JPS6056991B2 - Fluidized bed pre-reduction furnace with internal - Google Patents
Fluidized bed pre-reduction furnace with internalInfo
- Publication number
- JPS6056991B2 JPS6056991B2 JP21276882A JP21276882A JPS6056991B2 JP S6056991 B2 JPS6056991 B2 JP S6056991B2 JP 21276882 A JP21276882 A JP 21276882A JP 21276882 A JP21276882 A JP 21276882A JP S6056991 B2 JPS6056991 B2 JP S6056991B2
- Authority
- JP
- Japan
- Prior art keywords
- furnace
- fluidized bed
- reduction
- internal
- ore
- 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
- 239000002994 raw material Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 31
- 238000000034 method Methods 0.000 description 14
- 238000005243 fluidization Methods 0.000 description 8
- 238000003723 Smelting Methods 0.000 description 6
- 238000009826 distribution Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 239000000428 dust Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000003638 chemical reducing agent Substances 0.000 description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 238000005054 agglomeration Methods 0.000 description 3
- 230000002776 aggregation Effects 0.000 description 3
- 229910052804 chromium Inorganic materials 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 229910001021 Ferroalloy Inorganic materials 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 229910000604 Ferrochrome Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003779 heat-resistant material Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Manufacture Of Iron (AREA)
Description
【発明の詳細な説明】
この発明は、インターナルを具える流動層予備還元炉に
関し、とくに棒材を好適例とする縦桟・横桟複数本を組
合わせてなるインターナルを炉内に設置することにより
、流動層域を多段化均等の構造にして優れた還元率が得
られるようにした炉に関するものである。[Detailed Description of the Invention] The present invention relates to a fluidized bed pre-reduction furnace equipped with an internal, and in particular, an internal comprising a combination of a plurality of vertical bars and horizontal bars, of which bar material is a preferred example, is installed in the furnace. The present invention relates to a furnace in which an excellent reduction rate can be obtained by making the fluidized bed region have a multistage and uniform structure.
近年、酸化鉄または各種金属酸化物を含有する鉱石原料
は、塊状鉱石が減少して粉状もしくは粒状の鉱石が多く
なつており、その傾向は今後ますます顕著になると予想
される。In recent years, ore raw materials containing iron oxide or various metal oxides have become less bulky ores and more powdery or granular ores, and this trend is expected to become more pronounced in the future.
こうした現状に鑑み、最近かかる粉粒状鉱石を使用して
直接製錬する技術が発展してきた。In view of the current situation, a technology for directly smelting such powdery ore has recently been developed.
例えば、流動層を用いて粉粒状鉱石を予備還元し、その
後この予備還元鉱を電気炉、転炉そお他溶解炉で溶融還
元する方法等がそれである。For example, there is a method in which powdery ore is pre-reduced using a fluidized bed, and then the pre-reduced ore is melted and reduced in an electric furnace, converter or other melting furnace.
この既知技術の場合、予備還元鉱にバインダーを添加し
て一旦塊成化し、その塊状化した物を溶解炉で溶融還元
する方式が多い。ところが、かかる従来技術によれば、
塊成化のための燃料、処理費、処理エネルギーを余分に
必要とするばかりでなく、塊成化したのち、さらに焼成
を必要とするような場合には、焼成塊状物とする際に、
焼成炉から排出するガス中のＮ０ｘ、ＳＯｘおよびダス
ト等の処理が必要となり多大の費用を要するという欠点
があつた。また、上記方式の他にも、アーク炉やプラズ
マあるいは純酸素を利用する炉を用いて予備還元鉱・を
粉粒状のまま溶融還元する方式も提案されている。しか
し、アーク炉を用いる方式は電力消費量が莫大であるば
かりでなく立地条件にも制約がある。プラズマを利用す
る炉を用いる方式は工業的規模には適用が困難である。
純酸素を利用する炉Ｊを用いる方式は高温雰囲気を得る
ことは容易であるが、酸素を予熱することができないた
め、入熱量が小さいこと、それに加えて還元雰囲気の維
持が難しいことなど技術的に解決を要する問題が残され
ていると同時に、また純酸素製造設備を準備する必要が
あり、立地的な問題点もある。このように従来技術にあ
つては技術的および経済的に解決を要する多くの課題が
残されている。そこで叢近は、電力によらないフェロク
ロムその他のフェロアロイ製造技術として、溶融還元法
が注目されるに至つている。In the case of this known technology, there are many methods in which a binder is added to the pre-reduced ore to once agglomerate it, and the agglomerated material is melted and reduced in a melting furnace. However, according to such conventional technology,
In cases where not only extra fuel, processing cost, and processing energy are required for agglomeration, but also additional firing is required after agglomeration, when producing fired agglomerates,
This method has the disadvantage that it requires treatment of NOx, SOx, dust, etc. in the gas discharged from the firing furnace, which requires a large amount of cost. In addition to the above-mentioned method, a method has also been proposed in which pre-reduced ore is melted and reduced in the form of powder using an arc furnace, plasma, or a furnace using pure oxygen. However, the method using an arc furnace not only consumes a huge amount of electricity but also has restrictions on location. A method using a furnace that utilizes plasma is difficult to apply on an industrial scale.
Although it is easy to obtain a high-temperature atmosphere using Furnace J, which uses pure oxygen, there are technical issues such as a small amount of heat input because oxygen cannot be preheated, and in addition, it is difficult to maintain a reducing atmosphere. At the same time, there are still problems that need to be solved, and at the same time, it is necessary to prepare pure oxygen production equipment, and there are also location problems. As described above, with the conventional technology, many problems remain that need to be solved both technically and economically. Therefore, the smelting reduction method is attracting attention as a technology for producing ferrochrome and other ferroalloys that does not rely on electricity.
例えば、流動層予備還元炉と竪型溶融還元炉との結合に
かかる装置を用い、粉粒状鉱石から直接フェロアロイを
製造する方法がそれである。この既知の方法は、金属酸
化物含有鉱石の予備還元に必要な還元剤及び熱の供給源
として、溶融還元炉の高温排ガスを利用して流動層形式
により予備還元する方法てあり、粉粒状鉱石を塊成化す
ることなく直接使用できる点で前述の方法に比べると低
コストで溶融金属の製造が可能である。上記した既知方
法における予備還元炉としての流動層に必要な主な条件
としては、（１）必要な還元速度が得られる反応温度維
持のた“めの熱供給が容易なこと、（２）局部過熱や高
温域での予備還元鉱石の粘着によつて焼結が起り流動化
が阻害されるようなことがないこと、（３）均一かつ安
定な流動化現象が得られること、（４）短い滞留時間で
も必要な還元率が得られること（流動層を多段化する）
、（５）粒子の流動層からの飛び出しによるダスト発生
が少ないこと、などがある。For example, there is a method for directly producing ferroalloy from powdery ore using an apparatus that combines a fluidized bed pre-reduction furnace and a vertical smelting reduction furnace. In this known method, the high-temperature exhaust gas of a smelting reduction furnace is used as a source of the reducing agent and heat necessary for the preliminary reduction of metal oxide-containing ores, and the preliminary reduction is carried out in a fluidized bed format. Since molten metal can be used directly without agglomeration, it is possible to produce molten metal at a lower cost than the above-mentioned method. The main conditions necessary for the fluidized bed as a preliminary reduction furnace in the above-mentioned known method are (1) easy heat supply to maintain the reaction temperature to obtain the required reduction rate, and (2) local (3) A uniform and stable fluidization phenomenon can be obtained; (4) It is short. The required reduction rate can be obtained even with residence time (multi-stage fluidized bed)
(5) Less dust is generated due to particles flying out of the fluidized bed.
ところが、こうした各種の条件というのは、一般的に言
つて予備還元に必要な流動層の温度が高いほど、その維
持が難しく、しかも溶融還元炉から発生する流動化ガス
中に多量のダストが含まれると、その操業法はさらに、
難しさを増大させるので、各種の新しい方法や装置の開
発が必要となる。However, generally speaking, the higher the temperature of the fluidized bed required for preliminary reduction, the more difficult it is to maintain these various conditions, and the more dust is contained in the fluidized gas generated from the smelting reduction furnace. If the operation method is
This increases the difficulty and requires the development of various new methods and devices.
この発明は、流動層予備還元炉に要求される上述した条
件のうち４，５に記述した点に関してその改良を目的と
して案出した予備還元炉の構造にかかるものであつて、
その構成の要旨とするところは、炉底部に流動化還元ガ
スの導入口を設け、炉側壁には流動層域に臨んで原料供
給口を、また該流動層域に予備還元生成物の排出口を開
口させた構成にかかる流動層予備還元炉において、炉内
の上記流動層域に複数の縦桟と横桟との組合わせよりな
るインターナルを内装装置したことを特徴とする点にあ
る。This invention relates to a structure of a pre-reduction reactor devised for the purpose of improving the points described in 4 and 5 of the above-mentioned conditions required for a fluidized bed pre-reduction reactor.
The gist of its configuration is that an inlet for fluidized reducing gas is provided at the bottom of the furnace, a raw material supply port faces the fluidized bed area on the side wall of the furnace, and an outlet for preliminary reduction products is provided in the fluidized bed area. The fluidized bed pre-reduction furnace having an open structure is characterized in that an internal device consisting of a combination of a plurality of vertical bars and horizontal bars is installed in the fluidized bed area in the furnace.
以下にその発明の詳細な説明する。第１図は、一般的な
流動層予備還元炉について示すものであり、炉本体１は
たて型であつて、その胴部には流動層２域に臨んで粉粒
状鉱石原料の供給口４を具えており、ここには鉱石ホッ
パー７・からの鉱石を炉内に供給するための供給装置６
が設置してある。The invention will be explained in detail below. Fig. 1 shows a general fluidized bed pre-reduction furnace.The furnace body 1 is vertically shaped, and the body part has a supply port 4 for feeding powdery ore raw material facing the fluidized bed 2 area. It is equipped with a feeding device 6 for feeding ore from an ore hopper 7 into the furnace.
has been installed.
また、鉱石を滞留させるために炉内に設置してガス分散
板（火格子）３に当る炉下部には、高温の還元ガス導入
口８が開口させてある。上記還元ガスとしては、加熱炉
、還元ガス発生炉あるいは溶融還元炉から発生した高温
の排ガスを使い、還元剤ならびに流動化ガスとする。こ
の還元ガスを炉内に導入することにより、ガス分散板３
上の粉粒状鉱石は流動化して、流動層２を形成し流動還
元ができる。なお、図示の９は還元剤としてメタンなど
の炭化水素含有ガスを供給する還元剤供給口である。ま
た、図示の１０は排ガスの排出口で、ここを通じて排出
される流動層２からの排出ガス中には、ダストを多量に
含有するのでサイクロン１１て除塵する。一方、予備還
元生成物は、流動層２域上部排出管５より排出され、次
工程の溶融還元炉などへ移送される。上述した予備還元
炉にあつて、例えばクロム鉱石などの場合、予備還元す
るための温度は９５０〜１１０（代）位であり、該クロ
ム鉱石が焼結するに至る温度は１２５０〜１３５０℃位
とされている。こうしたクロム鉱石を上述の予備還元炉
で流動化反応によつて予備還元する場合について考える
と、その予備還元に必要な還元温度を、流動化ガスとし
て導入する流動化還元ガスの顕熱によつて維持しようと
すると、極めて高温の流動化還元ガスの導入が必要とな
り、そのために該還元ガスの温度が上記焼結限界温度を
越えてしまい、還元ガス導入口８およびガス分散板３の
近辺では、粉粒状鉱石力化ばしば焼結限界温度以上に過
熱されるので、焼結塊や付着物の成長があつたりしてガ
ス分散板３が目づまりしたり、流動化反応が阻害される
ことになる。こうした問題点を解決するためには、かか
る流動化還元ガスの導入温度を下ければよいが、単に温
度を低下するだけでは、還元温度が低下し、還元率を減
少させることになる。そこで、本発明は、第２，３図に
示すようなインターナルを炉内のとくに流動層域の部分
に設置することて流動層の安定化と多段化類似の効果を
付与してなるものである。Further, a high-temperature reducing gas inlet 8 is opened in the lower part of the furnace, which is installed in the furnace and corresponds to the gas distribution plate (grate) 3 in order to retain the ore. As the reducing gas, high-temperature exhaust gas generated from a heating furnace, a reducing gas generating furnace, or a melting reduction furnace is used, and is used as a reducing agent and a fluidizing gas. By introducing this reducing gas into the furnace, the gas distribution plate 3
The upper particulate ore is fluidized to form a fluidized bed 2 and fluidized reduction is possible. Note that 9 in the figure is a reducing agent supply port that supplies a hydrocarbon-containing gas such as methane as a reducing agent. Further, reference numeral 10 in the figure is an exhaust gas exhaust port, and since the exhaust gas from the fluidized bed 2 discharged through this port contains a large amount of dust, the dust is removed using a cyclone 11. On the other hand, the preliminary reduction product is discharged from the upper discharge pipe 5 of the fluidized bed 2 region and transferred to the next step, such as a smelting reduction furnace. In the above-mentioned preliminary reduction furnace, for example, in the case of chromium ore, the temperature for preliminary reduction is about 950 to 110 degrees Celsius, and the temperature at which the chromium ore is sintered is about 1250 to 1350 degrees Celsius. has been done. Considering the case where such chromium ore is pre-reduced by a fluidization reaction in the above-mentioned pre-reduction furnace, the reduction temperature required for the pre-reduction can be adjusted by the sensible heat of the fluidizing reducing gas introduced as the fluidizing gas. In order to maintain this, it is necessary to introduce extremely high-temperature fluidizing reducing gas, which causes the temperature of the reducing gas to exceed the sintering limit temperature, and in the vicinity of the reducing gas inlet 8 and the gas distribution plate 3, Powdered ore is often heated above the sintering limit temperature, which may cause sintered lumps and deposits to grow, clogging the gas distribution plate 3 or inhibiting the fluidization reaction. become. In order to solve these problems, it is sufficient to lower the introduction temperature of the fluidizing reducing gas, but simply lowering the temperature will lower the reduction temperature and reduce the reduction rate. Therefore, the present invention provides an effect similar to that of stabilizing the fluidized bed and increasing the number of stages by installing an internal as shown in Figures 2 and 3 in the furnace, especially in the fluidized bed area. be.
かかるインターナルは、炉内が高温になるために耐熱性
材料によつて、特に単純な構造のものにするのが望まし
い。Such internals are preferably made of heat-resistant materials and of a particularly simple construction, since the temperature inside the furnace is high.
第２図の例は、棒状の縦桟１２・・・と同素材の横桟１
３・・・とを適宜の間隔を介在させてそれぞれ平行に設
置した構造のものであつて、各縦桟１２、横桟１３は炉
壁に直接固定しておく。第３図のインターナルは、複数
の棒材を格子状に組合わせた例であり、ガス分散板３を
省略して、該格子状インターナル１４にガス分散効果を
付与し、均一で安定した流動化反応の確保とともに、ガ
ス分散板設置の不利益を解消するようにした。なお、本
発明の上述した実施態様で採用したインターナル素材に
は、棒材の他細い板材やメッシュ等も採用できる。The example in Figure 2 shows a bar-shaped vertical bar 12... and a horizontal bar 1 made of the same material.
3... are installed in parallel with each other at appropriate intervals, and each of the vertical bars 12 and horizontal bars 13 is directly fixed to the furnace wall. The internal shown in Fig. 3 is an example in which a plurality of rods are combined in a lattice shape, and the gas dispersion plate 3 is omitted, and the lattice-shaped internal 14 is given a gas dispersion effect, resulting in a uniform and stable In addition to ensuring fluidization reaction, the disadvantages of installing a gas distribution plate were eliminated. It should be noted that as the internal material employed in the above-described embodiments of the present invention, other than bar materials, thin plate materials, meshes, etc. can also be employed.
以上説明したように流動層２域に本発明にかかるインタ
ーナルを設置することで、流動化反応が各縦・横桟１２
，１３により、時には仕切られた流動を示すようになつ
て多段化に等しい効果を発揮すると同時に、流動化の偏
りや圧力の変動が減少し、気泡の成長等も抑制できるの
で、結果的にガスの反応率が増大し、均一で安定した流
動化が確保でき予備還元率の向上が達せられる。As explained above, by installing the internal according to the present invention in the fluidized bed 2 area, the fluidization reaction can be carried out on each vertical and horizontal bar 12.
, 13, sometimes exhibits a partitioned flow, which has the same effect as multi-stage, while at the same time reducing uneven fluidization and pressure fluctuations, and suppressing the growth of bubbles, etc., as a result, the gas The reaction rate increases, uniform and stable fluidization can be ensured, and the preliminary reduction rate can be improved.
第１図は、従来の一般的な流動層予備還元炉の路線図、
第２図は、本発明の一実施例を示すインターナルを具え
る流動層予備還元炉の路線図、第３図は、本発明の他の
実施例を示すインターナルを具える流動層予備還元炉の
路線図である。
１・・・予備還元炉、２・・・流動層、３・・・ガス分
散板、４・・・粉粒状鉱石供給口、５・・・予備還元鉱
石排出口、６・・・供給装置（バルブ）、７・・・鉱石
ホッパー、８・・・流動化還元ガス導入口、９・・・炭
化水素含有ガス供給口、１０・・・排ガス排出口、１１
・・・サイクロン、１２・・・縦桟、１３・・・横桟、
１４・・・格子状Ｌインターナル。Figure 1 is a route map of a conventional general fluidized bed pre-reduction reactor.
FIG. 2 is a route diagram of a fluidized bed pre-reduction furnace equipped with internals showing one embodiment of the present invention, and FIG. 3 is a route diagram of a fluidized bed pre-reduction furnace equipped with internals showing another embodiment of the present invention. This is a route map of the furnace. DESCRIPTION OF SYMBOLS 1... Pre-reduction furnace, 2... Fluidized bed, 3... Gas distribution plate, 4... Powdered ore supply port, 5... Pre-reduced ore discharge port, 6... Supply device ( Valve), 7... Ore hopper, 8... Fluidization reducing gas inlet, 9... Hydrocarbon-containing gas supply port, 10... Exhaust gas outlet, 11
...Cyclone, 12...Vertical bar, 13...Horizontal bar,
14... Lattice L internal.
Claims (1)
は流動層域に臨んで原料供給口を、また該流動層域に予
備還元生成物の排出口を開口させた構成にかかる流動層
予備還元炉において、炉内の上記流動層域に複数の縦桟
と横桟との組合わせよりなるインターナルを内装設置し
たことを特徴とするインターナルを具える流動層予備還
元炉。1. A fluidizing reducing gas inlet is provided at the bottom of the furnace, a raw material supply port facing the fluidized bed area is provided on the side wall of the furnace, and an outlet for preliminary reduction products is opened in the fluidized bed area. 1. A fluidized bed pre-reduction furnace equipped with an internal comprising a combination of a plurality of vertical bars and horizontal bars installed in the fluidized bed region of the furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21276882A JPS6056991B2 (en) | 1982-12-06 | 1982-12-06 | Fluidized bed pre-reduction furnace with internal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21276882A JPS6056991B2 (en) | 1982-12-06 | 1982-12-06 | Fluidized bed pre-reduction furnace with internal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59104078A JPS59104078A (en) | 1984-06-15 |
| JPS6056991B2 true JPS6056991B2 (en) | 1985-12-12 |
Family
ID=16628072
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21276882A Expired JPS6056991B2 (en) | 1982-12-06 | 1982-12-06 | Fluidized bed pre-reduction furnace with internal |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6056991B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991009261A1 (en) * | 1989-12-08 | 1991-06-27 | Kawasaki Steel Corporation | Fluidized bed gas sparger |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2021118993A (en) | 2018-04-23 | 2021-08-12 | 石原産業株式会社 | Internal, fluidized bed reaction apparatus, and method for manufacturing trifluoromethyl pyridine-based compound |
-
1982
- 1982-12-06 JP JP21276882A patent/JPS6056991B2/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991009261A1 (en) * | 1989-12-08 | 1991-06-27 | Kawasaki Steel Corporation | Fluidized bed gas sparger |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59104078A (en) | 1984-06-15 |
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