JPH0216364B2 - - Google Patents
Info
- Publication number
- JPH0216364B2 JPH0216364B2 JP59225048A JP22504884A JPH0216364B2 JP H0216364 B2 JPH0216364 B2 JP H0216364B2 JP 59225048 A JP59225048 A JP 59225048A JP 22504884 A JP22504884 A JP 22504884A JP H0216364 B2 JPH0216364 B2 JP H0216364B2
- Authority
- JP
- Japan
- Prior art keywords
- reduction furnace
- exhaust gas
- temperature
- iron ore
- gas
- 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 - Lifetime
Links
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 64
- 239000007789 gas Substances 0.000 claims description 64
- 229910052742 iron Inorganic materials 0.000 claims description 31
- 238000003723 Smelting Methods 0.000 claims description 18
- 238000002844 melting Methods 0.000 claims description 12
- 230000008018 melting Effects 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000003575 carbonaceous material Substances 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 description 10
- 238000006114 decarboxylation reaction Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- 239000012159 carrier gas Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
- C21B13/143—Injection of partially reduced ore into a molten bath
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
- C21B13/029—Introducing coolant gas in the shaft furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
- C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
- C21B2100/64—Controlling the physical properties of the gas, e.g. pressure or temperature
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture Of Iron (AREA)
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は鉄鉱石の溶融還元方法に関し、さらに
詳しくは、鉄鉱石の予備還元ガスに溶融還元炉の
排ガスを用い、かつ、この排ガスの昇温に予備還
元炉の排ガスを使用する鉄鉱石の溶融還元方法に
関するものである。[Detailed Description of the Invention] [Field of Industrial Application] The present invention relates to a method for smelting and reducing iron ore, and more specifically, the present invention relates to a method for smelting and reducing iron ore. The present invention relates to a method for melting and reducing iron ore using the exhaust gas from a preliminary reduction furnace.
［従来技術］
従来において、鉄鉱石を予備還元後、溶融還元
炉において溶融して溶鉄を製造するに際して、原
料の鉄鉱石は常温において直接予備還元炉に装入
し、そして、還元用のガスは溶融還元炉からの排
ガスを冷却、脱炭酸してから間接ガスヒーターに
より加熱してから、予備還元炉の直前の入口側に
ある自燃式昇温機により鉄鉱石の還元に必要な温
度に昇温して、予備還元炉に供給して鉄鉱石の予
備還元を行ない、予備還元された鉄鉱石を冷却し
てから溶融還元炉に装入したのである。[Prior Art] Conventionally, when iron ore is pre-reduced and then melted in a smelting reduction furnace to produce molten iron, the raw material iron ore is directly charged into the pre-reduction furnace at room temperature, and the reducing gas is The exhaust gas from the smelting reduction furnace is cooled and decarboxylated, then heated by an indirect gas heater, and then raised to the temperature required for iron ore reduction by a self-combustion temperature riser located on the inlet side just before the preliminary reduction furnace. The iron ore was then supplied to a pre-reduction furnace for pre-reduction, and the pre-reduced iron ore was cooled before being charged into a smelting reduction furnace.
しかし、このような方法においては、間接ガス
ヒーターにおいては燃料を間接的に燃焼させるの
で熱損失が大きく、また、自燃式昇温機は予備還
元炉の直前の入口側に設置されているので、溶融
還元炉からの冷却され、脱炭酸された排ガス中の
CO2、H2Oの量が増加し、酸化度が上昇し、予備
還元炉における滞留時間が長くなると共に循環系
統へのガス量が多くなるという問題がある。 However, in such a method, the heat loss is large because the fuel is burned indirectly in the indirect gas heater, and the self-combustion temperature riser is installed on the inlet side just before the pre-reducing furnace. in the cooled and decarboxylated exhaust gas from the smelting reduction furnace.
There are problems in that the amount of CO 2 and H 2 O increases, the degree of oxidation increases, the residence time in the pre-reduction furnace increases, and the amount of gas flowing into the circulation system increases.
［発明が解決しようとする問題点］
本発明は上記に説明した溶融還元炉からの排ガ
スの予備還元炉に供給する時の加熱昇温に関して
の種々の問題点に鑑みなされたものであり、即
ち、本発明者が鋭意研究を行なつた結果、予備還
元用のガスは溶融還元炉の排ガスを、自燃式昇温
機により昇温した予備還元炉から排出したガスと
熱交換して昇温し、予備還元に使用することによ
り、予備還元用の還元ガスの組成を一定とした状
態において、予備還元温度に効果的に昇温して予
備還元が行なうことができる鉄鉱石の溶融還元方
法を開発したのである。[Problems to be Solved by the Invention] The present invention has been made in view of the various problems described above regarding the heating temperature increase when exhaust gas from the smelting reduction furnace is supplied to the preliminary reduction furnace. As a result of the inventor's intensive research, the temperature of the preliminary reduction gas is increased by exchanging heat with the exhaust gas from the smelting reduction furnace and the gas discharged from the preliminary reduction furnace, which has been heated by a self-combustion heating device. Developed an iron ore smelting reduction method that can be used for preliminary reduction to effectively raise the temperature to the preliminary reduction temperature while keeping the composition of the reducing gas for preliminary reduction constant. That's what I did.
［問題点を解決するための手段］
本発明に係る鉄鉱石の溶融還元方法の特徴とす
るところは、鉄鉱石を予備還元炉において予備還
元した後、冷却した鉄鉱石を炭素質材料、造滓剤
および酸素と共に底部から溶融還元炉に装入して
溶鉄を製造するに際して、冷却され、かつ、脱炭
酸されて常温となつた溶融還元炉から排出された
排ガスを、予備還元炉からの排ガスを一部自燃さ
せて昇温した排ガスと熱交換して、予備還元に必
要な温度に昇温して予備還元炉の還元ガスとして
使用することにある。[Means for Solving the Problems] The iron ore smelting reduction method according to the present invention is characterized by pre-reducing iron ore in a pre-reduction furnace and then converting the cooled iron ore into carbonaceous material and slag. When producing molten iron by charging it into a smelting reduction furnace from the bottom together with a chemical agent and oxygen, the exhaust gas discharged from the smelting reduction furnace which has been cooled and decarboxylated to room temperature is used as the exhaust gas from the pre-reduction furnace. The purpose is to partially self-combust and exchange heat with the heated exhaust gas, raise the temperature to the temperature required for preliminary reduction, and use it as reducing gas in the preliminary reduction furnace.
本発明に係る鉄鉱石の溶融還元方法について以
下詳細に説明する。 The method for melting and reducing iron ore according to the present invention will be described in detail below.
先ず、本発明に係る鉄鉱石の溶融還元方法を第
１図に示す系統図により説明する。 First, the method for melting and reducing iron ore according to the present invention will be explained with reference to the system diagram shown in FIG.
鉄鉱石を流動床式の予備還元炉１において、50
〜70％の還元率まで還元した後、予備還元された
鉄鉱石を冷却器８により冷却してから、炭素質材
料、造滓剤、酸素等と共にキヤリヤーガスにより
鉄鉱石を溶融還元炉２の底部から装入して溶鉄
M.Feを製造する際に、溶融還元炉２の上部から
排出された排ガスＣ（約1700℃）は、溶融還元炉
２に設置されている熱交換器５により冷却（約
200℃）されてガスホルダー７に貯蔵され（約140
℃）、次いで、コンプレツサーにより圧縮されて
から冷却され（約100℃）、脱炭酸装置６により
CO2を除去された後にガス−ガス熱交換器４に供
給された排ガスＣ（約25℃）は、このガス−ガス
熱交換器４において、流動床式予備還元炉１から
の排ガスＡは鉄鉱石を還元して温度が約750〜900
℃となるので、この温度の低下した排ガスＡを自
燃式昇温機３において供給された理論的燃焼酸素
により一部自燃させて昇温し高温となつた排ガス
Ｂ（970〜1120℃）と熱交換して昇温された排ガス
Ｄ（800〜950℃）が、流動床式予備還元炉１下部
から供給されて鉄鉱石の還元が進行する。 In a fluidized bed pre-reduction furnace 1, iron ore is
After being reduced to a reduction rate of ~70%, the pre-reduced iron ore is cooled by a cooler 8, and then the iron ore is transferred from the bottom of the smelting reduction furnace 2 together with carbonaceous materials, slag forming agents, oxygen, etc. using a carrier gas. Charge and molten iron
When producing M.Fe, the exhaust gas C (approximately 1700°C) discharged from the upper part of the melting reduction furnace 2 is cooled (approximately
200℃) and stored in gas holder 7 (approximately 140℃).
℃), then compressed by a compressor, cooled (approximately 100℃), and decarboxylated by a decarboxylation device 6.
The exhaust gas C (approximately 25°C) supplied to the gas-gas heat exchanger 4 after CO 2 has been removed is in this gas-gas heat exchanger 4, where the exhaust gas A from the fluidized bed pre-reduction furnace 1 is When reducing the stone, the temperature is about 750-900
℃, so the temperature of this lowered exhaust gas A is partially self-combusted by the theoretical combustion oxygen supplied in the self-combustion type heating machine 3, and the temperature is raised, resulting in high temperature exhaust gas B (970 to 1120℃) and heat. The exchanged and heated exhaust gas D (800 to 950°C) is supplied from the lower part of the fluidized bed pre-reduction furnace 1, and the reduction of the iron ore proceeds.
なお、予備還元炉１へ鉄鉱石を供給する際に、
予熱器９において予備的に鉄鉱石を加熱し、予備
還元炉１からの排ガスＡの温度を予備還元炉１に
供給される排ガスＤの温度より50℃程度低下させ
るように維持するのである。 In addition, when supplying iron ore to the preliminary reduction furnace 1,
The iron ore is preliminarily heated in the preheater 9, and the temperature of the exhaust gas A from the pre-reduction furnace 1 is maintained to be approximately 50° C. lower than the temperature of the exhaust gas D supplied to the pre-reduction furnace 1.
しかして、自燃式昇温機３において、排ガスＡ
（750℃〜900℃）の温度を970−1120℃（排ガス
Ｂ）の範囲に昇温させるのは、970℃未満ではガ
ス−ガス熱交換器４において熱交換された排ガス
Ｄ（流動床式予備還元炉１に供給されるガス）の
温度が800℃未満となり、流動床式予備還元炉１
における鉄鉱石の還元率が50％以下となり、該還
元炉１の容量を大きくしなければならず、かつ、
溶融還元炉２の負荷が大きくなり、また、排ガス
Ｂの温度が1120℃を越えると排ガスＤの温度が
950℃を越えるようになり、鉄鉱石の還元率は70
％以上となり一見好ましいようではあるが、高温
となることにより流動床式予備還元炉１を高温に
耐える設備とするための費用が非常に増大するこ
とおよび設備の維持が困難となる。従つて、予備
還元炉１からの排ガスＡは自燃式昇温機３により
昇温する温度は970〜1120℃（排ガスＢ）とする
のがよい。このように、自燃式昇温機３により流
動床式予備還元炉１により排出される750〜900℃
の排ガスＡを970〜1120℃の排ガスＢとすること
により、予備還元炉１に供給される排ガスＤの温
度を800〜950℃の適温とすることができるのであ
る。 Therefore, in the self-combustion type heating machine 3, the exhaust gas A
(750°C to 900°C) to the range of 970-1120°C (exhaust gas B) is when the temperature is lower than 970°C, the exhaust gas D (fluidized bed preliminary The temperature of the gas (gas supplied to the reduction furnace 1) becomes less than 800℃, and the fluidized bed pre-reduction furnace 1
The reduction rate of iron ore becomes 50% or less, and the capacity of the reduction furnace 1 must be increased, and
When the load on the melting reduction furnace 2 increases and the temperature of the exhaust gas B exceeds 1120℃, the temperature of the exhaust gas D increases.
The temperature exceeds 950℃, and the reduction rate of iron ore is 70
% or more, which seems preferable at first glance, but the high temperature significantly increases the cost of equipping the fluidized bed pre-reduction furnace 1 to withstand high temperatures and makes it difficult to maintain the equipment. Therefore, it is preferable that the temperature of the exhaust gas A from the preliminary reduction furnace 1 to be raised by the self-combustion temperature riser 3 is 970 to 1120°C (exhaust gas B). In this way, the temperature of 750 to 900°C discharged from the fluidized bed pre-reduction furnace 1 by the self-combustion temperature riser 3 is
By setting the exhaust gas A to the exhaust gas B at 970 to 1120°C, the temperature of the exhaust gas D supplied to the preliminary reduction furnace 1 can be set to an appropriate temperature of 800 to 950°C.
なお、ガス−ガス熱交換器４においては、流動
床式予備還元炉１からの排ガス中に含まれるダス
トに影響されない構造の設計とするのが効果的で
あり、この排ガスは脱炭酸装置の前で溶融還元炉
２からの排ガスと混合されて脱炭酸されて、還元
ガスとして利用される。 Note that it is effective to design the gas-gas heat exchanger 4 to have a structure that is not affected by dust contained in the exhaust gas from the fluidized bed pre-reduction furnace 1, and this exhaust gas is removed before the decarboxylation device. It is mixed with the exhaust gas from the melting reduction furnace 2, decarboxylated, and used as a reducing gas.
［実施例］
本発明に係る鉄鉱石の溶融還元方法の実施例を
説明する。[Example] An example of the method for melting and reducing iron ore according to the present invention will be described.
実施例
流動床式予備還元炉で還元されて冷却した予備
還元鉱を72Ton／Hr、炭素質材料として石炭を
37Ton／Hr、造滓剤としてライムを5.70Ton／
Hr、O2を24800Nm3／Hr、キヤリヤーガスを
5290Nm3／Hrを溶融還元炉の底部から吹込み、
溶鉄60Ton／Hr、スラグ12Ton／Hrを得た。一
方、溶融還元炉の上部からの約1700℃の排ガスＣ
（71100Nm3、H2：12Vol％、CO：57Vol％、
CO2：16Vol％、H2O：15Vol％、N2：1Vol％、
圧力1.1ata）を熱交換器５により200℃まで降温
し、約40℃の温度でガスホルダー７に留め、コン
プレツサーにより圧縮して冷却後、脱炭酸装置に
よりCO2を除去した排ガスＤ（圧力4.0ata、
57330Nm3、H2：15Vol％、CO：81Vol％、
CO2：0.6Vol％、H2O：0.8Vol％、N2：2Vol％）
を、ガス−ガス熱交換器により昇温して約900℃
の温度とする。このガス−ガス熱交換器には、流
動床式予備還元炉からの約840℃の排ガスＡ（圧力
3.5ata、57330Nm3、H2：10Vol％、CO：55Vol
％、CO2：27Vol％、H2O：6Vol％、N2：2Vol
％）を自燃式昇温機により理論的酸素量を決定し
て自燃させて温度約1000℃の排ガスＢ（H2：
17Vol％、CO：30Vol％、CO2：45Vol％、
H2O：7Vol％、N2：1Vol％、ダスト：10ｇ／Ｎ
m3）と上記の排ガスＤと熱交換する。Example: 72T/Hr of pre-reduced ore reduced and cooled in a fluidized bed pre-reduction furnace, and coal as the carbonaceous material.
37Ton/Hr, 5.70Ton/Hr with lime as slag forming agent
Hr, O 2 to 24800Nm 3 /Hr, carrier gas
Inject 5290Nm 3 /Hr from the bottom of the melting reduction furnace.
Obtained 60Ton/Hr of molten iron and 12Ton/Hr of slag. On the other hand, the exhaust gas C at about 1700℃ from the upper part of the smelting reduction furnace
( 71100Nm3 , H2 : 12Vol%, CO: 57Vol%,
CO2 : 16Vol%, H2O : 15Vol%, N2 : 1Vol%,
The exhaust gas D (pressure 4.0 ata) is cooled down to 200 degrees Celsius by the heat exchanger 5, kept in the gas holder 7 at a temperature of about 40 degrees Celsius, compressed by the compressor and cooled, and then CO 2 is removed by the decarboxylation device. ata,
57330Nm3 , H2 : 15Vol%, CO: 81Vol%,
CO2 : 0.6Vol%, H2O : 0.8Vol%, N2 : 2Vol%)
is heated to approximately 900℃ using a gas-gas heat exchanger.
temperature. This gas-gas heat exchanger is equipped with exhaust gas A (pressure
3.5ata, 57330Nm3 , H2 :10Vol%, CO:55Vol
%, CO2 : 27Vol%, H2O : 6Vol%, N2 : 2Vol
%) is self-combusted by determining the theoretical amount of oxygen using a self-combustion temperature riser to generate exhaust gas B (H 2 :
17Vol%, CO: 30Vol%, CO2 : 45Vol%,
H 2 O: 7Vol%, N 2 : 1Vol%, Dust: 10g/N
m 3 ) and the above exhaust gas D.
そして、この流動床式予備還元炉における還元
率は70％であつた。 The reduction rate in this fluidized bed pre-reduction furnace was 70%.
［発明の効果］
以上説明したように、本発明に係る鉄鉱石の溶
融還元方法は上記の構成を有しているものである
から、溶融還元炉の排ガスを流動床式予備還元炉
の還元ガスとして有効に利用し、かつ、排ガスの
温度をボイラーに活用し、さらに、流動床式予備
還元炉の排ガスを自燃式昇温機により昇温させて
溶融還元炉の還元ガスを昇温するのに利用し、昇
温させた排ガスは脱炭酸装置の前で溶融還元炉か
らの排ガスと混合して脱炭酸させて還元ガスとし
て利用することができ、各装置において発生する
排ガスおよび温度を有効に利用できるという優れ
た効果を有するものである。[Effects of the Invention] As explained above, since the method for melting and reducing iron ore according to the present invention has the above configuration, the exhaust gas of the melting reduction furnace is converted into the reducing gas of the fluidized bed pre-reduction furnace. In addition, the temperature of the exhaust gas is used in the boiler, and the temperature of the exhaust gas from the fluidized bed pre-reduction furnace is raised by a self-combustion temperature riser to raise the temperature of the reducing gas in the smelting reduction furnace. The heated exhaust gas can be mixed with the exhaust gas from the smelting reduction furnace in front of the decarboxylation equipment, decarboxylated, and used as reducing gas, making effective use of the exhaust gas and temperature generated in each equipment. It has the excellent effect of being able to
第１図は本発明に係る鉄鉱石の溶融還元方法を
説明するための系統図である。
FIG. 1 is a system diagram for explaining the method for melting and reducing iron ore according to the present invention.
Claims (1)
後、冷却した鉄鉱石を炭素質材料、造滓剤および
酸素と共に底部から溶融還元炉に装入して溶鉄を
製造するに際して、冷却され、かつ、脱炭酸され
て常温となつた溶融還元炉から排出された排ガス
を、予備還元炉からの排ガスを一部自燃させて昇
温した排ガスと熱交換して、予備還元に必要な温
度に昇温して流動床式の予備還元炉の還元ガスと
して使用することを特徴とする鉄鉱石の溶融還元
方法。1 After pre-reducing iron ore in a pre-reduction furnace, the cooled iron ore is charged from the bottom into a smelting reduction furnace together with a carbonaceous material, a slag-forming agent and oxygen to produce molten iron. The exhaust gas discharged from the smelting reduction furnace, which has been carbonated and has reached room temperature, is heated to the temperature required for preliminary reduction by exchanging heat with the exhaust gas from the preliminary reduction furnace, which has been partially self-combusted and heated. A method for melting and reducing iron ore, which is characterized in that it is used as a reducing gas in a fluidized bed pre-reduction furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59225048A JPS61104011A (en) | 1984-10-25 | 1984-10-25 | Melt reduction method of iron ore |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59225048A JPS61104011A (en) | 1984-10-25 | 1984-10-25 | Melt reduction method of iron ore |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61104011A JPS61104011A (en) | 1986-05-22 |
| JPH0216364B2 true JPH0216364B2 (en) | 1990-04-17 |
Family
ID=16823220
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59225048A Granted JPS61104011A (en) | 1984-10-25 | 1984-10-25 | Melt reduction method of iron ore |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61104011A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0778249B2 (en) * | 1986-03-28 | 1995-08-23 | 新日本製鐵株式会社 | Smelting reduction method for iron ore |
| JP2514217Y2 (en) * | 1989-07-12 | 1996-10-16 | セイレイ工業株式会社 | Rotational posture adjustment structure of the tiller |
-
1984
- 1984-10-25 JP JP59225048A patent/JPS61104011A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61104011A (en) | 1986-05-22 |
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