and heavy oil to regenerate the used desulfurizing agent. Fluidized bed regeneration furnaces are also already known. In a conventional fluidized bed regeneration furnace, a fuel such as coal and a used desulfurization agent containing CaSO 4 are charged into a single layer of fluidized bed, and while the fuel such as coal is gasified, the desulfurization agent is regenerated in the same furnace. It is something to do. Gasification of fuels such as coal is preferably performed at a temperature in the range of 900 to 1050℃ at normal pressure.When the temperature exceeds 1050℃, heat spots occur during the oxidation reaction of fuels such as coal, and coal ash and desulfurization agent agglomerate. (sintering) phenomenon may occur, resulting in the formation of lumpy solids, which may make operations difficult. However, the regeneration reaction of the desulfurizing agent is preferably carried out within the range of 1050 to 1150°C, and side reactions occur below 1050°C. Therefore, because there is agglomeration in the coexistence of coal and desulfurization agent, and because the desired temperature ranges for the gasification reaction and the regeneration reaction do not necessarily match, the gasification reaction is performed in the same furnace with one layer of fluidized bed. It is not a good idea to carry out a regeneration reaction.
本考案は上記の諸点に鑑みなされたもので、流
動床を上下２層に区分し、下層の流動床では石炭
などの燃料とアグロメレーシヨンが起こり難いけ
い砂のような不活な流動媒体に、石炭などの燃料
と空気を投入して（さらにスチームを添加する場
合もある）石炭などの燃料をガス化し還元ガスを
発生させ、上層の流動床では投入された脱硫剤か
らなる流動媒体と前記還元ガスとを反応させて、
脱硫剤を再生するように構成することにより、ガ
ス化反応と再生反応とをきわめて効率よく行なう
ことができる流動床再生炉を提供せんとするもの
である。 The present invention was developed in view of the above points, and the fluidized bed is divided into two layers, upper and lower. , a fuel such as coal and air are introduced (steam may also be added) to gasify the fuel such as coal to generate reducing gas, and in the upper fluidized bed, the fluidized medium consisting of the desulfurization agent and the above By reacting with reducing gas,
It is an object of the present invention to provide a fluidized bed regeneration furnace that is configured to regenerate a desulfurization agent and can perform gasification reactions and regeneration reactions extremely efficiently.
以下、本考案の構成を図面に示す実施態様に基
づいて説明する。第１図は本考案の流動床再生炉
の一実施態様を示し、第２図はこの流動床再生炉
を流動床ボイラなどの流動床燃焼炉に接続した状
態を示している。１は流動床再生炉の炉本体で、
この炉本体１内の下部に多数の空気噴出孔２を有
する空気分散板３が設けられ、この空気分散板３
の上側に、けい砂などの流動媒体に石炭、重油、
コロイダル燃料などの燃料をガス化して水素、一
酸化炭素などの還元ガスを発生せしめるガス化層
４が形成される。さらに炉本体１内において、こ
のガス化層４の上側に空間部５を介して多数の還
元ガス噴出孔６を有する還元ガス分散板７が設け
られ、この還元ガス分散板７の上側に炉内に投入
されるCaSO4（石こう）を含む使用済の脱硫剤を
前記還元ガスによつて再生する再生層８が形成さ
れる。１０は燃料供給管、１１は空気供給管、１
２は風箱、１３は起動用バーナ、１４は灰抜出
管、１５は排ガス排出管、１６は流動床ボイラな
どから抜き出された使用済の劣化脱硫剤を再生層
に投入するための劣化脱硫剤投入管、１７は再生
した脱硫剤をオーバフローとして抜き出すための
オーバフロー管である。 Hereinafter, the configuration of the present invention will be explained based on embodiments shown in the drawings. FIG. 1 shows an embodiment of the fluidized bed regeneration furnace of the present invention, and FIG. 2 shows the fluidized bed regeneration furnace connected to a fluidized bed combustion furnace such as a fluidized bed boiler. 1 is the furnace body of the fluidized bed regeneration furnace,
An air distribution plate 3 having a large number of air injection holes 2 is provided in the lower part of the furnace body 1.
On the top side, coal, heavy oil,
A gasification layer 4 is formed that gasifies fuel such as colloidal fuel to generate reducing gas such as hydrogen and carbon monoxide. Further, in the furnace body 1, a reducing gas dispersion plate 7 having a large number of reducing gas ejection holes 6 is provided above the gasification layer 4 via a space 5. A regeneration layer 8 is formed in which the used desulfurization agent containing CaSO 4 (gypsum), which is introduced into the reactor, is regenerated by the reducing gas. 10 is a fuel supply pipe, 11 is an air supply pipe, 1
2 is a wind box, 13 is a start-up burner, 14 is an ash extraction pipe, 15 is an exhaust gas discharge pipe, and 16 is a deterioration tube for introducing used deteriorated desulfurization agent extracted from a fluidized bed boiler etc. into the regeneration layer. The desulfurizing agent input pipe 17 is an overflow pipe for extracting the regenerated desulfurizing agent as an overflow.
上記のように構成された流動床再生炉は、第２
図に示すように流動床ボイラ１８に接続される。
この流動床ボイラ１８は、炉内底部に多数の空気
噴出孔を有する空気分散板２０を設け、この空気
分散板２０の上側に石灰石または（および）ドロ
マイトなどの脱硫剤と石炭、重油、コロイダル燃
料などの燃料とからなる流動床２１を形成せし
め、この流動床２１内に伝熱管２２を配設してな
るものである。２３はメークアツプ用の脱硫剤を
投入するための脱硫剤供給管である。 The fluidized bed regeneration furnace configured as described above has a second
It is connected to a fluidized bed boiler 18 as shown in the figure.
This fluidized bed boiler 18 is equipped with an air distribution plate 20 having a large number of air ejection holes at the bottom of the furnace, and a desulfurizing agent such as limestone or/and dolomite and coal, heavy oil, colloidal fuel, etc. on the upper side of the air distribution plate 20. A fluidized bed 21 is formed of fuel such as fuel, and heat transfer tubes 22 are disposed within this fluidized bed 21. 23 is a desulfurizing agent supply pipe for introducing a desulfurizing agent for make-up.
流動床再生炉内において、ガス化層４に投入さ
れた石炭、重油などの燃料は常圧で900〜1000℃
の温度で部分酸化されて水素、一酸化炭素などの
還元ガスを発生する。一方、流動床ボイラ１８か
ら抜き出された使用済の劣化脱硫剤（CaSO4と未
反応のCaOとからなる）は、劣化脱硫剤投入管１
６を経て流動床再生炉内の再生層８に投入され、
この再生層８で劣化脱硫剤はガス化層４で発生し
上昇してくる水素、一酸化炭素などの還元ガスと
1050〜1150℃の温度で次式のように反応してCaO
に再生される。 In the fluidized bed regeneration reactor, fuel such as coal and heavy oil fed into the gasification layer 4 is heated to a temperature of 900 to 1000°C at normal pressure.
It is partially oxidized at a temperature of 100 mL to generate reducing gases such as hydrogen and carbon monoxide. On the other hand, the used degraded desulfurization agent (consisting of CaSO 4 and unreacted CaO) extracted from the fluidized bed boiler 18 is transferred to the degraded desulfurization agent input pipe 1.
6 and then put into the regeneration bed 8 in the fluidized bed regeneration furnace.
In this regeneration layer 8, the degraded desulfurization agent is mixed with reducing gases such as hydrogen and carbon monoxide generated and rising in the gasification layer 4.
CaO reacts at a temperature of 1050 to 1150℃ as shown in the following equation.
will be played.
CaSO4＋H2→CaO＋SO2＋H2O
CaSO4＋CO→CaO＋SO2＋CO2
この再生反応により再生したCaOはオーバフロ
ー管１７から抜き出され、リサイクル管２４を経
て流動床ボイラ１８に循環して再使用される。 CaSO 4 +H 2 →CaO+SO 2 +H 2 O CaSO 4 +CO→CaO+SO 2 +CO 2 CaO regenerated by this regeneration reaction is extracted from the overflow pipe 17 and circulated through the recycle pipe 24 to the fluidized bed boiler 18 for reuse. Ru.
つぎに本考案の流動床再生炉を用いて試験した
結果の一例を説明する。 Next, an example of the results of a test using the fluidized bed regeneration furnace of the present invention will be explained.
空気供給量 27.5Nm3／Hr 石炭供給量 4.6Kg／Hr 脱硫剤供給量 5.6Kg／Hr とすると、 ガス化層温度 950℃ カーボンのガス化率 80％ 再生層温度 1050℃ 脱硫剤の再生率 90％ の結果を得た。 Air supply amount 27.5Nm 3 /Hr Coal supply amount 4.6Kg/Hr Desulfurization agent supply amount 5.6Kg/Hr Gasification layer temperature 950℃ Carbon gasification rate 80% Regeneration layer temperature 1050℃ Desulfurization agent regeneration rate 90 % results were obtained.
以上説明したように、本考案の流動床再生炉は
炉内に望ましい温度領域が異なるガス化層と再生
層とを分離して形成せしめたものであるから、灰
と脱硫剤との焼結現象が生じるおそれはなく、こ
のため炉の操業を容易に行なうことができ、また
ガス化層で発生した還元ガスが上昇し還元ガス分
散板から噴出するように構成されているので、還
元ガスの均一な分布が得られ再生反応が円滑に行
なわれ、さらに熱を有効利用できるので炉全体を
コンパクトにすることができるなどの効果を有し
ている。 As explained above, the fluidized bed regeneration furnace of the present invention has a gasification layer and a regeneration layer that have different desirable temperature ranges formed separately in the furnace, so that the sintering phenomenon of ash and desulfurization agent is prevented. There is no risk of this occurring, and the furnace can therefore be operated easily.Also, since the structure is such that the reducing gas generated in the gasification layer rises and is ejected from the reducing gas distribution plate, the reducing gas is uniformly distributed. This has the advantage that a uniform distribution is obtained, the regeneration reaction is carried out smoothly, and the heat can be used effectively, making it possible to make the entire furnace more compact.
第１図は本考案の流動床再生炉の一実施態様を
示す断面説明図、第２図は本考案の流動床再生炉
を流動床燃焼炉に接続した状態を示すフローシー
トである。
１……炉本体、２……空気噴出孔、３……空気
分散板、４……ガス化層、５……空間部、６……
還元ガス噴出孔、７……還元ガス分散板、８……
再生層、１０……燃料供給管、１１……空気供給
管、１２……風箱、１３……起動用バーナ、１４
……灰抜出管、１５……排ガス排出管、１６……
劣化脱硫剤投入管、１７……オーバフロー管、１
８……流動床ボイラ、２０……空気分散板、２１
……流動床、２２……伝熱管、２３……脱硫剤供
給管、２４……リサイクル管。
FIG. 1 is a cross-sectional explanatory diagram showing one embodiment of the fluidized bed regeneration furnace of the present invention, and FIG. 2 is a flow sheet showing the state in which the fluidized bed regeneration furnace of the present invention is connected to a fluidized bed combustion furnace. DESCRIPTION OF SYMBOLS 1...Furnace main body, 2...Air jet hole, 3...Air distribution plate, 4...Gasification layer, 5...Space part, 6...
Reducing gas outlet, 7... Reducing gas distribution plate, 8...
Regeneration layer, 10... Fuel supply pipe, 11... Air supply pipe, 12... Wind box, 13... Start-up burner, 14
... Ash extraction pipe, 15 ... Exhaust gas discharge pipe, 16 ...
Degraded desulfurizing agent input pipe, 17...Overflow pipe, 1
8...Fluidized bed boiler, 20...Air distribution plate, 21
... Fluidized bed, 22 ... Heat exchanger tube, 23 ... Desulfurizing agent supply pipe, 24 ... Recycle pipe.
Claims (1)
還元ガスによつて、亜硫酸ガスを吸収したCaSO4
を含む脱硫剤を再生する流動床再生炉において、
炉内の下部にけい砂などの流動媒体に石炭などの
燃料と空気とを投入し石炭などの燃料をガス化し
て還元ガスを発生せしめるガス化層を形成し、こ
のガス化層の上方に炉内に投入されるCaSO4を含
む脱硫剤を前記還元ガスによつて再生する再生層
を形成してなることを特徴とする流動床再生炉。 CaSO 4 absorbs sulfur dioxide gas by reducing gas generated by partial oxidation reaction of fuel such as coal.
In a fluidized bed regeneration furnace that regenerates a desulfurization agent containing
At the bottom of the furnace, fuel such as coal and air are injected into a fluidized medium such as silica sand to form a gasification layer that gasifies the fuel such as coal and generates reducing gas.The furnace is placed above this gasification layer. 1. A fluidized bed regeneration furnace comprising a regeneration layer for regenerating a desulfurization agent containing CaSO 4 introduced into the furnace using the reducing gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6551380U JPS6125861Y2 (en) | 1980-05-12 | 1980-05-12 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6551380U JPS6125861Y2 (en) | 1980-05-12 | 1980-05-12 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56168239U JPS56168239U (en) | 1981-12-12 |
| JPS6125861Y2 true JPS6125861Y2 (en) | 1986-08-04 |
Family
ID=29659657
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6551380U Expired JPS6125861Y2 (en) | 1980-05-12 | 1980-05-12 |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6125861Y2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003027019A1 (en) * | 2001-09-26 | 2003-04-03 | Yabashi Industries Co., Ltd. | Method for recycling calcium sulfate |
-
1980
- 1980-05-12 JP JP6551380U patent/JPS6125861Y2/ja not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003027019A1 (en) * | 2001-09-26 | 2003-04-03 | Yabashi Industries Co., Ltd. | Method for recycling calcium sulfate |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56168239U (en) | 1981-12-12 |
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