JPH0335574B2 - - Google Patents
Info
- Publication number
- JPH0335574B2 JPH0335574B2 JP59269932A JP26993284A JPH0335574B2 JP H0335574 B2 JPH0335574 B2 JP H0335574B2 JP 59269932 A JP59269932 A JP 59269932A JP 26993284 A JP26993284 A JP 26993284A JP H0335574 B2 JPH0335574 B2 JP H0335574B2
- Authority
- JP
- Japan
- Prior art keywords
- combustion
- catalyst layer
- combustion catalyst
- layer
- oxidation catalyst
- 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
- 239000003054 catalyst Substances 0.000 claims description 71
- 238000002485 combustion reaction Methods 0.000 claims description 60
- 238000007254 oxidation reaction Methods 0.000 claims description 20
- 230000003647 oxidation Effects 0.000 claims description 18
- 239000000446 fuel Substances 0.000 claims description 14
- 230000003197 catalytic effect Effects 0.000 claims description 11
- 229910052751 metal Inorganic materials 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- 239000000919 ceramic Substances 0.000 claims description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims description 4
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 4
- 239000000835 fiber Substances 0.000 claims description 3
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 3
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- -1 platinum group metals Chemical class 0.000 claims description 2
- 229910052703 rhodium Inorganic materials 0.000 claims description 2
- 229910052746 lanthanum Inorganic materials 0.000 claims 1
- 229910052763 palladium Inorganic materials 0.000 claims 1
- 239000002759 woven fabric Substances 0.000 claims 1
- 239000010410 layer Substances 0.000 description 58
- 239000002737 fuel gas Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 9
- 239000006185 dispersion Substances 0.000 description 6
- 238000009792 diffusion process Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000002344 surface layer Substances 0.000 description 5
- 230000009257 reactivity Effects 0.000 description 4
- 239000007789 gas Substances 0.000 description 3
- 230000001681 protective effect Effects 0.000 description 3
- 125000006850 spacer group Chemical group 0.000 description 3
- 238000007084 catalytic combustion reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 1
- 239000010763 heavy fuel oil Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910001120 nichrome Inorganic materials 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/12—Radiant burners
- F23D14/18—Radiant burners using catalysis for flameless combustion
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、触媒体上に気体燃料あるいは気化さ
せた液体燃料を供給し、燃焼用空気によつて前記
の燃料を触媒酸化させ、その反応により生じた燃
焼熱および輻射熱を利用する触媒バーナに関す
る。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention supplies gaseous fuel or vaporized liquid fuel onto a catalyst body, catalytically oxidizes the fuel with combustion air, and oxidizes the fuel produced by the reaction. This invention relates to a catalytic burner that utilizes combustion heat and radiant heat.
従来の技術
従来この種の触媒バーナは、第２図に示すよう
に多数の小孔を有した燃料分散管１を裏面から設
置したバーナケース２内に、拡散材３とPt、Rh、
Pd等の白金族金属の内１種類以上を用いた酸化
触媒を一定の担持率で担持した単一の燃焼用触媒
層４を設けた構成になつており、燃料分散管１か
ら送入されたガス燃料は拡散材３の内部を均一に
拡散しながら燃焼用触媒層４内に至り、何らかの
着火手段で着火された後、燃焼用触媒層４の表面
上で定常的な触媒燃焼が行われるようになつてい
た。（例えば、特開昭58−213110号公報）
発明が解決しようとする問題点
しかしながら上記構成では、燃焼用触媒層４の
大気側、中央部、裏面部でそれぞれ反応性が異な
るため各部の温度も違いが生じる。特に燃焼用触
媒層の裏面部付近は燃料ガスの燃焼用空気に対す
る割合が非常に大であるため、燃焼ガスの一部し
か反応しないのに対し、燃焼触媒層の中央部に燃
料ガスが至れば、燃焼用空気の存在する割合が大
きくなり、反応は急激に進行するため急激に反応
温度は上昇する。また燃焼用触媒層４の大気側に
近い部分に燃料ガスが至る頃には、中央部で反応
しきれなかつた残余の燃料ガスが大量の拡散空気
によつて酸化されるため生じる反応熱は大ではな
く、同時に生じた反応熱を放出し、また拡散空気
の冷却作用も影響するため、最も低温部分を形成
する。したがつて、定常触媒酸化反応中の燃焼用
触媒層４の温度分布は、中央部が最も高温で、次
いで裏面付近、大気側付近となる。したがつて理
想的な酸化触媒の担持率の分布も中央部が最も多
量に必要とし、反応に関与する割合の低い裏面部
では低担持率ですみ、また燃焼用空気が大量に存
在する大気側付近は中央部よりも低担持率です
む。しかるに酸化触媒の担持率が各部で一定の単
一の燃焼用触媒層４では、反応性に対応した担持
率分布となり得ず、特に酸化触媒に白金族金属等
の高価なものを用いた場合、燃焼に必要な量の酸
化触媒量を得るためには相当な高コストを覚悟し
なければならなかつた。BACKGROUND ART Conventionally, this type of catalytic burner has a burner case 2 in which a fuel dispersion pipe 1 having a large number of small holes is installed from the back side, as shown in FIG. 2, and a diffusion material 3 and Pt, Rh,
The structure includes a single combustion catalyst layer 4 that supports an oxidation catalyst using one or more types of platinum group metals such as Pd at a constant loading rate, and the fuel is fed from the fuel distribution pipe 1. The gaseous fuel reaches the combustion catalyst layer 4 while uniformly diffusing inside the diffusion material 3, and after being ignited by some kind of ignition means, steady catalytic combustion is carried out on the surface of the combustion catalyst layer 4. I was getting used to it. (For example, Japanese Unexamined Patent Publication No. 58-213110) Problems to be Solved by the Invention However, in the above configuration, the reactivity differs between the atmosphere side, the center portion, and the back surface portion of the combustion catalyst layer 4, so the temperature of each portion also varies. It makes a difference. Particularly near the back surface of the combustion catalyst layer, the ratio of fuel gas to combustion air is very large, so only a portion of the combustion gas reacts, whereas if the fuel gas reaches the center of the combustion catalyst layer, , the proportion of combustion air present increases, and the reaction proceeds rapidly, resulting in a rapid rise in reaction temperature. Furthermore, by the time the fuel gas reaches the part of the combustion catalyst layer 4 close to the atmosphere, the residual fuel gas that has not completely reacted in the central part is oxidized by a large amount of diffused air, so the reaction heat generated is large. Rather, the reaction heat generated at the same time is released, and the cooling effect of the diffused air also affects the temperature, so it forms the lowest temperature region. Therefore, the temperature distribution of the combustion catalyst layer 4 during the steady catalytic oxidation reaction has the highest temperature at the center, followed by the back surface and the atmosphere side. Therefore, the ideal distribution of the oxidation catalyst loading rate requires the largest amount in the central area, a lower loading rate in the back area where the proportion involved in the reaction is low, and the atmospheric side where a large amount of combustion air exists. The surrounding area requires a lower loading rate than the central area. However, in a single combustion catalyst layer 4 in which the oxidation catalyst loading rate is constant in each part, it is not possible to achieve a loading rate distribution that corresponds to the reactivity, especially when an expensive oxidation catalyst such as a platinum group metal is used. In order to obtain the amount of oxidation catalyst necessary for combustion, one had to be prepared for considerably high costs.
本発明はかかる従来の問題点を解消するもの
で、燃焼用触媒体の各層を反応性に応じた触媒性
能とし、効率的な酸化反応をさせ、かつ全体的な
触媒量の節減を行うことを目的とする。 The present invention solves these conventional problems by making each layer of the combustion catalyst have catalytic performance according to its reactivity, allowing efficient oxidation reaction, and reducing the overall amount of catalyst. purpose.
問題点を解決するための手段
上記の問題点を解決するために、本発明の触媒
バーナは、耐熱性セラミツク担体に酸化触媒を担
持した燃焼用触媒体を３層に分け、燃料供給部に
近い裏面層と拡散空気に近接する表面層の部分を
中央層よりも低い担持率にしたものである。Means for Solving the Problems In order to solve the above problems, the catalytic burner of the present invention has a combustion catalyst body in which an oxidation catalyst is supported on a heat-resistant ceramic carrier, which is divided into three layers. The back layer and the surface layer close to the diffusion air have a lower loading rate than the central layer.
作 用
本発明は上記の構成によつて、燃料供給部から
供給された燃料ガスが燃焼用触媒体の裏面層で一
部反応し、温度上昇しながら最も酸化触媒の担持
率の高い中央層に至り、急激に反応が進み、同時
に急激に温度上昇しながら表面層に至る。表面層
では、燃料ガスの大半が燃焼し、未燃成分の完全
燃焼の段階となる。したがつて中央層における酸
化触媒の担持率を裏面層、表面層よりも比較的多
くして効率のよい、安価なものとなる。Effects According to the present invention, with the above configuration, the fuel gas supplied from the fuel supply part partially reacts in the back layer of the combustion catalyst, and as the temperature rises, the fuel gas is transferred to the center layer where the oxidation catalyst is supported the highest. The reaction progresses rapidly and at the same time reaches the surface layer with a rapid temperature rise. In the surface layer, most of the fuel gas is combusted, and unburned components are completely combusted. Therefore, the supporting ratio of the oxidation catalyst in the center layer is relatively higher than that in the back layer and the surface layer, resulting in a highly efficient and inexpensive product.
実施例
以下、本発明の一実施例を添付の図面に基いて
説明を行う。Embodiment An embodiment of the present invention will be described below with reference to the accompanying drawings.
第１図に於て、耐熱性金属からなるバーナケー
ス１の下部には燃料分散ノズル２が貫通設置さ
れ、通気抵抗が無視できる程度の高い開孔度を有
する金網あるいはラス網形式のスペーサ３と前記
バーナケース１によりガス室４が形成されてい
る。一方、スペーサ３から前方には、スペーサ３
に近接した部分から耐熱性セラミツク繊維成型体
からなる保温拡散材５、ニクロムヒータ線を一定
パターンで分布させた予熱器６、Al2O3・SiO2等
の微小細孔を有しかつ高い比表面積を有する耐熱
性セラミツク繊維成型体を担体とし、0.2〜0.3％
のRhの担持率を有する裏面燃焼用触媒層７、同
様の担体に0.5〜１％のRh担持率を有する中央燃
焼用触媒層８、さらに同様の担体に0.2〜0.3％の
Rh担持率を有する表面燃焼用触媒層９があり、
表面燃焼用触媒層９の前面は通気抵抗をほとんど
無視できる程度の高い開孔度を有する金網あるい
はラス網からなる保護ネツト１０によつて保持さ
れており、保護ネツト１０はその外周部を保持金
具１１によつて固定されている。また、裏面燃焼
用触媒層７と中央燃焼用触媒層８の間には燃焼温
度検知用の熱電対１２が設置されている。 In Fig. 1, a fuel dispersion nozzle 2 is installed through the lower part of a burner case 1 made of heat-resistant metal, and a spacer 3 in the form of a wire mesh or lath mesh having a high degree of aperture so that ventilation resistance can be ignored. A gas chamber 4 is formed by the burner case 1 . On the other hand, in front of spacer 3, spacer 3
A heat insulating diffusion material 5 made of a heat-resistant ceramic fiber molded body, a preheater 6 having nichrome heater wires distributed in a fixed pattern, and a material having micropores such as Al 2 O 3 / SiO 2 and having a high ratio A heat-resistant ceramic fiber molded body with a surface area of 0.2 to 0.3% is used as a carrier.
The back combustion catalyst layer 7 has a Rh loading rate of 0.5% to 1% on the same carrier, and the central combustion catalyst layer 8 has a Rh loading rate of 0.2% to 0.3% on the same carrier.
There is a surface combustion catalyst layer 9 having a Rh loading rate,
The front surface of the surface combustion catalyst layer 9 is held by a protective net 10 made of a wire mesh or lath mesh having a high degree of aperture that allows airflow resistance to be almost ignored, and the protective net 10 is held at its outer periphery by a holding metal fitting. 11. Further, a thermocouple 12 for detecting combustion temperature is installed between the back combustion catalyst layer 7 and the center combustion catalyst layer 8.
次に上記構成に於ける作用を説明する。 Next, the operation of the above configuration will be explained.
予熱器６に通電されると、発生した熱は裏面燃
焼用触媒層７から表面燃焼用触媒層９へ伝達さ
れ、裏面燃焼用触媒層７と中央燃焼触媒層８の間
の温度が一定の温度（260〜300℃）に到達するま
で通電が続行される。そして、燃焼温度検知用の
熱電対１２が一定温度以上に予熱が進んだことを
感知すると、燃料ガス供給用の電磁弁（図示せ
ず）にも通電され、燃料が供給される。供給され
た燃料ガスは燃料分散ノズル２によつてガス室４
内に充満し、保護拡散材５内を均一に拡散しなが
ら、裏面燃焼用触媒層７に至り燃料ガスの一部が
酸化され、発生した熱によつて裏面燃焼用触媒層
７、中央燃焼用触媒層８の温度が上昇する。一部
反応しながら裏面燃焼用触媒層７を通過した燃料
ガスは中央燃焼用触媒層８に至つて、内部に拡散
してくる燃焼用空気により急激に酸化され、同時
に中央燃焼用触媒層９の温度も500℃程度に急上
昇する。さらに大半が酸化された燃料ガスは表面
燃焼用触媒層９に至つてほぼ完全に酸化される。
この段階では予熱器６は必要とせず、予熱器６へ
の通電は停止される。 When the preheater 6 is energized, the generated heat is transferred from the back combustion catalyst layer 7 to the front combustion catalyst layer 9, and the temperature between the back combustion catalyst layer 7 and the center combustion catalyst layer 8 remains constant. (260 to 300°C) is reached. When the thermocouple 12 for detecting combustion temperature detects that preheating has progressed to a certain temperature or higher, a solenoid valve (not shown) for supplying fuel gas is also energized, and fuel is supplied. The supplied fuel gas is passed through the fuel dispersion nozzle 2 to the gas chamber 4.
While uniformly diffusing inside the protective diffusion material 5, a part of the fuel gas reaches the back combustion catalyst layer 7 and is oxidized, and the generated heat causes the back combustion catalyst layer 7, the center combustion The temperature of the catalyst layer 8 increases. The fuel gas that has passed through the rear combustion catalyst layer 7 while partially reacting reaches the central combustion catalyst layer 8 and is rapidly oxidized by the combustion air that diffuses inside, and at the same time the central combustion catalyst layer 9. The temperature also rises rapidly to around 500℃. Furthermore, the fuel gas, most of which has been oxidized, reaches the surface combustion catalyst layer 9 and is almost completely oxidized.
At this stage, the preheater 6 is not required, and the power supply to the preheater 6 is stopped.
この時、表面燃焼用触媒層９は中央燃焼用触媒
層での燃焼熱の伝熱と、自己の反応熱を得るが、
それにも増して輻射熱としての熱放出、拡散空気
の冷却作用が強いため、表面燃焼用触媒層９の温
度は最も低く250〜350℃程度となる。このように
して裏面燃焼用触媒層７、中央燃焼用触媒層８、
表面燃焼用触媒層９の各層での触媒燃焼は定常状
態に至る。中央燃焼用触媒層８のRh担持率は、
他の２層に比べ高くなつているが、担体として、
100〜200m2／ｇといつた高い比表面積を有し、
800〜900℃といつた高い耐熱性を有するAl2O3・
SiO2を用いているため、450〜550℃の燃焼温度
を保持している中央燃焼用触媒層８でも、触媒粒
子は比較的高分散で微粒子状態を保持できる。ま
た、表面燃焼用触媒層９の酸化触媒の担持率は中
央燃焼用触媒層８の酸化触媒の担持率よりも低い
ため、表面燃焼用触媒層９の酸化触媒粒子の分散
度は中央燃焼用触媒層８における分散度よりも高
く、極めて良好な微粒子状態を保持できる。さら
に、表面燃焼用触媒層９での反応温度が250〜350
℃程度であることからシンタリングの心配は全く
ない。 At this time, the surface combustion catalyst layer 9 receives heat of combustion from the central combustion catalyst layer and its own reaction heat, but
Moreover, since the heat release as radiant heat and the cooling effect of the diffused air are strong, the temperature of the surface combustion catalyst layer 9 is the lowest, about 250 to 350°C. In this way, the back combustion catalyst layer 7, the central combustion catalyst layer 8,
Catalytic combustion in each layer of the surface combustion catalyst layer 9 reaches a steady state. The Rh loading rate of the central combustion catalyst layer 8 is
Although it is higher than the other two layers, as a carrier,
It has a high specific surface area of 100 to 200 m 2 /g,
Al 2 O 3 with high heat resistance of 800 to 900℃.
Since SiO 2 is used, even in the central combustion catalyst layer 8 which maintains a combustion temperature of 450 to 550°C, the catalyst particles can be relatively highly dispersed and maintain a fine particle state. Furthermore, since the supporting rate of the oxidation catalyst in the surface combustion catalyst layer 9 is lower than the supporting rate of the oxidation catalyst in the central combustion catalyst layer 8, the degree of dispersion of the oxidation catalyst particles in the surface combustion catalyst layer 9 is lower than that of the central combustion catalyst layer. The degree of dispersion is higher than that in layer 8, and an extremely good state of fine particles can be maintained. Furthermore, the reaction temperature in the surface combustion catalyst layer 9 is between 250 and 350.
There is no need to worry about sintering since the temperature is about ℃.
発明の効果
以上のように本発明の触媒バーナによれば、以
下のような効果が得られる。Effects of the Invention As described above, according to the catalytic burner of the present invention, the following effects can be obtained.
(1) 燃焼用触媒体を３層に分割し、表面層と裏面
層の酸化触媒の担持率を中央層の酸化触媒の担
持率よりも少くしたことにより、中央層での反
応性よりも低い反応性を有する表面層と裏面層
に於ける酸化触媒の量を節減することができ
る。(1) The combustion catalyst body is divided into three layers, and the oxidation catalyst supported on the front and back layers is lower than the oxidation catalyst supported on the middle layer, resulting in lower reactivity than the middle layer. The amount of oxidation catalyst in the reactive surface layer and back layer can be reduced.
(2) 上記構成により、一定の担持率に固定した単
一の燃焼用触媒体の場合よりも、触媒金属の所
要量を節減することができる。(2) With the above configuration, the required amount of catalyst metal can be reduced compared to the case of a single combustion catalyst body with a fixed loading rate.
第１図は本発明の一実施例である触媒バーナの
縦断面図、第２図は従来の触媒バーナの縦断面図
である。
２……燃料分散ノズル、７……裏面燃焼用触媒
層、８……中央燃焼用触媒層、９……表面燃焼用
触媒層。
FIG. 1 is a longitudinal sectional view of a catalytic burner according to an embodiment of the present invention, and FIG. 2 is a longitudinal sectional view of a conventional catalytic burner. 2... Fuel dispersion nozzle, 7... Catalyst layer for back side combustion, 8... Catalyst layer for center combustion, 9... Catalyst layer for front side combustion.
Claims (1)
いは織布、又は多孔体等の内１種類を担体とし、
酸化触媒を担持した燃焼用触媒体を３層に分割し
燃料供給部に近い層および外気に面した層の酸化
触媒の担持率をこの２つの層の間に位置する中央
の層の酸化触媒の担持率よりも少くした触媒バー
ナ。 ２ 燃焼用触媒体の担体としてγ−Al2O3、
Al2O3・SiO2、SiO2等の多孔質かつ高い比表面積
を有するセラミツクスを用いた特許請求の範囲第
１項記載の触媒バーナ。 ３ 酸化触媒として、Pt、Pd、Rh等の白金族金
属の内１種類以上、またはLa、Co、Ce、Sr等か
らなるペロブスカイト型構造を有する酸化物等を
用いた特許請求の範囲第１項記載の触媒バーナ。[Claims] 1. A non-compressed molded body made of ceramic fiber, a woven fabric, a porous body, etc. as a carrier,
The combustion catalyst supporting the oxidation catalyst is divided into three layers, and the loading ratio of the oxidation catalyst in the layer near the fuel supply section and the layer facing the outside air is compared with that of the oxidation catalyst in the middle layer located between these two layers. Catalytic burner with lower loading rate. 2 γ-Al 2 O 3 as a support for combustion catalyst,
The catalytic burner according to claim 1, which uses ceramics such as Al 2 O 3 .SiO 2 and SiO 2 that are porous and have a high specific surface area. 3. Claim 1 in which one or more of platinum group metals such as Pt, Pd, Rh, etc., or oxides having a perovskite structure consisting of La, Co, Ce, Sr, etc. are used as the oxidation catalyst. Catalytic burner as described.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59269932A JPS61147014A (en) | 1984-12-21 | 1984-12-21 | Catalytic burner |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59269932A JPS61147014A (en) | 1984-12-21 | 1984-12-21 | Catalytic burner |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61147014A JPS61147014A (en) | 1986-07-04 |
| JPH0335574B2 true JPH0335574B2 (en) | 1991-05-28 |
Family
ID=17479203
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59269932A Granted JPS61147014A (en) | 1984-12-21 | 1984-12-21 | Catalytic burner |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61147014A (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5281128A (en) * | 1990-11-26 | 1994-01-25 | Catalytica, Inc. | Multistage process for combusting fuel mixtures |
| US5425632A (en) * | 1990-11-26 | 1995-06-20 | Catalytica, Inc. | Process for burning combustible mixtures |
| US5248251A (en) * | 1990-11-26 | 1993-09-28 | Catalytica, Inc. | Graded palladium-containing partial combustion catalyst and a process for using it |
| US5326253A (en) * | 1990-11-26 | 1994-07-05 | Catalytica, Inc. | Partial combustion process and a catalyst structure for use in the process |
| US5259754A (en) * | 1990-11-26 | 1993-11-09 | Catalytica, Inc. | Partial combustion catalyst of palladium on a zirconia support and a process for using it |
| US5250489A (en) * | 1990-11-26 | 1993-10-05 | Catalytica, Inc. | Catalyst structure having integral heat exchange |
| US5258349A (en) * | 1990-11-26 | 1993-11-02 | Catalytica, Inc. | Graded palladium-containing partial combustion catalyst |
| US5559073A (en) * | 1994-09-26 | 1996-09-24 | Beijing Huaxia Environmental Protection Company | Pollution control catalyst with mutual protective distributed-active-combinations each including noble-metal-atoms stably structured and protected therein |
| WO2009105907A1 (en) * | 2008-02-27 | 2009-09-03 | Radiamon S.A. | Catalytic radiating heating appliance |
| KR100987417B1 (en) | 2008-11-11 | 2010-10-13 | 주식회사 영재 | Catalyst heater |
-
1984
- 1984-12-21 JP JP59269932A patent/JPS61147014A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61147014A (en) | 1986-07-04 |
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