JPH02219893A - Entrained bed type of pulverized solid fuel gasifier and operation thereof - Google Patents
Entrained bed type of pulverized solid fuel gasifier and operation thereofInfo
- Publication number
- JPH02219893A JPH02219893A JP4281489A JP4281489A JPH02219893A JP H02219893 A JPH02219893 A JP H02219893A JP 4281489 A JP4281489 A JP 4281489A JP 4281489 A JP4281489 A JP 4281489A JP H02219893 A JPH02219893 A JP H02219893A
- Authority
- JP
- Japan
- Prior art keywords
- gasifier
- solid fuel
- pulverized solid
- oxidizer
- oxidizing agent
- 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
- 239000004449 solid propellant Substances 0.000 title claims description 28
- 239000007800 oxidant agent Substances 0.000 claims abstract description 89
- 239000007789 gas Substances 0.000 claims abstract description 36
- 238000002309 gasification Methods 0.000 claims abstract description 24
- 239000011261 inert gas Substances 0.000 claims abstract description 23
- 238000000034 method Methods 0.000 claims description 28
- 238000002844 melting Methods 0.000 claims description 14
- 230000008018 melting Effects 0.000 claims description 14
- 239000000446 fuel Substances 0.000 claims description 7
- 238000001514 detection method Methods 0.000 claims description 5
- 238000005259 measurement Methods 0.000 claims 1
- 239000002893 slag Substances 0.000 abstract description 64
- 239000002994 raw material Substances 0.000 abstract description 38
- 239000003245 coal Substances 0.000 abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 9
- 239000001301 oxygen Substances 0.000 abstract description 9
- 229910052760 oxygen Inorganic materials 0.000 abstract description 9
- 239000007787 solid Substances 0.000 abstract description 7
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000010586 diagram Methods 0.000 description 14
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 230000001590 oxidative effect Effects 0.000 description 8
- 239000002956 ash Substances 0.000 description 7
- 239000012159 carrier gas Substances 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000011819 refractory material Substances 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 238000010191 image analysis Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 230000002354 daily effect Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- -1 nitrogen Chemical compound 0.000 description 2
- 238000011017 operating method Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野〕
本発明は、微粉固体燃料のガス化装置に係り、特に安定
して起動、停止ができ、信頼性の高い噴流層式微粉固体
燃料ガス化装置およびその運転方法に関する。Detailed Description of the Invention (Industrial Application Field) The present invention relates to a pulverized solid fuel gasification device, and in particular to a spouted bed type pulverized solid fuel gasification device that can stably start and stop and has high reliability. Concerning the device and its operating method.
（従来の技術）
従来、石炭ガス化炉には、固定層、流動層、噴流層等の
各方式が種々提案されている。これらの方式の中で、噴
流層は原料を微粉にして酸素、空気等の酸化剤とともに
石炭の灰の溶融温度以上（１３００Ｎ１６００℃）の温
度の炉内に供給してガス化させるため、他の方式に比較
し、ガス化効率が高く、適用炭種が広く、また公害性の
副産物が少ない等の特徴を有していることから、合成ガ
ス、複合発電、燃料電池等の燃料製造に適しており、コ
ンパクトで、例えば毎日の起動・停止、あるいは負荷追
随性がよい特徴を有している。(Prior Art) Conventionally, various types of coal gasifiers, such as fixed bed, fluidized bed, and spouted bed, have been proposed. Among these methods, in the spouted bed method, the raw material is pulverized and supplied together with oxidizing agents such as oxygen and air into a furnace at a temperature higher than the melting temperature of coal ash (1300 N 1600°C) for gasification. Compared to other methods, this method has higher gasification efficiency, a wider range of applicable coal types, and fewer polluting byproducts, making it suitable for producing fuels such as synthetic gas, combined cycle power generation, and fuel cells. It is compact and has features such as daily startup and shutdown, and good load followability.
噴流層方式のガス化炉としては、微粉炭またはチャー（
ガスとともに飛散するカーボン粒子）とガス化剤（酸素
あるいは空気）を同じバーナより吹込む１段方式の装置
と、前記のバーナに加えて、微粉炭またはチャーだけを
単独に吹込むバーナを設置する２段方式の装置がある。A spouted bed gasifier uses pulverized coal or char (
A one-stage device that blows carbon particles (which are scattered with the gas) and a gasifying agent (oxygen or air) from the same burner, and a burner that blows only pulverized coal or char alone in addition to the burner described above. There is a two-stage system.
石炭ガス化反応は、大別すると以下の方式で表わされる
。Coal gasification reactions can be broadly classified into the following methods.
石炭→チャー、）！、、Ｃｏ、Ｃｏｗ ５ＣＨ４（１）
チャー＋０３→ＣＯｔ、Ｃｏ、Ｈ！
石炭＋０２→ＣＣ０１ＣＯ、Ｈｚ
（１）式は熱分解反応であり、前記した２段方式におい
て、微粉炭だけを単独に吹込むバーナによって起こり易
い。（１）式と（２）式の反応を明らかに区別して併発
させる方式の代表例としては、公知のごとく米国のＢｌ
−ＧＡＳプロセスがある。またバーナから石炭とガス化
剤とを同時に供給し、意図的に（１）式と（２）式とを
区別しない（３）式の反応式によるプロセスがあり、代
表例としてはＴｅｘａｃｏプロセス、５ｈｅ１β−Ｋｏ
ｐｐｅｒｓプロセス等がある。また本発明者らは、例え
ば特願昭５８−４７１６２および特願昭５８−５０４９
６に示すように、炉内に酸化剤の配分の異なるバーナを
２段に複数設置した２段方式のプロセスを提案している
。第８図に示す従来のガス化法では、微粉炭のごとき原
料１を窒素のごとき原料搬送ガス３０と酸素、空気のよ
うな酸化剤４０とを供給するバーナ６８および６９を、
ガス化室（炉内）６７の上段および下段に設置し、酸化
剤４０を上段バーナ６８には少なく、下段バーナ６９に
は多く投入するものである。なお図中９２は生成ガス、
２０および２１はフィーダ、６１は断熱耐火材よりなる
炉壁、６０はガス化炉本体である。酸化剤４０を上述の
ごとく配分することによって、下段バーナでは特に石炭
＋０□→ＣＯ，十Ｈｓ Ｏ（４）
上段バーナでは特に
チャー＋ＣＯｔ→２ＣＯ（５）
チャー十Ｈ２０→Ｈ，＋ＣＯ（６）
の反応を起こり易くするものである。この方法では、酸
化剤４０を下段バーナ６９に多く配分し、スラグ６６を
流下させる孔（スラグタップ）６３の付近を高温にせし
め、かつ上段バーナ６８では活性なチャーを生成させよ
うとするものである。Coal → Char, )! ,,Co,Cow 5CH4(1)
Char +03 → COt, Co, H! Coal+02→CC01CO, Hz Equation (1) is a thermal decomposition reaction, which is likely to occur in the two-stage system described above by a burner that blows only pulverized coal alone. As a typical example of a system in which the reactions of formulas (1) and (2) are clearly distinguished and caused to occur simultaneously, as is well known, the American
- There is a GAS process. There is also a process using reaction formula (3) in which coal and gasifying agent are supplied simultaneously from a burner and intentionally does not distinguish between formula (1) and formula (2). Typical examples include the Texaco process, 5he1β -Ko
There are processes such as pers processes. In addition, the present inventors have, for example, Japanese Patent Applications No. 58-47162 and No. 58-5049.
As shown in Fig. 6, we have proposed a two-stage process in which a plurality of burners with different oxidizing agent distributions are installed in two stages in the furnace. In the conventional gasification method shown in FIG. 8, burners 68 and 69 are used to supply a raw material 1 such as pulverized coal with a raw material carrier gas 30 such as nitrogen and an oxidizing agent 40 such as oxygen or air.
The oxidizing agent 40 is installed in the upper and lower stages of the gasification chamber (inside the furnace) 67, and a small amount of the oxidizing agent 40 is introduced into the upper burner 68 and a large amount is introduced into the lower burner 69. In addition, 92 in the figure is generated gas,
20 and 21 are feeders, 61 is a furnace wall made of a heat insulating refractory material, and 60 is a gasifier main body. By distributing the oxidizer 40 as described above, in the lower burner, especially coal +0□→CO, 10Hs O(4), and in the upper burner, especially char+COt→2CO(5), and char+0H20→H, +CO(6). It makes it easier for the reaction to occur. In this method, a large amount of the oxidizing agent 40 is distributed to the lower burner 69, the area near the hole (slag tap) 63 through which the slag 66 flows is heated to a high temperature, and active char is generated in the upper burner 68. be.
また第９図にはガス化炉に設置する従来のバーナの一例
を示す。第９図に示すバーナは、原料ノズル１２２の周
りに酸化剤噴出ノズル１２３を多敞設置したものであり
、原料１と酸化剤４０との混合を良好にするため、原料
ノズル１２２と酸化剤噴出ノズル１２３を近接して設置
したものである。いずれのプロセスにおいても、ガス化
に用いられるバーナは、（１）弐〜（６）式に示すよう
な反応を速やかに起こさせようとして、石炭と酸化剤と
が速やかにかつ良好に混合させようとしたものである。Further, FIG. 9 shows an example of a conventional burner installed in a gasifier. The burner shown in FIG. 9 has multiple oxidant jetting nozzles 123 installed around a raw material nozzle 122. In order to improve the mixing of the raw material 1 and the oxidizing agent 40, the raw material nozzle 122 and the oxidizing agent jetting nozzle 123 are installed around the raw material nozzle 122. Nozzles 123 are installed close to each other. In either process, the burner used for gasification tries to cause the reactions shown in equations (1) 2 to (6) to occur quickly, so that the coal and oxidizer are mixed quickly and well. That is.
（発明が解決しようとする課題〕
噴流層石炭ガス化法では、石炭等の原料を微粉にし、さ
らに原料の灰の溶融温度以上にガス化室６７の温度を高
めるので、ガス化運転時にはバーナ６８および６９を設
置している炉壁６１を灰の溶融物であるスラグが流下す
る。ガス化時には、原料ノズル１２２および酸化剤噴出
ノズル１２３から原料および酸化剤を噴出しているので
、スラグ６６が上記ノズル類を覆うことはない。ガス化
運転を停止するときには、原料ｌおよび酸化剤４０の供
給を停止するが、上述したように噴流層ガス化法では炉
内を溶融温度以上の高温にしており、原料の供給を停止
しても、時間おくれにより、炉内には溶融スラグ６６が
存在し、炉壁６１にはスラグ６６が流下している。した
がって、炉壁に設置しているバーナ６８および６９の上
方からスラグ６６が流下することになり、バーナ１面１
２４（第９図）を覆うようになる。このため、再び、ガ
ス化炉を起動しようとしても、上記ノズル出口がスラグ
で覆われているため、原料および酸化剤が供給できない
ことになる。各ノズルの出口がスラグで覆われるのを防
止しようとして原料の供給を停止して、原料搬送ガスの
み供給すれば、原料噴出ノズル１２２でのスラグの付着
を防止できる。(Problems to be Solved by the Invention) In the spouted bed coal gasification method, raw materials such as coal are pulverized and the temperature of the gasification chamber 67 is raised above the melting temperature of the raw material ash. Slag, which is a molten ash, flows down the furnace wall 61 where the ash and ash 69 are installed.During gasification, the raw material and oxidizer are spouted from the raw material nozzle 122 and the oxidizer jet nozzle 123, so the slag 66 flows down. The nozzles mentioned above are not covered.When stopping the gasification operation, the supply of the raw material 1 and the oxidizing agent 40 is stopped, but as mentioned above, in the spouted bed gasification method, the temperature inside the furnace is raised to a temperature higher than the melting temperature. Therefore, even if the supply of raw materials is stopped, molten slag 66 still exists in the furnace due to the time lag, and the slag 66 flows down the furnace wall 61. Therefore, the burner 68 installed on the furnace wall The slag 66 flows down from above the burner 1 side 1.
24 (Figure 9). Therefore, even if an attempt is made to start up the gasifier again, the nozzle outlet is covered with slag, and the raw material and oxidizer cannot be supplied. In order to prevent the outlet of each nozzle from being covered with slag, the supply of the raw material is stopped and only the raw material carrier gas is supplied, thereby preventing slag from adhering to the raw material spouting nozzle 122.
しかし、酸化剤ノズル１２３については、前記ガス化法
では酸素あるいは空気を酸化剤に使用しており、炉内に
はガス化によって住成したＣＯおよび）Ｉｔに富む生成
ガスが存在しているので、非常に危険であり、石炭等の
原料を停止した後に酸化剤のみ供給することはできない
。したがって、停止するたびに、炉内の温度が充分下が
った後にバーナ６８および６９をガス化炉６０より取出
し、バーナ端面１２４に付着したスラグを除去するしか
なかった。このとき、バーナ先端部１２４を覆うスラグ
は、炉壁６１に付着しているスラグとつながっており、
また耐火材の表面を覆っているため、バーナ端面１２４
のスラグだけを除去しようとしても、炉壁６１の耐火物
までも剥離させてしまう欠点があった。したがって、従
来法では毎日起動、停止を繰返す運転はできなかった。However, regarding the oxidizing agent nozzle 123, since oxygen or air is used as an oxidizing agent in the gasification method described above, there is a generated gas rich in CO and ) It formed by gasification in the furnace. However, it is very dangerous and it is not possible to supply only the oxidizer after stopping the raw materials such as coal. Therefore, every time the furnace is stopped, the burners 68 and 69 have to be taken out from the gasifier 60 after the temperature inside the furnace has sufficiently decreased, and the slag adhering to the burner end face 124 has to be removed. At this time, the slag covering the burner tip 124 is connected to the slag attached to the furnace wall 61,
In addition, since the surface of the refractory material is covered, the burner end face 124
Even if an attempt was made to remove only the slag, the refractory material on the furnace wall 61 would also come off. Therefore, with the conventional method, it was not possible to repeatedly start and stop the system every day.
本発明の目的は、上記した従来技術の欠点をなくし、さ
らにバーナ先端部の各ノズル出口にスラグが付着するの
を防止し、特に安定して起動、停止ができ、信韻性の高
い噴流層式微粉固体燃料ガス化装置およびその運転方法
を提供するにある。The purpose of the present invention is to eliminate the above-mentioned drawbacks of the prior art, further prevent slag from adhering to each nozzle outlet at the tip of the burner, and provide a spouted bed that can be started and stopped particularly stably and has high reliability. The present invention provides a pulverized solid fuel gasifier and a method for operating the same.
〔！１題を解決するための手段〕
上記した目的は、酸化剤供給ラインに窒素ガス、炭酸ガ
ス、蒸気等の酸素を含まないガスを供給するラインを設
置し、ガス化炉内の温度に対応して、該酸化剤供給ライ
ンに供給する上記ガス供給量を制御することによって達
成される。[! Means for Solving Problem 1] The above purpose is to install a line that supplies oxygen-free gas such as nitrogen gas, carbon dioxide gas, or steam in the oxidizer supply line, and to adjust the temperature in the gasifier. This is achieved by controlling the amount of gas supplied to the oxidizing agent supply line.
すなわち、本発明は、噴ｆＬ層ガス化炉と、このガス化
炉内に微粉固体燃料と酸化剤を噴出するバーナと、バー
ナに微粉固体燃料を供給する管路および酸化剤を供給す
る管路とを備えた噴流層式微粉固体燃料ガス化装置にお
いて、酸化剤供給管路に切換装置を介して接続された不
活性ガス供給管路と、ガス化炉内の温度検出装置と、酸
化剤の供給量測定装置と、酸化剤の供給量が設定値以下
で、かつガス化炉内の温度が所定値以上の条件を検知す
る装置と、この検知結果に基づき酸化剤供給管路を不活
性ガス供給管路に切換装置を介して切換える装置とを設
けたことを特徴とする噴流層式微粉固体燃料ガス化装！
および噴流層式ガス化炉内にノズル装置を介して微粉固
体燃料と酸化剤とを供給して微粉固体燃料をガス化する
噴流層式微粉固体燃料ガス化装置の運転方法において、
微粉固体燃料の供給を停止した状態で、ガス化炉内の温
度が微粉固体燃料中の灰分Φ溶融温度以上で、かつ酸化
剤の供給量が所定値以下の場合に、ノズル装置への酸化
剤の供給を停止して不活性ガスを供給することを特徴と
する噴流層式微粉固体燃料ガス化装置の運転方法に関す
る。That is, the present invention provides a blower layer gasifier, a burner for spouting pulverized solid fuel and an oxidizer into the gasifier, a pipe line for supplying the pulverized solid fuel to the burner, and a pipe line for supplying the oxidizer. In the spouted bed type pulverized solid fuel gasifier, the inert gas supply pipe is connected to the oxidizer supply pipe via a switching device, the temperature detection device in the gasifier, and the oxidizer A supply amount measuring device, a device that detects the conditions where the oxidant supply amount is below a set value and the temperature inside the gasifier is above a predetermined value, and based on the detection results, the oxidant supply pipe is connected to an inert gas. A spouted bed type pulverized solid fuel gasification system characterized by having a switching device installed in the supply pipe line via a switching device!
And in a method of operating a spouted bed type pulverized solid fuel gasifier, which gasifies the pulverized solid fuel by supplying pulverized solid fuel and an oxidizing agent into the spouted bed type gasifier through a nozzle device,
When the supply of pulverized solid fuel is stopped and the temperature inside the gasifier is higher than the ash melting temperature of Φ in the pulverized solid fuel, and the amount of oxidizer supplied is below a predetermined value, the oxidizer is supplied to the nozzle device. The present invention relates to a method of operating a spouted bed type pulverized solid fuel gasifier, characterized in that the supply of inert gas is stopped and inert gas is supplied.
（作用〕
酸化剤噴出ノズルからは、酸素、空気等の酸化剤の他に
窒素、炭酸ガスなどのガスをも噴出できる。したがって
、ガス化炉内の温度を検出する手段を設置し、石炭等固
体原料および酸化剤が供給されておらず、かつ、炉内温
度が原料の灰の溶融温度以上のときに、酸化剤噴出ノズ
ルから窒素、炭酸ガス、蒸気等の酸素を含まないガスを
供給することによって、酸化剤噴出ノズルにスラグが付
着することを防止できる。その結果、ガス化炉の運転お
よび停止時に関係なく、常に酸化剤および原料噴出ノズ
ルがスラグで覆われることがなくなるので、停止後にバ
ーナを取外すこともなく、また取外すことによる炉壁の
耐火材の剥離もなく、再度簡単に起動できる。(Function) In addition to oxidizing agents such as oxygen and air, gases such as nitrogen and carbon dioxide can also be ejected from the oxidizing agent injection nozzle. When solid raw materials and oxidizing agents are not supplied and the temperature inside the furnace is higher than the melting temperature of the raw material ash, supplying oxygen-free gas such as nitrogen, carbon dioxide, steam, etc. from the oxidizing agent jet nozzle. By doing so, it is possible to prevent slag from adhering to the oxidant jetting nozzle.As a result, the oxidizing agent and raw material jetting nozzle are not always covered with slag regardless of whether the gasifier is in operation or stopped. It is easy to start up again without removing the burner, and without peeling off the refractory material on the furnace wall due to removal.
以下、本発明の実施例を図面に基づいて説明する。 Embodiments of the present invention will be described below based on the drawings.
実施例１
第１図は、本発明の一実施例の石炭ガス化装置の系統図
である。この装置は、第８図の装置と同じく原料として
の微粉炭１および原料搬送ガスとしての窒素３０と酸化
剤４０とを供給するバーナ６８および６９を、ガス化室
６７の上段および下段に設置している。この装置と第８
図と異なる点は、ガス化炉内に、熱電対のごとく炉内の
温度を検出する手段７０あるいは７１が設置され、その
信号が制御器８０に入り、また酸化剤ライン４１および
４２の制御弁４３および４４の下流に、窒素、炭酸ガス
、蒸気等の酸化剤と反応しない不活性ガス５０を供給す
るライン５３および５４が接続され、該ガス５０の供給
量が制御器８０からの信号で弁５１および５２によって
制′４ｎされる点である。Example 1 FIG. 1 is a system diagram of a coal gasifier according to an example of the present invention. In this device, burners 68 and 69 for supplying pulverized coal 1 as a raw material, nitrogen 30 as a raw material carrier gas, and an oxidizing agent 40 are installed in the upper and lower stages of a gasification chamber 67, as in the device shown in FIG. ing. This device and the 8th
The difference from the diagram is that a means 70 or 71 for detecting the temperature inside the furnace, such as a thermocouple, is installed in the gasifier, and the signal is sent to a controller 80, and control valves for the oxidizer lines 41 and 42 are installed in the gasifier. Lines 53 and 54 supplying an inert gas 50 that does not react with the oxidizing agent, such as nitrogen, carbon dioxide, or steam, are connected downstream of the gases 43 and 44, and the supply amount of the gas 50 is controlled by a signal from a controller 80. 51 and 52.
第２図には、第１図のガス１ヒ装置の制御方法の一例を
示す。酸化剤供給量が設定値Ｏｓ以下で、かつ熱電対７
０あるいは７１で検出した炉内温度が設定値Ｔｓ以上の
温度であるとき、酸化剤供給ライン４１および４２から
、窒素のごとく酸素を含まないガスの供給を行ない制御
するものである。FIG. 2 shows an example of a method of controlling the gas supply device shown in FIG. 1. The oxidizer supply amount is below the set value Os, and the thermocouple 7
When the temperature inside the furnace detected at 0 or 71 is higher than the set value Ts, a gas not containing oxygen, such as nitrogen, is supplied from the oxidizing agent supply lines 41 and 42 for control.
ここで、温度の設定値Ｔｓとは、炉内のスラグが溶融し
ているかどうかを判別する温度であり、炉内下部の温度
を７０で直接計測できるならば、スラグの溶融温度を基
準にした温度であり、炉出口の温度を７１で測定し、炉
内の温度を推定した値でもよい。この設定温度Ｔｓは、
安全を見れば原料の灰の溶融温度よりも約ｌＯＯから３
００ ’Ｃ低い値に設定すればよい。また、酸化剤供給
量の設定値Ｏｓとは、一般にＯあるいは流量の検出限界
付近の値である。Here, the temperature set value Ts is the temperature that determines whether or not the slag in the furnace is melted, and if the temperature in the lower part of the furnace can be directly measured at 70, The temperature may be a value obtained by measuring the temperature at the furnace outlet at 71 and estimating the temperature inside the furnace. This set temperature Ts is
To be safe, the melting temperature of the raw material ash is about 10 to 3
It is sufficient to set it to a low value of 00'C. Further, the set value Os of the oxidizing agent supply amount is generally a value near the detection limit of O or the flow rate.
さらに第３図は、第２図のガス化装置の制御方法を適用
したときの搬送ガス、酸化剤流量、原料供給量、酸素を
含まないガス流量および炉内温度の時間経過を示す図で
ある。ここで上述の設定値は、スラグの溶融温度でＴｓ
、酸化剤供給量は０よりも若干高いＯ３としている。ガ
ス化炉の起動時、スラグタップよりも下方にあるバーナ
６５で点火し、炉内を昇温するのであるが、時間も、の
ときに酸化剤４０を供給しておらず、さらに炉内温度が
スラグの溶融温度以上になったとき、制御弁５１および
５２を開き、バーナの酸化剤噴出ノズル１２３から窒素
のようなガス５０を噴出するのである。炉内がスラグの
溶融温度よりも高くなり、炉壁に原料あるいは固化した
スラグがあればスラグは溶融して流下するが第２図に示
す制ｆ１１１方法を採用することによって、酸化剤噴出
ノズル１２３からは不活性ガスが噴出しているので、ス
ラグによってノズル出口１２３が閉塞することはない。Furthermore, FIG. 3 is a diagram showing the time course of the carrier gas, oxidizer flow rate, raw material supply amount, oxygen-free gas flow rate, and furnace temperature when the control method for the gasifier shown in FIG. 2 is applied. . Here, the above setting value is Ts at the melting temperature of the slag.
, the oxidizing agent supply amount is set to O3, which is slightly higher than 0. When starting up the gasifier, the burner 65 located below the slag tap is ignited to raise the temperature inside the furnace, but at the time of , the oxidizer 40 was not being supplied, and the temperature inside the furnace was rising. When the temperature exceeds the melting temperature of the slag, the control valves 51 and 52 are opened, and a gas 50 such as nitrogen is jetted from the oxidizer jet nozzle 123 of the burner. If the temperature inside the furnace becomes higher than the melting temperature of slag and there is raw material or solidified slag on the furnace wall, the slag will melt and flow down. Since inert gas is ejected from the nozzle outlet 123, the nozzle outlet 123 will not be blocked by slag.
微粉炭のごとき固体原料と酸化剤を供給し、設定値Ｏ３
を越えればバルブ５１および５２を閉じて、酸素を含ま
ないガス５０の供給を停止する。Supply solid raw material such as pulverized coal and oxidizing agent to set value O3.
If the oxygen-free gas exceeds this value, valves 51 and 52 are closed to stop the supply of oxygen-free gas 50.
次に、ガス化炉の停止のときであるが、原料供給量を減
少し、時間がＬ３のとき、酸化剤４０の供給量が設定値
Ｏ８以下になり、かつ炉内温度が設定値のＴｓよりも高
い温度であるとき、窒素のごとく酸素を含まないガス５
０を供給する。そして時間ｔ４ で、炉内温度が設定値
のＴｓよりも低くなったときに、上記ガス５０の供給を
停止する。Next, when the gasifier is stopped, the feed rate of the raw material is reduced, and when the time is L3, the feed rate of the oxidizing agent 40 becomes less than the set value O8, and the temperature inside the furnace is the set value Ts. A gas that does not contain oxygen, such as nitrogen, when the temperature is higher than 5
Supply 0. Then, at time t4, when the temperature inside the furnace becomes lower than the set value Ts, the supply of the gas 50 is stopped.
このように制御することによって、炉壁に溶融スラグが
存在する間は、酸化剤噴出ノズル１２３にはガスを流し
ているので、スラグが酸化剤噴出ノズル１２３を閉塞す
ることがない。By controlling in this way, gas is allowed to flow through the oxidizer jet nozzle 123 while molten slag is present on the furnace wall, so that the slag does not block the oxidizer jet nozzle 123.
その結果、本発明によって、ガス化炉を停止するたびに
、バーナをガス化炉より取出し、バーナ先端部に付着し
たスラグを除去する必要がなくなる。したがって、バー
ナ解放に伴う炉壁の耐火物の剥離もなくなる。一般にガ
ス化炉はコンパクトにするため、約５０ａｔｇの高圧機
器であるので、バーナ６８および６９を解放点検した後
には当然パツキン等を交換する必要があったが、本発明
ではその必要がなくなる。また、本発明により、解放点
検およびスラグの除去等の必要もないため、運転コスト
を大幅に低減することもできるのである。したがって、
例えば、毎日の起動、停止沖転も容易にできるのである
。なお、酸化剤噴出ノズルからのガス流速については本
発明者らの実験によれば、圧力にほとんど関係な（、最
低５ｍ／ｓ以上であれば溶融スラグを除去できた。した
がって、安全を考慮すれば、酸化剤および酸素を含まな
いガスで上述のガス噴出流速以上のになるように制御す
ればよい。As a result, the present invention eliminates the need to take out the burner from the gasifier and remove the slag attached to the tip of the burner each time the gasifier is stopped. Therefore, peeling of the refractory material on the furnace wall when the burner is released is also eliminated. Generally, in order to make the gasifier compact, it is a high-pressure device of about 50 atg, so it was naturally necessary to replace the gaskets etc. after opening and inspecting the burners 68 and 69, but this is not necessary with the present invention. Further, according to the present invention, there is no need for release inspection, slag removal, etc., so operating costs can be significantly reduced. therefore,
For example, daily starting and stopping operations can be easily performed. According to experiments conducted by the present inventors, the gas flow rate from the oxidizing agent jet nozzle has little to do with the pressure (molten slag could be removed if it was at least 5 m/s or higher. Therefore, it is important to consider safety. For example, the gas may be controlled to have a flow rate higher than the above-mentioned gas ejection flow rate using a gas that does not contain an oxidizing agent or oxygen.
実施例２
第４図は、本発明の他の実施例のガス化炉装置の系統図
である。第１図では、炉内のスラグの溶融状態を検出す
る手段として、例えば熱電対を用い、炉内の温度を検出
して、その信号を制御信号として用いたが、第４図の装
置では、スラグタップ６３から流れるスラグの流下状況
を、例えば赤外線カメラ７３による画像解析、あるいは
通常のテレビカメラ７３による可視画像の画像解析装置
７４により、スラグ６６の流下状況を検出し、その信号
を制御信号８７として用いるものである。Embodiment 2 FIG. 4 is a system diagram of a gasifier apparatus according to another embodiment of the present invention. In FIG. 1, as a means for detecting the molten state of the slag in the furnace, for example, a thermocouple is used to detect the temperature in the furnace, and the signal is used as a control signal. However, in the apparatus shown in FIG. The flow state of the slag 66 flowing from the slag tap 63 is detected by image analysis using an infrared camera 73, for example, or by an image analysis device 74 of a visible image from a normal television camera 73, and the flow state of the slag 66 is detected as a control signal 87. It is used as a.
この装置は、特にガス化炉の停止時に有効であり、スラ
グが流下し、また酸化剤４０が供給されている場合は不
活性ガス５０を供給せず、酸化剤供給量が設定値Ｏ８以
下で、画像解析によればスラグタップ６３からスラグが
流下している場合は不活性ガス５０を酸化剤ライン４１
および４２から供給して酸化剤噴出ノズル１２３より噴
出するものである。ここで、画像解析は、スラグタップ
６３の断面積の変化あるいは温度分布そのものによって
、スラグが流下しているかどうかを解析するものである
。第１図では、原料の溶融温度をあらかじめ分析し、そ
れを参考に制御系に入力する必要があるが、第４図の装
置では、実際に炉内の温度がスラグ溶融状態かどうかを
直接判定するために、溶融温度は特に計測する必要がな
く、また運転中に原料の性状が変化したときでも有効で
ある。This device is particularly effective when the gasifier is stopped, and when the slag is flowing down and the oxidizer 40 is being supplied, the inert gas 50 is not supplied, and the oxidizer supply amount is less than the set value O8. According to the image analysis, if slag is flowing down from the slag tap 63, the inert gas 50 is transferred to the oxidizer line 41.
and 42 and is ejected from the oxidant ejection nozzle 123. Here, the image analysis is to analyze whether the slag is flowing down based on a change in the cross-sectional area of the slag tap 63 or the temperature distribution itself. In Fig. 1, it is necessary to analyze the melting temperature of the raw material in advance and input it into the control system with reference to it, but with the device shown in Fig. 4, it is possible to directly determine whether the temperature inside the furnace is actually in the slag melting state. Therefore, there is no need to particularly measure the melting temperature, and it is effective even when the properties of the raw material change during operation.
実施例３
第５図は、本発明の装置の他の運転方法における時間経
過を示す図である。この方法は、ガス化炉を停止する前
に酸化剤４０の供給量を増加させて炉内６７の温度を上
昇させ、炉内の溶融スラグ６６の粘度を減少させた後で
、炉内温度が設定温度Ｔｓよりも高い温度ならば、酸化
剤供給ライン４１および４２より、酸素を含まないガス
５ｏを供給し、酸化剤噴出ノズル１２３より、ガスを噴
出させて、炉壁を流下するスラグ６６が、該ノズルの出
口１２３を覆い、閉塞するのを防止するものである。こ
のように、炉内の温度を停止前に上昇させてスラグの粘
度を減少することによって、ガス噴出による溶融スラグ
の除去作用が大きく、また炉内で溶融してい゛るスラグ
の晴を減少できるので、バーナ端面に付着するスラグ量
も減少する。Example 3 FIG. 5 is a diagram showing the passage of time in another method of operating the apparatus of the present invention. In this method, before stopping the gasifier, the supply amount of the oxidizing agent 40 is increased to raise the temperature in the furnace 67, and after the viscosity of the molten slag 66 in the furnace is decreased, the temperature in the furnace is increased. If the temperature is higher than the set temperature Ts, oxygen-free gas 5o is supplied from the oxidizing agent supply lines 41 and 42, and the gas is ejected from the oxidizing agent injection nozzle 123, so that the slag 66 flowing down the furnace wall is , to cover the outlet 123 of the nozzle and prevent it from clogging. In this way, by increasing the temperature inside the furnace and reducing the viscosity of the slag before stopping, the removal effect of the molten slag by the gas jet is greater, and the amount of slag molten inside the furnace can be reduced. Therefore, the amount of slag adhering to the burner end face is also reduced.
したがって、この方法によればスラグによるノズル閉塞
のトラブルの危険性が小さくなる。Therefore, this method reduces the risk of nozzle clogging problems caused by slag.
実施例４
第６図は、本発明のさらに他のガス化装置の概略系統図
である。この装置は、微わ）炭等の原料供給系の他に、
石灰石、鉄鉱石等スラグの溶融温度を低下する添加剤を
供給する系統、添加側供給ホッパー１００、フィーダ１
０３などを有するものである。第７図は、このガス化炉
の運転方法における経時変化を示す図である。前述の実
施例３では、スラグの粘度を減少するために酸化剤４０
の量を増加させたが、本実施例では、スラグの粘度を減
少させる手段として、添加剤を用いるものである。すな
わち、ガス化炉を停止する前に該添加剤を炉内に供給さ
せて、スラグの）容量温度を低下することによって、溶
融スラグ６６の粘度を減少させ、その後に、炉内温度が
設定温度Ｔｓよりも低い温度になるまで、酸化剤供給ラ
イン４１および４２より、酸化剤とは反応しないガス５
ｏを供給するものである。そして、酸化剤噴出ノズル１
２３より、ガスを噴出させて、炉壁を流下するスラグ６
６が該ノズルの出口を覆い、閉塞するのを防止するので
ある。このように、スラグの粘度を減少することによっ
て、ガス噴出による溶融スラグの除去作用が大きく、ま
た炉内で）容量しているスラグの情を減少できるので、
バーナ端面に付着するスラグ量も減少するため、スラグ
によるノズル閉塞のトラブルの危険性が小さくなる。Embodiment 4 FIG. 6 is a schematic system diagram of still another gasifier of the present invention. In addition to the supply system for raw materials such as charcoal, this equipment
System for supplying additives that lower the melting temperature of slag such as limestone and iron ore, addition side supply hopper 100, feeder 1
03 etc. FIG. 7 is a diagram showing changes over time in the operating method of this gasifier. In the aforementioned Example 3, oxidizer 40 was added to reduce the viscosity of the slag.
However, in this example, an additive is used as a means to reduce the viscosity of the slag. That is, the viscosity of the molten slag 66 is reduced by supplying the additive into the furnace before stopping the gasification furnace to lower the volumetric temperature of the slag, and then the temperature inside the furnace reaches the set temperature. A gas 5 that does not react with the oxidant is supplied from the oxidant supply lines 41 and 42 until the temperature becomes lower than Ts.
o. And oxidant jet nozzle 1
From 23, gas is ejected and the slag 6 flows down the furnace wall.
6 covers the outlet of the nozzle and prevents it from clogging. In this way, by reducing the viscosity of the slag, the removal effect of the molten slag by gas jetting is greater, and the amount of slag (in the furnace) can be reduced.
Since the amount of slag adhering to the burner end face is also reduced, the risk of nozzle clogging problems due to slag is reduced.
実施例５
第１０図に示す内部混合型バーナを使用する際も、本発
明を適用可能である。微粉固体燃料と搬送ガス（Ｎ、ま
たは空気）の混合体１２１は、原料ノズル１２２から噴
射される。酸化剤（Ｏ２または空気）４０は、酸化剤噴
出ノズル１２３を通じて、原料ノズル１２２の出口端よ
り手前の部分に合流するようになっている。このような
内部混合型バーナを使用する場合も、ガス化炉内の温度
が所定値以上で、かつ酸化剤の供給量が設定値以下にな
ったとき、酸化剤の供給を不活性ガスの供給に切換える
のである。Embodiment 5 The present invention can also be applied when using the internal mixing type burner shown in FIG. 10. A mixture 121 of pulverized solid fuel and carrier gas (N or air) is injected from a raw material nozzle 122 . The oxidizing agent (O2 or air) 40 passes through the oxidizing agent jetting nozzle 123 and flows into a portion of the raw material nozzle 122 in front of the outlet end thereof. Even when using such an internal mixing type burner, when the temperature inside the gasifier is above a predetermined value and the oxidizer supply amount is below the set value, the oxidizer supply is replaced by an inert gas supply. It is switched to .
内部混合型バーナの停止時には、微粉固体燃料の供給お
よび酸化剤の供給を停止しても、燃料搬送管路内に残留
した燃料が短時間（２〜３分）ではあるがバーナから噴
出する。その際、酸化剤供給路に燃料が逆流する危険性
があり、逆流した燃料が酸化剤供給路に堆積すると、運
転中に爆発が生じる危険がある。本発明を実施すること
により、上述の危険を防止できる。When the internal mixing type burner is stopped, even if the supply of the pulverized solid fuel and the oxidizer are stopped, the fuel remaining in the fuel conveyance pipe is ejected from the burner for a short time (2 to 3 minutes). At this time, there is a risk that fuel will flow back into the oxidizer supply path, and if the fuel that flows back is deposited in the oxidizer supply path, there is a risk that an explosion will occur during operation. By implementing the present invention, the above-mentioned dangers can be prevented.
本発明によれば、バーナ先端の各ノズル出口部にスラグ
が付着することがないので、安全にかつ効率よく運転す
ることができる。According to the present invention, since slag does not adhere to each nozzle outlet portion at the tip of the burner, the burner can be operated safely and efficiently.
第１図は、本発明の一実施例の装置系統図、第２図は、
第１図の運転フロー図、第３図は、第２図の運転フロー
の説明図、第４図は、本発明の他の実施例の装置系統図
、第５図は、第４図の運転フロー図、第６図は、本発明
のさらに他の実施例の装置系統図、第７図は、第６図の
運転フロー図、第８図は、従来のガス化装置の系統図、
第９図および第Ｎｏ図は、ガス化装置に使用されるバー
ナの断面図である。
■・・・微粉固体原料、１０・・・常圧ホッパー、１４
・・・加圧ホッパー １７・・・供給ホッパー、３０・
・・搬送ガス、３３・・・エゼクタ、３５．３６・・・
微粉固体供給管路、４０・・・酸化剤、４１．４２・・
・酸化剤供給管路、４３．４４・・・酸化剤供給制御弁
、５０・・・不活性ガス、５１．５２・・・不活性ガス
供給制御弁、５３．５４・・・不活性ガス供給管路、６
０・・・ガス化炉本体、６３・・・スラグタップ、６５
・・・点火、１ｍバーナ、６６・・・スラグ、６７・・
・ガス化室、６８、。
６９・・・バーナ、７０．７１・・・熱電対、７３・・
・赤外線カメラ、８０・・・制御機、８１〜８６・・・
制御ライン、１２２・・・原料ノズル、１２３・・・酸
化剤噴出ノズル、１２４・・・バーナ端面。
出願人 バブコック日立株式会社
代理人 弁理士 川 北 武 長
１：微粉固体原料
１０：常圧ホッパ
＋４：加圧ホッパ
＋７：供給ホッパ
３０：搬送ガス
３３：エゼクタ
３５．３６：微粉固体像Ｃイソ
４３．４４
５１、５２
３Ｊ４
Ｊ６９
７０．７１
酸化剤供給制御弁
不活性ガス
不活性ガス供給制御弁
不活性ガス供給ライン
ガス化炉本体
スラグタップ
点 火・昇温バーナ
スラグ
ガス化室
ノ（−す
熱電対
８１〜８６：制御ライン
原
第３
図
第
図
時
間FIG. 1 is a system diagram of an apparatus according to an embodiment of the present invention, and FIG.
FIG. 1 is an operation flow diagram, FIG. 3 is an explanatory diagram of the operation flow in FIG. 2, FIG. 4 is an apparatus system diagram of another embodiment of the present invention, and FIG. Flowchart, FIG. 6 is an apparatus system diagram of still another embodiment of the present invention, FIG. 7 is an operation flow diagram of FIG. 6, and FIG. 8 is a system diagram of a conventional gasification apparatus.
FIGS. 9 and 9 are cross-sectional views of burners used in the gasifier. ■...Fine powder solid raw material, 10...Normal pressure hopper, 14
... Pressure hopper 17 ... Supply hopper, 30.
...Carrier gas, 33...Ejector, 35.36...
Fine powder solid supply pipe, 40... Oxidizing agent, 41.42...
- Oxidizing agent supply pipe line, 43.44... Oxidizing agent supply control valve, 50... Inert gas, 51.52... Inert gas supply control valve, 53.54... Inert gas supply conduit, 6
0...Gasifier body, 63...Slag tap, 65
...Ignition, 1m burner, 66...Slag, 67...
- Gasification chamber, 68. 69...Burner, 70.71...Thermocouple, 73...
・Infrared camera, 80...Controller, 81-86...
Control line, 122... Raw material nozzle, 123... Oxidizer jet nozzle, 124... Burner end face. Applicant Babcock Hitachi Co., Ltd. Agent Patent Attorney Takeshi Kawakita 1: Fine powder solid raw material 10: Normal pressure hopper + 4: Pressure hopper + 7: Supply hopper 30: Carrier gas 33: Ejector 35.36: Fine powder solid image C iso 43 .44 51, 52 3J4 J69 70.71 Oxidizing agent supply control valve Inert gas Inert gas supply control valve Inert gas supply line Gasification furnace main body slag tap point Fire/heating burner slag gasification chamber (-) thermoelectric Pairs 81 to 86: Control line original figure 3 figure time
Claims (3)
料と酸化剤を噴出するバーナと、バーナに微粉固体燃料
を供給する管路および酸化剤を供給する管路とを備えた
噴流層式微粉固体燃料ガス化装置において、酸化剤供給
管路に切換装置を介して接続された不活性ガス供給管路
と、ガス化炉内の温度検出装置と、酸化剤の供給量測定
装置と、酸化剤の供給量が設定値以下で、かつガス化炉
内の温度が所定値以上の条件を検知する装置と、この検
知結果に基づき酸化剤供給管路を不活性ガス供給管路に
切換装置を介して切換える装置とを設けたことを特徴と
する噴流層式微粉固体燃料ガス化装置。(1) A spouted bed gasifier, a burner for spouting pulverized solid fuel and an oxidizer into the gasifier, a pipe for supplying the pulverized solid fuel to the burner, and a pipe for supplying the oxidizer. In a spouted bed type pulverized solid fuel gasifier, an inert gas supply pipe connected to the oxidizer supply pipe via a switching device, a temperature detection device in the gasifier, and an oxidizer supply amount measurement device and a device that detects the conditions when the oxidizer supply amount is below a set value and the temperature inside the gasifier is above a predetermined value, and based on the detection results, the oxidizer supply pipe is replaced with an inert gas supply pipe. What is claimed is: 1. A spouted bed type pulverized solid fuel gasification device, characterized in that it is provided with a device for switching via a switching device.
体燃料と酸化剤とを供給して微粉固体燃料をガス化する
噴流層式微粉固体燃料ガス化装置の運転方法において、
微粉固体燃料の供給を停止した状態で、ガス化炉内の温
度が微粉固体燃料中の灰分の溶融温度以上で、かつ酸化
剤の供給量が所定値以下の場合に、ノズル装置への酸化
剤の供給を停止して不活性ガスを供給することを特徴と
する噴流層式微粉固体燃料ガス化装置の運転方法。(2) In a method of operating a spouted bed type pulverized solid fuel gasifier, which gasifies the pulverized solid fuel by supplying pulverized solid fuel and an oxidizing agent into the spouted bed type gasifier through a nozzle device,
When the supply of pulverized solid fuel is stopped and the temperature inside the gasifier is higher than the melting temperature of the ash in the pulverized solid fuel, and the amount of oxidizer supplied is below a predetermined value, the oxidizer is supplied to the nozzle device. A method for operating a spouted bed type pulverized solid fuel gasifier, characterized by stopping the supply of gas and supplying inert gas.
固体燃料の供給を停止する前に、上記燃料中の灰分の溶
融物の粘度低下操作を行ない、その後ノズル装置への酸
化剤の供給を停止して不活性ガスを供給するようにした
ことを特徴とする噴流層式微粉固体燃料ガス化装置の運
転方法。(3) In claim (2), before stopping the supply of the pulverized solid fuel into the gasifier, an operation is performed to reduce the viscosity of the ash melt in the fuel, and then the oxidizing agent is supplied to the nozzle device. 1. A method for operating a spouted bed type pulverized solid fuel gasifier, characterized in that the supply of gas is stopped and inert gas is supplied.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4281489A JPH0776345B2 (en) | 1989-02-22 | 1989-02-22 | Spouted bed type fine powder solid fuel gasifier and its operating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4281489A JPH0776345B2 (en) | 1989-02-22 | 1989-02-22 | Spouted bed type fine powder solid fuel gasifier and its operating method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02219893A true JPH02219893A (en) | 1990-09-03 |
| JPH0776345B2 JPH0776345B2 (en) | 1995-08-16 |
Family
ID=12646418
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4281489A Expired - Lifetime JPH0776345B2 (en) | 1989-02-22 | 1989-02-22 | Spouted bed type fine powder solid fuel gasifier and its operating method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0776345B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105400550A (en) * | 2015-09-30 | 2016-03-16 | 中国石油化工股份有限公司 | Apparatus for preventing slag adhering to slag screen of slag-tap gasifier |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010163499A (en) * | 2009-01-13 | 2010-07-29 | Electric Power Dev Co Ltd | Method for operating entrained-bed gasification furnace |
| KR101096632B1 (en) | 2009-12-10 | 2011-12-21 | 에스케이이노베이션 주식회사 | Top feeding dual swirling gasifier |
-
1989
- 1989-02-22 JP JP4281489A patent/JPH0776345B2/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105400550A (en) * | 2015-09-30 | 2016-03-16 | 中国石油化工股份有限公司 | Apparatus for preventing slag adhering to slag screen of slag-tap gasifier |
| CN105400550B (en) * | 2015-09-30 | 2018-10-26 | 中国石油化工股份有限公司 | Prevent the device of slag tap gasifier slag screen dross |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0776345B2 (en) | 1995-08-16 |
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