JPS61284502A - Heat treatment device for finishing iron and steel powder - Google Patents
Heat treatment device for finishing iron and steel powderInfo
- Publication number
- JPS61284502A JPS61284502A JP60126333A JP12633385A JPS61284502A JP S61284502 A JPS61284502 A JP S61284502A JP 60126333 A JP60126333 A JP 60126333A JP 12633385 A JP12633385 A JP 12633385A JP S61284502 A JPS61284502 A JP S61284502A
- Authority
- JP
- Japan
- Prior art keywords
- chamber
- gas
- decarburization
- deoxidation
- powder
- 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
- 239000000843 powder Substances 0.000 title claims abstract description 76
- 238000010438 heat treatment Methods 0.000 title claims abstract description 38
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims description 20
- 229910000831 Steel Inorganic materials 0.000 title claims description 19
- 239000010959 steel Substances 0.000 title claims description 19
- 229910052742 iron Inorganic materials 0.000 title claims description 8
- 238000005261 decarburization Methods 0.000 claims abstract description 61
- 238000005192 partition Methods 0.000 claims abstract description 34
- 238000011282 treatment Methods 0.000 claims abstract description 10
- 238000003756 stirring Methods 0.000 claims abstract description 8
- 238000012545 processing Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 3
- 239000010410 layer Substances 0.000 abstract 1
- 238000007789 sealing Methods 0.000 abstract 1
- 239000002344 surface layer Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 104
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 238000001816 cooling Methods 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000011261 inert gas Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 235000013312 flour Nutrition 0.000 description 2
- 238000009499 grossing Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 238000004663 powder metallurgy Methods 0.000 description 2
- 238000010298 pulverizing process Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 229910001341 Crude steel Inorganic materials 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000007885 magnetic separation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000007788 roughening Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000011144 upstream manufacturing 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、粉末冶金用または粉末のままで利用する用途
に適する鉄鋼粉の仕上熱処理装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application] The present invention relates to an apparatus for finishing heat treatment of iron and steel powder, which is suitable for powder metallurgy or for applications in which the powder is used as it is.
一般に、工業的な鉄鋼粉の製造装置として、鉄鉱石粉や
ミルスケール粉の還元装置、水、ガス。Generally, industrial steel powder manufacturing equipment includes iron ore powder and mill scale powder reduction equipment, water, and gas.
油などの高圧流体を溶湯に噴射するアトマイズ装置、鋼
材の切削加工で発生するダライコやショットを粉砕する
粉砕装置、高炉スラグや鉄鋼粉を含むダスト類の粉砕と
磁選とを組み合せた製造装置などがある。これらの製造
装置では、いずれもまず炭素、酸素、窒素などの不純物
が目標とする値より相当高い粗製鉄鋼粉（以下粗製粉と
略す）を製造し、次に適切な仕上熱処理により粗製粉の
脱炭、脱酸、脱窒を行う、しかし、粉末冶金用鉄鋼粉を
得ようとする場合、仕上熱処理における脱皮、脱酸、脱
窒が不充分な場合、鉄鋼粉の圧縮性やその焼結体の機械
的特性が向上しないし、鉄鋼粉を粉末のままで使用する
場合、金属鉄が所望の値より低くなって、目的とする用
途に合致しない、従って、粗製粉の仕上熱処理する装置
につき種々研究されている。These include atomization equipment that injects high-pressure fluids such as oil into molten metal, pulverization equipment that pulverizes slag and shot generated during cutting of steel materials, and manufacturing equipment that combines pulverization and magnetic separation of dust, including blast furnace slag and steel powder. be. In each of these manufacturing devices, crude steel powder (hereinafter referred to as "crude powder") containing impurities such as carbon, oxygen, and nitrogen that is considerably higher than the target value is first produced, and then the crude powder is removed through an appropriate finishing heat treatment. Carbonization, deoxidation, and denitrification are performed, but when trying to obtain steel powder for powder metallurgy, if descaling, deoxidization, and denitrification in the finishing heat treatment are insufficient, the compressibility of the steel powder and its sintered body may be affected. The mechanical properties of iron and steel powder do not improve, and when iron and steel powder is used in powder form, the value of the metallic iron becomes lower than the desired value and does not meet the intended use. being researched.
例えば、特開昭５８−１９４０１では、油アトマイズ粗
製粉を連続式移動床炉の移動床上に供給し、移動床上の
粗製粉を非酸化性ガス雰囲気に保った予熱装置内で５５
０〜１２００℃に加熱し、ついで非酸化性ガス雰囲気を
保った冷却装置内で冷却することによって、脱炭を能率
よく行う仕上熱処理装置を開示している。また、その際
に使用すべき炉構造としては、前記移動床炉の上流側の
上方に粗製粉を供給する供給装置と、その供給装置の下
流側に設けられ非酸化性ガス供給系に接続した予熱室と
、その予熱室の下流側に設けられ脱炭性ガス供給系に接
続した脱炭室と、その脱炭室の下流側に設けられ非酸化
性ガス供給系に接続した冷却室とから構成した装置であ
ることと。For example, in Japanese Patent Application Laid-Open No. 58-19401, oil atomized crude powder is supplied onto the moving bed of a continuous moving bed furnace, and the crude powder on the moving bed is heated at 50% by heat in a preheating device that maintains the crude powder on the moving bed in a non-oxidizing gas atmosphere.
The present disclosure discloses a finishing heat treatment apparatus that efficiently performs decarburization by heating to 0 to 1200° C. and then cooling in a cooling device that maintains a non-oxidizing gas atmosphere. In addition, the furnace structure to be used at that time includes a feeding device that supplies coarse powder above the upstream side of the moving bed furnace, and a feeding device provided downstream of the feeding device and connected to a non-oxidizing gas supply system. A preheating chamber, a decarburization chamber provided downstream of the preheating chamber and connected to a decarburizing gas supply system, and a cooling chamber provided downstream of the decarburization chamber and connected to a non-oxidizing gas supply system. The device must have been configured.
予熱室と脱炭室との境界、あるいは、脱炭室と冷却室と
の境界、あるいはその両方に脱炭室のガスが予熱室ある
いは冷却室に混入することを防ぐ中空構造のガス流出壁
を設けた装置としている。さらに、脱炭性ガス中に混入
した脱炭反応阻害成分を除去しながら、脱炭性ガスを循
環使用する装置についても記載されている。A hollow structure gas outflow wall is installed at the boundary between the preheating chamber and the decarburization chamber, the boundary between the decarburization chamber and the cooling chamber, or both to prevent gas from the decarburization chamber from entering the preheating chamber or the cooling chamber. This is a device that has been installed. Furthermore, an apparatus is also described that circulates and uses the decarburizing gas while removing components that inhibit the decarburizing reaction mixed in the decarburizing gas.
しかし、前記特開昭５８−１９４０１は脱炭のみを行う
ものであり、脱炭、脱酸、脱窒のうち二種以上の什ヒ熱
処理を連続的に行う装置ではない、また、使用すべき雰
囲気ガスの露点については何も記載されておらず、予熱
室、脱炭室、冷却室での雰囲気ガスの流れは、各室の圧
力差のみで制御しており、各室内でのガス流速を増大さ
せる工夫がされていない、従って、この技術は脱炭、脱
酸、脱窒の二種以上を効率的に進める仕上熱処理装置で
はない。However, the above-mentioned Japanese Patent Application Laid-Open No. 58-19401 only performs decarburization, and is not an apparatus that continuously performs two or more types of heat treatment among decarburization, deoxidation, and denitrification. Nothing is written about the dew point of the atmospheric gas, and the flow of the atmospheric gas in the preheating chamber, decarburization chamber, and cooling chamber is controlled only by the pressure difference in each chamber, and the gas flow rate in each chamber is controlled. Therefore, this technology is not a finishing heat treatment device that can efficiently perform two or more of decarburization, deoxidation, and denitrification.
そこで、粗製粉の脱炭、脱酸または脱窒のうち二種以上
の処理を連続的に効率よく行うための熱処理装置を提供
することが本発明の目的である。Therefore, it is an object of the present invention to provide a heat treatment apparatus that can continuously and efficiently perform two or more types of treatments among coarse powder, decarburization, deoxidation, and denitrification.
本発明は、粗製粉の脱炭、脱酸、脱窒の各処理がもっと
も効率的゛に進むように工夫した装置の組合せであり、
また雰囲気ガスの流れの速度を増大させる工夫をこらし
た連続式熱処理装置とした。The present invention is a combination of devices designed to most efficiently decarburize, deoxidize, and denitrify coarse powder.
In addition, the continuous heat treatment equipment was designed to increase the flow rate of atmospheric gas.
前記目的を達成するため、本発明は、移動床炉内の床上
に粗製粉充填層表面を凹凸状に成形する装置と、炉の処
理空間をその長手方向に脱炭室、脱酸室、脱窒室に分割
する仕切壁と、炉内の鉄鋼粉が焼結する位置以降で雰囲
気ガスを攪拌させるファンとを有し、さらに好ましくは
脱炭室へ水蒸気を添加するための加湿器とを有すること
からなる熱処理炉である。In order to achieve the above object, the present invention provides an apparatus for forming the surface of a coarse powder packed bed into an uneven shape on the floor of a moving bed furnace, and a processing space of the furnace that has a decarburization chamber, a deoxidation chamber, and a deoxidation chamber in the longitudinal direction. It has a partition wall that divides the nitrogen chamber, a fan that stirs the atmospheric gas after the position where the steel powder is sintered in the furnace, and preferably a humidifier that adds water vapor to the decarburization chamber. This is a heat treatment furnace consisting of:
本発明者らは、粗製粉の脱炭、脱酸または脱窒のうち二
種以上の処理を連続的に行う熱処理装置について、種々
検討した結果４次の第一から第四までを合理的に組合せ
ることによって、もっとも効果的に熱処理できる装置を
開発した。The present inventors have conducted various studies on heat treatment equipment that continuously performs two or more types of decarburization, deoxidation, or denitrification of coarse powder. By combining these two methods, we have developed a device that can perform heat treatment most effectively.
第一に脱炭、脱酸または脱窒のうち二種類以上の化学反
応時間を短縮するために移動床上の粗製粉充填層の表面
を凹凸状に成形して充填層表面の反応面積を増大させる
装置、例えばスクレーパや異径ロールなどを設けること
。First, in order to shorten the chemical reaction time of two or more types of decarburization, deoxidation, or denitrification, the surface of the coarse powder packed bed on the moving bed is shaped into an uneven shape to increase the reaction area on the surface of the packed bed. Provide equipment such as scrapers and rolls of different diameters.
第二に脱皮、脱酸、脱窒の各過程での加熱温度制御を容
易にするためと、脱炭、脱酸、脱窒の灸室内の雰囲気ガ
スを望ましい組成に保つための装置として脱炭室と脱酸
室との境界、または脱酸室と脱窒室との境界、または脱
炭室と脱窒室との境界に、雰囲気ガスを所望の組成に保
つためのガス仕切壁を設けること。Second, it is used as a decarburization device to facilitate heating temperature control in each process of decarburization, deoxidation, and denitrification, and to maintain the atmospheric gas in the moxibustion chamber at a desired composition during decarburization, deoxidation, and denitrification. A gas partition wall is provided at the boundary between the chamber and the deoxidizing chamber, the boundary between the deoxidizing chamber and the denitrifying chamber, or the boundary between the decarburizing chamber and the denitrifying chamber in order to maintain the atmospheric gas at a desired composition. .
また脱炭、脱酸、脱窒処理にそれぞれ適した雰囲気ガス
を移動床炉上の粗製粉の移動方向と逆向きに流せるよう
にし、しかも、脱炭室では露点３０〜６０℃のＮ２．Ａ
ｒ等の不活性ガスもしくはＨ２，ＡＸガス等の還元性ガ
スを導き、６００−１１００℃に加熱し、脱酸室では露
点４０℃以下、望ましくは室温以下の前記還元性ガスを
導き、７００〜１１００℃に加熱し、脱窒室では露点４
０℃以下、望ましくは室温以下のＨ２を主体とするガス
を導き、４５０〜７５０℃に加熱するように各室を独立
に制御する装置とする。In addition, atmospheric gases suitable for decarburization, deoxidation, and denitrification treatments are made to flow in the opposite direction to the movement direction of the coarse powder on the moving bed furnace, and in the decarburization chamber, N2. A
An inert gas such as R or a reducing gas such as H2 or AX gas is introduced and heated to 600-1100°C, and in the deoxidation chamber, the reducing gas having a dew point of 40°C or less, preferably room temperature or less, is introduced and heated to 700-1100°C. Heated to 1100℃, and the denitrification chamber had a dew point of 4.
The device controls each chamber independently to introduce a gas mainly composed of H2 at 0°C or lower, preferably room temperature or lower, and heat it to 450 to 750°C.
第三に前記各室の雰囲気ガスの流れ速度をさらに向上さ
せる装置として前記移動床上の鉄鋼粉が焼結する位置以
降で炉内雰囲気ガスを撹拌するフアンを設けること。Thirdly, as a device for further increasing the flow rate of the atmospheric gas in each of the chambers, a fan is provided to stir the atmospheric gas in the furnace after the position on the moving bed where the steel powder is sintered.
第四にさらに好ましい態様として雰囲気ガスの露点ｉＪ
節装置を設置すること、すなわち脱炭室へ水蒸気を添加
するための加湿器を設置する。Fourthly, as a further preferred embodiment, the dew point iJ of the atmospheric gas
Install a moderation device, i.e. a humidifier to add steam to the decarburization chamber.
以上により、粗製粉の脱炭、脱酸、脱窒の各速度を増大
させることができる。With the above, each rate of decarburization, deoxidation, and denitrification of the coarse powder can be increased.
以下、この発明の装置について作用とともにさらに詳細
に説明する。Hereinafter, the device of the present invention will be explained in more detail along with its operation.
本発明者らは、連続的かつ効率的に、脱炭、脱酸、脱窒
処理する装置につき検討した結果、連続的に動く移動床
を採用した。移動床としてはベルト式、またはプッシャ
ーやローラー上でトレイを連続的に移動する形式の装置
も含まれる。移動床上の粗製粉をます脱炭し、次に脱酸
して、最後に脱窒する工程順序とし、脱炭、脱酸、脱窒
の各室での各処理に適した雰囲気ガスを粉末の移動方向
と逆の方向すなわち向流式に流すこととすれば。The present inventors studied an apparatus for continuously and efficiently decarburizing, deoxidizing, and denitrifying, and as a result, adopted a continuously moving moving bed. The moving bed also includes belt-type devices or devices that continuously move trays on pushers or rollers. The rough powder on the moving bed is first decarburized, then deoxidized, and finally denitrified. If the flow is in the opposite direction to the moving direction, that is, in a countercurrent manner.
各処理を連続的かつ効率的に行うことが出来る。Each process can be performed continuously and efficiently.
ただし、前記の各種粗製粉のうち、脱炭が不必要な場合
には、脱酸、脱窒の順で、脱酸が不必要な場合には、脱
炭、脱窒の順で、脱窒が不必要な場合には、脱炭、脱酸
の順でそれぞれ熱処理すればよい装置とした。このよう
な処理工程順序とする根拠は次のようなことからである
。つまり。However, among the above various coarse powders, if decarburization is not necessary, deoxidation and denitrification are performed in that order; If this is not necessary, the device is designed so that it is sufficient to perform heat treatment in the order of decarburization and deoxidation. The basis for such a processing step order is as follows. In other words.
ａ） 脱炭、脱酸、脱窒に好適な加熱温度はそれぞれ６
００〜１１００℃、７００〜１１００℃。a) The suitable heating temperature for decarburization, deoxidation, and denitrification is 6.
00-1100°C, 700-1100°C.
４５０〜４７０℃である。The temperature is 450-470°C.
ｂ） 連続式の移動床炉で最も採用しやすい熱処理パタ
ーンが非対称台形型のパターンである。b) The most easily adopted heat treatment pattern for continuous moving bed furnaces is an asymmetric trapezoidal pattern.
Ｃ） 高温処理が必要な脱炭、脱酸を加熱の前半に、低
温処理が必要でかつ冷却をかねて処理できる脱窒を後半
にすべきである。C) Decarburization and deoxidation, which require high-temperature treatment, should be done in the first half of the heating process, and denitrification, which requires low-temperature treatment and can be treated in combination with cooling, should be done in the second half.
ｄ） また、各室間に仕切壁を設置して、粗製粉の通過
部には開口を設けるので、室間での雰囲気ガスの流出、
流入が不完全であるから、高霧点での処理と低露点での
処理と区別する方が望ましい。d) In addition, partition walls will be installed between each chamber, and openings will be provided in the passage area for coarse powder, so atmospheric gas will not flow between the chambers.
Since the inflow is incomplete, it is preferable to distinguish between high fog point and low dew point treatments.
以上の理由から粗製粉の熱処理においては脱炭、脱酸、
脱窒の順序とする熱処理装置とすべきであり、第１図（
ａ）は実施例の縦断面図を示した。For the above reasons, heat treatment of coarse powder requires decarburization, deoxidation,
The heat treatment equipment should be used in the order of denitrification, as shown in Figure 1 (
a) shows a longitudinal sectional view of the example.
まず、移動床上の粗製粉充填層の表面を凹凸状に成形す
る装置につき記載する０例えば、連続式ベルト上の粗製
粉層の表面を凹凸状に成形するには本発明に含まれる第
１図（ｂ）や第２図に示した装置を炉の入口近傍に設け
、粉末の進む方向に凹凸の溝をつける。この装置の取付
位２は炉の外側とするかまたは粗製粉が焼結前の状態で
あれば炉の中であってもよい、第１図（ｂ）はベルト上
の粗製粉層２の表面に下縁が凹凸上の鉄板製スクレーパ
３で凹凸をつける装置である。第２図は軸方向に凹凸を
有する異径ロール４を用いた装置、である、いずれの場
合でも凹凸の斜面の傾斜角度は使用する粗製粉の安息角
以下とするのが望ましい、凹凸を付ける理由は脱炭、脱
酸、脱窒の反応面積を増大させて、反応時間を短縮する
ことと、粉末の移送中に粉末がケーキ状に固着するが、
凹部からクラックが入り易くシ、後工程でのケーキ粉砕
が容易となるからである。First, an apparatus for forming the surface of a coarse powder packed layer on a moving bed into an uneven shape will be described. The apparatus shown in FIG. 2 and FIG. 2 is installed near the entrance of the furnace, and grooves are formed in the direction in which the powder advances. The installation position 2 of this device may be outside the furnace or inside the furnace if the coarse powder is in a state before sintering. Figure 1 (b) shows the surface of the coarse powder layer 2 on the belt. This is a device for making unevenness on the lower edge using a scraper 3 made of iron plate. Figure 2 shows a device using a roll 4 of different diameters with unevenness in the axial direction. In either case, it is desirable that the angle of inclination of the slope of the unevenness is equal to or less than the angle of repose of the coarse flour used. The reason is that the reaction area for decarburization, deoxidation, and denitrification is increased to shorten the reaction time, and that the powder sticks like a cake during powder transfer.
This is because cracks are likely to form from the concave portions, making it easier to crush the cake in the subsequent process.
以上のスクレーパなどによって凹凸状に成形した粗製粉
層は移動床の移動に伴って脱炭室２７へ入る。この脱炭
室２７での雰囲気ガスの必要条件としては、露点３０〜
６０℃のＮ２．Ａｒ等の不活性ガスもしくはＮ２．ＡＸ
ガス等の還元性ガス中で、６００〜１１００℃に加熱す
る必要がある。露点が６０℃を越えると、後工程で脱酸
すべき粗製粉が６００℃での加熱下の脱炭室でさらに酸
化するので不可であり、一方露点が３０℃未満では、１
１００℃の加熱下でも脱炭速度が著しく低下して、効率
的に脱炭することが困難となる。The coarse powder layer formed into an uneven shape by the above-mentioned scraper or the like enters the decarburization chamber 27 as the moving bed moves. The necessary conditions for the atmospheric gas in this decarburization chamber 27 include a dew point of 30 to
N2 at 60°C. Inert gas such as Ar or N2. AX
It is necessary to heat it to 600 to 1100°C in a reducing gas such as gas. If the dew point exceeds 60°C, this is not possible because the coarse powder to be deoxidized in the subsequent process will be further oxidized in the decarburization chamber heated at 600°C.On the other hand, if the dew point is less than 30°C,
Even under heating at 100°C, the decarburization rate decreases significantly, making it difficult to decarburize efficiently.
従って、脱炭室２７での条件としては６００〜１１００
℃の温度で、雰囲気ガスの露点を３０〜６０℃とすべき
である。Therefore, the conditions in the decarburization chamber 27 are 600 to 1100
The dew point of the ambient gas should be between 30 and 60°C.
脱炭室２７における雰囲気ガスとしては湿潤したガスで
あれば、目的は達成されるため、Ｎ２゜Ａｒ等の不活性
ガスもしくは、Ｎ２ 、ＡＸガス等の還元性ガスが適し
ている。したがって、脱炭室の露点を所望の値に設定す
るために加湿器４０を設けることが好ましい、そこで、
設置すべき加湿器につき記載する。Since the purpose can be achieved as long as the atmospheric gas in the decarburization chamber 27 is a moist gas, an inert gas such as N2°Ar or a reducing gas such as N2 or AX gas is suitable. Therefore, it is preferable to provide a humidifier 40 in order to set the dew point of the decarburization chamber to a desired value.
Describe the humidifier that should be installed.
設置すべき加湿器４０としては、第３図に示したように
所望の重量の水蒸気４１を直接水蒸気導入口３６ｂから
炉内に吹き込む装置であってもよく、第４図に示したよ
うに雰囲気ガスを所望の露点に加湿して脱炭室２７の水
蒸気導入口３６ｂへ導く装置でもよい、第３図において
、バルブ５を介して導入された水蒸気４１は複数個の衝
突板６を有するドレンセパレータ７内を経由し、そして
、水蒸気流量を測定するメータ８をへてオリフィス９を
通過した後、電磁バルブ１０をへて脱炭室２７の水蒸気
導入口３６ｂに導かれる。ただし、オリフィス９と電磁
バルブ１０は流量指示計１１を介して電気的に連動する
装置とする。第４図においては、３つの水槽すなわち給
水槽１２と加湿槽１３と水位指示槽１４とからなる加湿
器内へ、加湿すべき雰囲気ガスを導入し、仕切板１５の
下を通過させながら加湿し、加湿器出口から炉内の脱炭
室２７へ導く、給水槽１２においては、給水電磁バルブ
１６から必要な量の水４３を、給水槽１２へ導き、給水
槽１２の下部に設けた水蒸気ヒータ１７に水蒸気４１を
送り希望の温度に加熱する。加湿槽１３においては、槽
１３の下部に設けた水蒸気ヒータ１７と電気ヒータ１８
により水を加熱し、水温は温度計１９により測温する。The humidifier 40 to be installed may be a device that directly blows a desired weight of steam 41 into the furnace from the steam inlet 36b as shown in FIG. It may be a device that humidifies the gas to a desired dew point and guides it to the steam inlet 36b of the decarburization chamber 27. In FIG. After passing through an orifice 9 through a meter 8 that measures the steam flow rate, the steam passes through an electromagnetic valve 10 and is guided to a steam inlet 36b of a decarburization chamber 27. However, the orifice 9 and the electromagnetic valve 10 are electrically linked via a flow rate indicator 11. In FIG. 4, atmospheric gas to be humidified is introduced into a humidifier consisting of three water tanks, namely a water supply tank 12, a humidification tank 13, and a water level indicator tank 14, and is humidified while passing under a partition plate 15. In the water supply tank 12, which leads from the humidifier outlet to the decarburization chamber 27 in the furnace, the required amount of water 43 is guided from the water supply electromagnetic valve 16 to the water supply tank 12, and is connected to a steam heater provided at the bottom of the water supply tank 12. Steam 41 is sent to 17 and heated to a desired temperature. In the humidifying tank 13, a steam heater 17 and an electric heater 18 are provided at the bottom of the tank 13.
The water is heated by a thermometer 19, and the water temperature is measured by a thermometer 19.
水位指示槽１４では水位２０を検知する水位測定子２１
により水位検知器２２を介して検知する。In the water level indicator tank 14, a water level measuring element 21 detects the water level 20.
The water level is detected via the water level detector 22.
ただし、給水１！磁バルブ１６は検知器２１と電気的に
連動している。第４図の加湿器４０の特徴は水の急速加
熱に水蒸気ヒータ１７を使用し、水温の微調節には電気
ヒータ１８を使用することにある。However, water supply 1! The magnetic valve 16 is electrically interlocked with the detector 21. A feature of the humidifier 40 shown in FIG. 4 is that a steam heater 17 is used for rapid heating of water, and an electric heater 18 is used for fine adjustment of water temperature.
脱炭室２７を通過した粉末は脱酸室２８に入る。この脱
酸室２８の熱処理条件としては露点４０℃以下、望まし
くは室温以下のＨ２，ＡＸガス等の還元性ガスを使用し
、７００〜１１００℃に加熱すべきである。８点４０℃
を越えて７００℃未満で加熱すると脱酸速度は非常に小
さく、効率的な脱酸処理ができない、また脱炭でも同様
であるが、脱酸温度が１１００℃を越えると熱処理終了
後の鉄鋼粉ケーキが粉砕できない程硬くなり、それを無
理して粉末化すると、通常使用される粒度の粉砕歩留が
低下する上に、鉄鋼粉の成形性が著しく低下してしまう
、従って、脱酸室２８での条件としては露点４０℃以下
、望ましくは室温以下のＨ２，ＡＸガス等の還元性ガス
を使用し、７００−１１００℃加熱とすべきである。The powder that has passed through the decarburization chamber 27 enters the deoxidation chamber 28. The heat treatment conditions for the deoxidizing chamber 28 should be to use a reducing gas such as H2 or AX gas having a dew point of 40 DEG C. or lower, preferably room temperature or lower, and heating to 700 DEG C. to 1100 DEG C. 8 points 40℃
If the deoxidation temperature exceeds 1100℃, the deoxidation rate will be very low and efficient deoxidation treatment will not be possible.The same is true for decarburization, but if the deoxidation temperature exceeds 1100℃, the steel powder after the heat treatment will deteriorate. If the cake becomes so hard that it cannot be crushed, and if it is forced into powder, the crushing yield of the normally used particle size will be reduced, and the formability of the steel powder will be significantly reduced. As for the conditions, a reducing gas such as H2 or AX gas with a dew point of 40°C or lower, preferably room temperature or lower, should be used, and the heating should be 700-1100°C.
次に脱窒室２９の条件としては露点４０℃以下、望まし
くは室温以下のＨ２を主体とするガス中で４５０〜７５
０℃の加熱とする。鉄鋼粉の脱窒では鉄鋼粉中の窒素と
雰囲気中のＨ２とが反応し、ＮＨ３となり粉末から除去
されるため、Ｈ２分圧が高いほど脱窒速度が大きい、脱
窒速度が最大となる温度は５５０〜６５０℃の範囲にあ
り、その前後の１００℃を加えた４５０〜７５０℃でも
十分に脱窒する。露点４０℃を越えると水蒸気分圧が急
激に上昇してＨ２分圧が低下して脱窒速度が小さくなる
。Ｈ２分圧低下は脱酸においても不利である。Next, the conditions for the denitrification chamber 29 are 450 to 75°C in a gas mainly composed of H2 with a dew point of 40°C or less, preferably room temperature or
Heat to 0°C. In the denitrification of steel powder, nitrogen in the steel powder reacts with H2 in the atmosphere to form NH3, which is removed from the powder, so the higher the H2 partial pressure, the higher the denitrification rate, and the temperature at which the denitrification rate is maximum. is in the range of 550 to 650°C, and sufficient denitrification can be achieved even at 450 to 750°C, which is the sum of 100°C before and after that. When the dew point exceeds 40° C., the water vapor partial pressure rapidly increases, the H2 partial pressure decreases, and the denitrification rate decreases. A decrease in H2 partial pressure is also disadvantageous in deoxidation.
以上の条件下で粗製粉を熱処理すると、脱炭。When crude powder is heat-treated under the above conditions, it is decarburized.
脱酸、脱窒は比較的効率よく進行するが、さらに効率を
上げるためには、各室の境界に開口を有する仕切壁２３
を設置する。Deoxidation and denitrification proceed relatively efficiently, but in order to further increase efficiency, partition walls 23 having openings at the boundaries of each chamber are used.
Set up.
後述するように各室２７．２８．２９へのガス導入位置
、各室２７，２８．２９からのガス排出位置を適切に決
めても、各室２７，２８．２９で使用するガスの種類と
雰囲気ガスの混入がさけられない、従って、各室の境界
に仕切壁２３を設置して脱炭、脱酸、脱窒に好適な雰囲
気とする。開口を有する仕切壁の設置例を第５図、第６
図に示した。第５図においては仕切壁２３が炉壁２４の
天井と底部から上下に設置する場合であって、ハースロ
ール２５とベルトｌと粗製粉層２との断面積を開口２６
とする仕切壁２３を示す、第６図は、仕切壁を炉壁２４
の側壁にも設けた場合を示している。第５図または第６
図において、仕切壁の設計指針として、第一に、ベルト
上に供給した粉末は連続的に雰囲気ガス導入口側に向っ
て移動するがために、粉末とベルトが通過する部分を除
いて、第５図に示したように移動床天井と底部とからの
上下の仕切壁２３、さらに、第６図に示したように、第
５図に追加した左右の仕切壁２３すなわち開口を有する
仕切壁を設けるべきである。As will be described later, even if the gas introduction position into each chamber 27, 28, 29 and the gas exhaust position from each chamber 27, 28, 29 are determined appropriately, the type of gas used in each chamber 27, 28, 29 and Mixing of atmospheric gas cannot be avoided. Therefore, partition walls 23 are installed at the boundaries of each chamber to create an atmosphere suitable for decarburization, deoxidation, and denitrification. Examples of installing partition walls with openings are shown in Figures 5 and 6.
Shown in the figure. In FIG. 5, the partition wall 23 is installed above and below the ceiling and bottom of the furnace wall 24, and the cross-sectional area of the hearth roll 25, the belt l, and the coarse powder layer 2 is
FIG. 6 shows a partition wall 23 with a furnace wall 24.
The figure shows a case in which it is also provided on the side wall of the Figure 5 or 6
In the figure, as a design guideline for the partition wall, firstly, since the powder supplied onto the belt continuously moves toward the atmospheric gas inlet side, the As shown in Fig. 5, upper and lower partition walls 23 from the movable floor ceiling and the bottom, and furthermore, as shown in Fig. 6, left and right partition walls 23 added to Fig. 5, that is, partition walls with openings. It should be established.
第二に、各室で異種の露点、異種の雰囲気ガスを使用す
るとすれば、仕切壁２３の開口の部分を小さくする必要
があり、また各室でほぼ等しい露点、はぼ等しい組成の
ガスを使用するとすれば、開口の部分は大きくてもよい
、開口の寸法は使用するガスの露点とガスの組成によっ
て適宜選択することができる。第三に開口を有する仕切
壁の設置位置は各室の境界とし、各室内での設置は不要
である。各室内に設置すれば導入ガスの圧力負荷をいた
ずらに増し１強力な送風機が必要となり好ましくない、
従って、二つの室であれば一箇所の仕切壁、三つの室で
あれば二箇所の仕切壁を設置すべきである。脱炭、脱酸
、脱窒の各室間で熱処理温度に大きな差異がある場合は
、各室を所望の温度に制御させるため断熱効果を持たせ
た仕切壁２３に、また必要に応じて各室の境界内に冷却
室を設こしてもよい。Second, if different types of atmospheric gases with different dew points and different types of atmospheric gases are used in each chamber, it is necessary to make the opening in the partition wall 23 small, and also to use gases with approximately the same dew point and approximately the same composition in each chamber. If used, the portion of the opening may be large, and the size of the opening may be appropriately selected depending on the dew point of the gas used and the composition of the gas. Thirdly, the partition walls with openings are installed at the boundaries of each room, and there is no need to install them within each room. If installed in each room, it will undesirably increase the pressure load of the introduced gas and require a powerful blower.
Therefore, if there are two rooms, one partition wall should be installed, and if there are three rooms, two partition walls should be installed. If there is a large difference in heat treatment temperature between the decarburization, deoxidation, and denitrification chambers, use a partition wall 23 with a heat insulating effect to control each chamber to the desired temperature, or if necessary, A cooling chamber may be provided within the boundaries of the chamber.
各室で使用する雰囲気ガスの露点または種類が異なれば
、当然独立に各室へガスを導入しなければならないが、
その導入位置は各室の粉末出口付近として向流式とし、
排ガス出口は各室の粉末入口付近とすべきである。向流
式とすれば、出口付近に近ずくほど、脱炭、脱酸または
脱窒に最適のフレッシュなガスが被処理物に接触し、各
反応が促進される。Ｈ２またはＡＸガスのような一種類
のガスを使用する場合には、脱窒、脱酸室は同一種類、
同一露点のガスで処理することができ、脱炭室では脱酸
室で使用したガスを加湿して使用すればよい、従って、
この場合、脱窒室２９からの排ガス出口と脱酸室２９へ
のガス導入口は不要であり、かつ脱酸室２９と脱窒室２
８との境界における仕切壁２３の開口の部分は大きくす
る。If the dew point or type of atmospheric gas used in each room is different, it is natural that the gas must be introduced into each room independently.
The introduction position is a counter-current type near the powder outlet of each chamber.
The exhaust gas outlet should be near the powder inlet of each chamber. If a countercurrent type is used, the closer to the outlet, fresh gas optimal for decarburization, deoxidation, or denitrification comes into contact with the object to be treated, and each reaction is accelerated. When using one type of gas such as H2 or AX gas, the denitrification and deoxidation chambers should be of the same type,
Processing can be done using gas with the same dew point, and in the decarburization chamber, the gas used in the deoxidation chamber can be humidified before use.
In this case, the exhaust gas outlet from the denitrification chamber 29 and the gas inlet to the deoxidation chamber 29 are unnecessary, and the deoxidation chamber 29 and the denitrification chamber 2
The opening portion of the partition wall 23 at the boundary with 8 is made large.
炉内に開口を有する仕切壁を設置する場合の大きな問題
点は、雰囲気ガスの流れと対流が欠しいことである。す
なわち、開口を有する仕切壁２３のみを設置し、室間の
ガス圧力差のみを利用して雰囲気ガスを流動させても、
仕切壁の開口部、ガス導入口およびガス排出口より比較
的離れた。仕切壁根元や炉内壁付近ではガスが淀む、こ
の淀みをなくすために、各室内の炉天井にファン３１を
設置する必要がある。すなわち強制的にガスを攪拌し、
粉末充填層表面に新鮮なガスを送ると同時に、粉末充填
層表面付近に滞留した脱炭、脱酸、脱窒によって生成し
たＣ０１Ｈ２０，ＮＨ３を一掃する必要がある。ファン
３１の設置位置としては粉体が固結する温度領域以降と
する。これは粉体が固結する前の位置でファン３１を回
転すれば、移動床上の粉末の一部を吹き上げるなどの欠
点があるからである。またファン３１は各室に一部以上
の設置が適しており、その筒数は加熱パターン、ファン
の形状１回転数、直径や、設置高さ、移動床上の粉末充
填幅などにより異なるため、適宜選択して設置する。A major problem with installing partition walls with openings in the furnace is the lack of atmospheric gas flow and convection. That is, even if only the partition wall 23 having an opening is installed and the atmospheric gas is made to flow using only the gas pressure difference between the chambers,
Relatively far away from the partition wall opening, gas inlet, and gas outlet. Gas stagnates near the base of the partition wall and the inner wall of the furnace. In order to eliminate this stagnation, it is necessary to install a fan 31 on the furnace ceiling in each room. In other words, by forcibly stirring the gas,
At the same time as sending fresh gas to the surface of the powder packed bed, it is necessary to sweep away the C01H20 and NH3 generated by decarburization, deoxidation, and denitrification that have accumulated near the surface of the powder packed bed. The fan 31 is installed at a temperature range below which the powder solidifies. This is because if the fan 31 is rotated at a position before the powder solidifies, there is a drawback that part of the powder on the moving bed will be blown up. In addition, it is suitable to install one or more of the fans 31 in each room, and the number of fans 31 varies depending on the heating pattern, fan shape, number of revolutions per rotation, diameter, installation height, powder filling width on the moving bed, etc. Select and install.
本発明装置には、必要に応じて、各室から排出する雰囲
気ガスのそれぞれまたは全部を一緒にして純化しながら
雰囲気ガスを循環して利用するガス純化装置を付属する
ことができる。脱炭室から排出した雰囲気ガスには循環
使用に有害なＣＯＸガス混入し、脱酸室ではＨ２Ｏ、脱
窒室ではＮＨ３が混入し、これらのガスをそれぞれ、ま
たは全部を一緒にしてｍ環使用すると、雰囲気ガス中に
は所定量より多いＣ０，１（２０、ＮＨ３を含み、脱炭
、脱酸、脱窒に使用不可能となるので、ガス純化装置に
よりこれらを除去する。If necessary, the apparatus of the present invention may be attached with a gas purification device that circulates and utilizes the atmospheric gas while purifying each or all of the atmospheric gas discharged from each chamber. The atmospheric gas discharged from the decarburization chamber contains COX gas, which is harmful to circulation, and the deoxidation chamber contains H2O, and the denitrification chamber contains NH3. Then, the atmospheric gas contains more C0,1(20, NH3) than a predetermined amount and cannot be used for decarburization, deoxidation, and denitrification, so these are removed by a gas purification device.
本発明は以上のように、表面凹凸成形装こ、仕切壁、フ
ァン、加湿器を同時に有する移動床炉としたので、これ
らの相互作用により粗製粉の脱炭、脱酸、脱窒を最も効
率よく進行させることができる。As described above, the present invention provides a mobile bed furnace that simultaneously has a surface roughening device, a partition wall, a fan, and a humidifier, so that the interaction of these elements enables the most efficient decarburization, deoxidation, and denitrification of coarse powder. It can be progressed well.
以下の実施例をみれば、本発明がいかに有効であるか明
らかである。The effectiveness of the present invention will be clear from the following examples.
以下１本発明装置の実施例について図面に基づき説明す
る。An embodiment of the apparatus of the present invention will be described below with reference to the drawings.
第１図（ａ）は本発明装置の実施例の連続式ベルト炉で
あり、第７図に示す従来の炉にｉｔ図（ｂ）に示した凹
凸状のスクレーパ３と、第３図または第４図に示した加
湿器４０と、第５図、第６図に示した仕切壁２３とファ
ン３１とを設け、ガス出入口を変更して改造したもので
ある。第７図は従来装置として使用した平滑用板状金属
スクレーパーを有するベルト炉を示す、従って第１図と
第７図の炉長は同じである。FIG. 1(a) shows a continuous belt furnace according to an embodiment of the present invention, in which a conventional furnace shown in FIG. The humidifier 40 shown in FIG. 4, the partition wall 23 and fan 31 shown in FIGS. 5 and 6 are provided, and the gas inlet and outlet ports are changed. FIG. 7 shows a belt furnace with a smoothing plate metal scraper used as a conventional device; therefore, the furnace lengths in FIGS. 1 and 7 are the same.
第１図（ａ）に示したように、まず、第５図に示した仕
切壁２３によって、脱炭室２７、脱酸室２８、脱窒室２
９に分け、各室にモータ３０によって回転し、雰囲気ガ
スを攪拌するファン３１を設置し１次に雰囲気ガスを脱
窒室２９のガス導入口３６ａから入れ、脱酸室２８へ導
き、一方、第３図に示した加湿器４０を介して水蒸気を
脱炭室２７に導くようにした。As shown in FIG. 1(a), first, the decarburization chamber 27, the deoxidation chamber 28, and the denitrification chamber 2 are separated by the partition wall 23 shown in FIG.
A fan 31 that is rotated by a motor 30 and stirs the atmospheric gas is installed in each chamber, and the atmospheric gas is first introduced from the gas inlet 36a of the denitrification chamber 29 and guided to the deoxidation chamber 28. Water vapor was introduced into the decarburization chamber 27 via a humidifier 40 shown in FIG.
粗製粉３２は、原料ホッパ３３を介して、ベルト１上に
供給され、第１図（ａ）においては、第１図（ｂ）の凹
凸状スクレーパ３、第７図においては従来の平滑用スク
レーパによりベル）ｌ上に凹凸状または平坦に成形して
載せられる。この粗製粉３２を図示しない駆動装置によ
り回転するホイール３４によって連続的に送り、脱炭室
２７゜脱酸室２８．脱窒室２９を経て、ケーキ軟塊を出
口側シールロール３５から排出した。The coarse powder 32 is supplied onto the belt 1 via a raw material hopper 33, and in FIG. 1(a), the uneven scraper 3 of FIG. 1(b) is used, and in FIG. 7, a conventional smoothing scraper is used. It is placed on the bell) in an uneven or flat shape. This coarse powder 32 is continuously fed by a wheel 34 rotated by a drive device (not shown) to a decarburization chamber 27 and a deoxidization chamber 28. After passing through the denitrification chamber 29, the soft cake mass was discharged from the exit side seal roll 35.
一方、雰囲気ガス（ＡＸガス）はガス導入口３６ａまた
は３６ｂから導入し、排ガス（ＡＸガス）はガス出口３
７から排出した。ガス出口３７から排出したガスはバル
ブ５をへて、燃焼器３８で燃焼した。ただし、第７図の
ガス導入口３６ａ、３６ｂはパイプ製である。粗製粉の
加熱はコークス炉ガスをラジアントチューブ３９内で燃
焼して行った。On the other hand, atmospheric gas (AX gas) is introduced from the gas inlet 36a or 36b, and exhaust gas (AX gas) is introduced from the gas outlet 36a or 36b.
It was discharged from 7. The gas discharged from the gas outlet 37 passed through the valve 5 and was burned in the combustor 38. However, the gas introduction ports 36a and 36b in FIG. 7 are made of pipes. The coarse powder was heated by burning coke oven gas in the radiant tube 39.
粗製粉として、ミルスケール粗還元粉（炭素量０．２８
重量％（以下％と略す）、酸素量０．９０％、窒素量０
．０１５％）を使用する場合、第８図の熱処理パターン
（イ）として、第７図の従来装置ではＡＸガスを単純な
加湿器により露点５１℃に加湿し１合計５ＯＮｍ’／ｈ
ｒをガス導入口３°６ｂから炉内の昇温ゾーンに導入し
、同時に、乾燥したＡＸガスの合計１００Ｎｒｎ’／ｈ
ｒをガス導入口３６ａから均熱ゾーンと冷却ゾーンに導
入して、粗製粉を仕上熱処理した。その結果。As a coarse powder, mill scale coarse reduced powder (carbon content 0.28
Weight% (hereinafter abbreviated as %), oxygen content 0.90%, nitrogen content 0
．． 015%), the conventional apparatus shown in Fig. 7 uses a simple humidifier to humidify the AX gas to a dew point of 51°C and heat treatment pattern (a) in Fig. 8.
r was introduced into the heating zone in the furnace from the gas inlet 3°6b, and at the same time, a total of 100Nrn'/h of dried AX gas was added.
r was introduced into the soaking zone and the cooling zone through the gas inlet 36a, and the coarse powder was subjected to final heat treatment. the result.
炭素量０． ＯＯ９％、酸素量０．３１％、窒素量０−
００４８％を含有するミルスケール還元鉄粉１．３トン
／ ｈ ｒを得た。Carbon content 0. OO9%, oxygen amount 0.31%, nitrogen amount 0-
1.3 tons/hr of mill scale reduced iron powder containing 0.048% was obtained.
これに対し、本発明装置である第１図（ａ）に示す炉を
使用し、乾燥したＡＸガスを１１００Ｎ″／ ｈ ｒだ
け導入口３６ａから導入し、一方、脱炭室での露点が５
１℃になるように水蒸気を導入口３６ｂから導き、同時
に５箇の攪拌ファン３１を１５０ｏｒｐｍで回転しなが
ら、前記と同じ粗製粉を第８図の熱処理パターン（イ）
の条件で熱処理した。その結果、炭素量０． ＯＯ７％
、酸素量０．２５％、窒素量０．００３１％を含有する
ミルスケール遺児鉄粉１．３トン／ ｈ ｒを得た。On the other hand, using the furnace shown in FIG. 1(a), which is the apparatus of the present invention, dry AX gas was introduced from the inlet 36a at a rate of 1100 N''/hr, while the dew point in the decarburization chamber was 5.
While introducing water vapor from the inlet 36b to a temperature of 1°C and simultaneously rotating the five stirring fans 31 at 150 rpm, the same coarse powder as above was subjected to the heat treatment pattern (a) in Fig. 8.
It was heat treated under the following conditions. As a result, the carbon content was 0. OO7%
, 1.3 tons/hr of mill scale orphan iron powder containing 0.25% oxygen and 0.0031% nitrogen was obtained.
粗製粉として水アトマイズ生成粉（炭素量０．１９％、
酸素量１．１θ％、窒素量０．０ Ｏ８２％）を原料と
する場合、第８図の熱処理パターン（ロ）として、従来
装置ではガス導入口３６ｂから合計５ＯＮｍ″／ ｈ
ｒのＡＸガス（露点４０℃）を、ガス導入ｒ１３６ａか
ら合計１１ＯＮｒｎ’／ｈｒの乾燥ＡＸガスをそれぞれ
導入し、熱処理した。Water atomized powder (carbon content 0.19%,
When the raw material is an oxygen content of 1.1θ% and a nitrogen content of 0.0% (O82%), the heat treatment pattern (b) in Figure 8 shows a total of 5ONm''/h from the gas inlet 36b in the conventional equipment.
A total of 11 ONrn'/hr of dry AX gas was introduced from the gas introduction r136a and heat-treated.
その結果、炭素量０． ＯＯ９％、酸素量０．１５％、
窒素量０．００４５％を含有したアトマイズ純鉄粉１．
５トン／ ｈ ｒを得た。As a result, the carbon content was 0. OO9%, oxygen amount 0.15%,
Atomized pure iron powder containing 0.0045% nitrogen 1.
5 tons/hr was obtained.
これに対し、本発明装置である第１図（ａ）に示す炉を
用い、乾燥したＡＸガスを１３０ Ｎｒｎ”／ｈｒだけ
導入口３６ａから入れ、脱炭室の露点が４０℃になるよ
うに水蒸気を導入口３６ｂから導き熱処理パターン（ロ
）で、ファンを攪拌しなから熱処理した。その結果、炭
素量０．００７％、酸素量０．１１％、窒素量０． Ｏ
Ｏ３９％含むアトマイズ鉄粉１．５トン／ ｈ ｒを得
た。On the other hand, using the furnace shown in FIG. 1(a), which is the apparatus of the present invention, dry AX gas was introduced from the inlet 36a at a rate of 130 Nrn''/hr so that the dew point of the decarburization chamber became 40°C. Steam was introduced from the inlet 36b and heat-treated according to the heat treatment pattern (b) without stirring the fan.As a result, the carbon content was 0.007%, the oxygen content was 0.11%, and the nitrogen content was 0.0.
1.5 tons/hr of atomized iron powder containing 39% O was obtained.
以上の実施例からも明らかなように、凹凸状のスクレー
パ設置による脱炭、脱酸、脱窒などの反応時間の短縮、
炉内に開口を有する仕切壁の設置により室内の雰囲気ガ
スの独立制御化、仕切壁とファン設置により脱窒室の脱
酸室側の隅や、脱酸室の脱窒室側の隅に滞留したＡＸガ
スの対流促進と鉄鋼粉ケーキ表面でのガス流れの速度向
上、さらに加湿器設置による多量の水蒸気添加などの相
乗効果によって１本発明装置を使用すると、従来装置を
使用する場合に比較して脱炭、脱酸、脱窒の速度が著し
く向上した。As is clear from the above examples, by installing an uneven scraper, the reaction time for decarburization, deoxidation, denitrification, etc. can be shortened,
By installing a partition wall with an opening in the furnace, the atmospheric gas in the room can be controlled independently, and by installing a partition wall and a fan, it will stay in the corner of the denitrification chamber on the deoxidization chamber side and the corner of the deoxidization chamber on the denitrification chamber side. Due to the synergistic effects of promoting convection of the AX gas, increasing the speed of the gas flow on the surface of the steel powder cake, and adding a large amount of water vapor by installing a humidifier, the use of the device of the present invention is more effective than when using the conventional device. The speed of decarburization, deoxidation, and denitrification was significantly improved.
第１図（ａ）は本発明の実施例の縦断面図、第１図（ｂ
）はそのＡ−Ａ矢視要部正面図、第２図は他の凹凸成形
装置の正面図、第３図および第４図は加湿器装置の縦断
正面図、第５図および第６図は仕切壁の縦断正面図、第
７図は従来の装置を示す縦断側面図、第８図は熱処理温
度パターン図である。
ｌ・・・ベルト、２・・・粗製粉層、３・・・スクレー
パ、４・・・異径ロール、５・・・バルブ、６・・・衝
突板。
７・・・ドレンセパレータ、８・・・流量メータ、９・
・・オリフィス、ｌＯ・・・水蒸気供給用電磁バルブ。
１１・・・流量指示計、１２・・・給水槽、１３・・・
加湿槽、１４・・・水位指示槽、１５・・・仕切板、１
６・・・給水用電磁バルブ、１７・・・水蒸気ヒータ。
１８・・・電気ヒータ、１９・・・温度計、２０・・・
水位、２１・・・水位測定ｒ、２２・・・水位調節器、
２３・・・仕切壁、２４・・・炉壁、２５・・・ハース
ロール、２６・・・開口、２７・・・脱炭室、２８・・
・脱酸室、２９・・・脱窒室、３０・・・モータ、３１
・・・ファン、３２・・・粗製粉、３３・・・ホッパ、
３４・・・ホイール、３５・・・シールロール、３６（
３６ａ。FIG. 1(a) is a longitudinal sectional view of an embodiment of the present invention, FIG. 1(b)
) is a front view of the main part as seen from arrow A-A, FIG. 2 is a front view of another uneven molding device, FIGS. 3 and 4 are longitudinal sectional front views of the humidifier device, and FIGS. 5 and 6 are front views of the humidifier device. FIG. 7 is a longitudinal sectional front view of a partition wall, FIG. 7 is a longitudinal sectional side view showing a conventional device, and FIG. 8 is a heat treatment temperature pattern diagram. l... Belt, 2... Coarse powder layer, 3... Scraper, 4... Different diameter roll, 5... Valve, 6... Collision plate. 7... Drain separator, 8... Flow meter, 9...
... Orifice, lO... Solenoid valve for water vapor supply. 11...Flow rate indicator, 12...Water tank, 13...
Humidification tank, 14... Water level indicator tank, 15... Partition plate, 1
6... Solenoid valve for water supply, 17... Steam heater. 18... Electric heater, 19... Thermometer, 20...
Water level, 21... water level measurement r, 22... water level regulator,
23... Partition wall, 24... Furnace wall, 25... Hearth roll, 26... Opening, 27... Decarburization chamber, 28...
・Deoxidation chamber, 29...Denitrification chamber, 30...Motor, 31
...Fan, 32...Coarse flour, 33...Hopper,
34... Wheel, 35... Seal roll, 36 (
36a.
Claims (1)
式移動床炉で連続的に行う鉄鋼粉の仕上熱処理装置にお
いて、移動床炉の入口近傍に鉄鋼粉充填層の表面を凹凸
状に成形する装置を設定し、前記移動床炉の処理空間に
原料走行方向と直交する仕切壁を設けて移動床炉を複数
個の空間に分割し、該分割空間には移動床と向流にガス
通路を設けると共に各空間上部にはガス撹拌装置を設置
したことを特徴とする鉄鋼粉の仕上熱処理装置。1. In a finishing heat treatment equipment for steel powder that continuously performs two or more treatments among decarburization, deoxidation, and denitrification in a continuous moving bed furnace, the surface of the packed bed of steel powder is made uneven near the entrance of the moving bed furnace. The moving bed furnace is divided into a plurality of spaces by providing a partition wall perpendicular to the raw material running direction in the processing space of the moving bed furnace, and the divided space has a countercurrent flow to the moving bed. A finishing heat treatment apparatus for iron and steel powder, characterized in that a gas passage is provided in the space, and a gas stirring device is installed in the upper part of each space.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60126333A JPH0686601B2 (en) | 1985-06-12 | 1985-06-12 | Finishing heat treatment apparatus for iron and steel powder and its operating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60126333A JPH0686601B2 (en) | 1985-06-12 | 1985-06-12 | Finishing heat treatment apparatus for iron and steel powder and its operating method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61284502A true JPS61284502A (en) | 1986-12-15 |
| JPH0686601B2 JPH0686601B2 (en) | 1994-11-02 |
Family
ID=14932584
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60126333A Expired - Fee Related JPH0686601B2 (en) | 1985-06-12 | 1985-06-12 | Finishing heat treatment apparatus for iron and steel powder and its operating method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0686601B2 (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5751201A (en) * | 1980-09-09 | 1982-03-26 | Toyota Motor Corp | Device for breaking reduced cake of metallic powder to constant size |
| JPS5827902A (en) * | 1981-08-10 | 1983-02-18 | Sumitomo Metal Ind Ltd | Method and device for treating metallic powder |
-
1985
- 1985-06-12 JP JP60126333A patent/JPH0686601B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5751201A (en) * | 1980-09-09 | 1982-03-26 | Toyota Motor Corp | Device for breaking reduced cake of metallic powder to constant size |
| JPS5827902A (en) * | 1981-08-10 | 1983-02-18 | Sumitomo Metal Ind Ltd | Method and device for treating metallic powder |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0686601B2 (en) | 1994-11-02 |
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