JPS6347311A - Smelting, reducing and refining equipment - Google Patents
Smelting, reducing and refining equipmentInfo
- Publication number
- JPS6347311A JPS6347311A JP19246686A JP19246686A JPS6347311A JP S6347311 A JPS6347311 A JP S6347311A JP 19246686 A JP19246686 A JP 19246686A JP 19246686 A JP19246686 A JP 19246686A JP S6347311 A JPS6347311 A JP S6347311A
- Authority
- JP
- Japan
- Prior art keywords
- coal
- exhaust gas
- furnace
- smelting
- temp
- 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.)
- Pending
Links
- 238000003723 Smelting Methods 0.000 title claims abstract description 36
- 238000007670 refining Methods 0.000 title claims description 9
- 239000003245 coal Substances 0.000 claims abstract description 60
- 238000011084 recovery Methods 0.000 claims abstract description 21
- 238000001035 drying Methods 0.000 claims description 22
- 239000007789 gas Substances 0.000 abstract description 60
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 16
- 229910052742 iron Inorganic materials 0.000 abstract description 8
- 239000000843 powder Substances 0.000 abstract description 6
- 238000010298 pulverizing process Methods 0.000 abstract description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract description 4
- 235000011941 Tilia x europaea Nutrition 0.000 abstract description 4
- 239000004571 lime Substances 0.000 abstract description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 3
- 239000001301 oxygen Substances 0.000 abstract description 3
- 229910052760 oxygen Inorganic materials 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 2
- 238000007664 blowing Methods 0.000 abstract 3
- 239000002994 raw material Substances 0.000 abstract 2
- 239000000446 fuel Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000002844 melting Methods 0.000 description 7
- 230000008018 melting Effects 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 5
- 229910001882 dioxygen Inorganic materials 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 238000005192 partition Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910000805 Pig iron Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 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
- 238000004519 manufacturing process Methods 0.000 description 2
- 241001070941 Castanea Species 0.000 description 1
- 235000014036 Castanea Nutrition 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
Landscapes
- Manufacture Of Iron (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野〕
この発明は、鉄鉱石を石炭及び石灰と共に精錬炉内の溶
銑中に吹き込み、ランス及び底部羽口から酸素ガスを吹
き込んで溶銑を得る溶融還元精錬設備に関し、更に詳述
すれば、石炭の水分を極めて少なくして最適の条件で溶
融還元操業する溶融還元精錬設備に関する。Detailed Description of the Invention [Industrial Application Field] This invention is a smelting reduction method in which iron ore is blown into molten pig iron in a smelting furnace together with coal and lime, and oxygen gas is blown into the molten pig iron through a lance and a bottom tuyere. The present invention relates to smelting equipment, and more specifically, to a smelting reduction smelting equipment that performs smelting and reduction operations under optimum conditions with extremely low water content in coal.
［従来の技術］
溶融還元ｒ′ｒ４ｉｉ法は高炉製鉄法に代るものであり
、高炉製鉄法においては、高炉の建設費が高く広大な敷
地が必要であるという高炉製鉄法の欠点を解消すべく、
近年に至り開発されたものである。このような溶融還元
精錬法においては、精錬炉内の溶銑中に炉底に設けた羽
口から予備還元された鉱石並びに粉末状の石炭及び石灰
を吹き込み、更に別の羽口から酸素ガスを溶銑中に吹き
込むと共に、炉頂部から炉内に装入されたランスを介し
て溶銑に酸素ガスを吹き付ける。そうすると、石炭が溶
銑中に溶解すると共に、石炭の炭素が酵素ガスによって
酸化される。そして、この酸化熱によって鉱石が溶融す
ると共に、鉱石が石炭中の炭素によって還元される。溶
銑から発生するＣＯガスはランスから吹き付けられる酸
素ガスによって２次燃焼されてＣＯ２ガスになる。この
ＣＯ２ガスの顕熱は溶銑上を覆っているフォーミング状
のスラブに伝達され１次いで、溶銑に戻される。[Prior art] The smelting reduction r'r4ii method is an alternative to the blast furnace iron manufacturing method, and it eliminates the drawbacks of the blast furnace iron manufacturing method, such as the high construction cost of the blast furnace and the need for a vast site. As much as possible
It has been developed in recent years. In such a smelting reduction smelting method, pre-reduced ore, powdered coal and lime are injected into the hot metal in the smelting furnace through a tuyere provided at the bottom of the furnace, and oxygen gas is injected into the hot metal from another tuyere. At the same time, oxygen gas is blown into the hot metal from the top of the furnace through a lance inserted into the furnace. Then, the coal is dissolved in the hot metal, and the carbon in the coal is oxidized by the enzyme gas. Then, the ore is melted by this oxidation heat, and the ore is reduced by the carbon in the coal. CO gas generated from hot metal is secondary combusted by oxygen gas blown from a lance and becomes CO2 gas. The sensible heat of this CO2 gas is transferred to the forming slab covering the hot metal, and then returned to the hot metal.
［発明が解決しようとする問題点〕
ところで、この溶融還元プロセスにおいては、石炭の水
分巳が季節により又は天候により大きく変動する。例え
ば、冬期においては水分含有旦が６乃至７％であるが、
梅雨時には１５乃至１６％に上昇し、また、それ以外の
季節にも天候により９乃至１３％に変動する。このよう
に石炭の水分量が変動すると、水分の蒸発分解に必要な
熱量が変動し、溶融還元炉に投入すべき熱源としての石
炭量が変動する。換言すれば、操業状態を一定に維持す
るために、石炭の吹込み農を増減する必要があり、これ
が溶融還元操業を複雑化させる要因になっている。また
、石炭を粉砕して粉末状にした後、これを溶融還元炉に
吹込んでいるが、湿ったまま石炭を粉砕すると、多大の
動力が必要であるという問題点もある。[Problems to be Solved by the Invention] Incidentally, in this melting reduction process, the moisture level of coal varies greatly depending on the season or the weather. For example, in winter, the moisture content is 6 to 7%,
During the rainy season, it rises to 15 to 16%, and in other seasons, it fluctuates to 9 to 13% depending on the weather. When the moisture content of coal fluctuates in this way, the amount of heat required for evaporative decomposition of the moisture fluctuates, and the amount of coal that should be input into the smelting reduction furnace as a heat source fluctuates. In other words, in order to maintain a constant operating state, it is necessary to increase or decrease the amount of coal injection, and this becomes a factor that complicates the smelting reduction operation. Furthermore, after the coal is pulverized into powder, it is blown into the smelting reduction furnace, but there is a problem in that a large amount of power is required if the coal is pulverized while it is still wet.
この発明は、かかる事情に鑑みてなされたものであって
、溶融還元炉に吹込む石炭を予め乾燥することにより、
石炭粉砕の動力を軽減すると共に、溶融還元操業を安定
して実施することができる溶融還元量ｍ設備を提供する
ことを目的とする。This invention was made in view of such circumstances, and by drying the coal beforehand to be blown into the melting reduction furnace,
It is an object of the present invention to provide a smelting reduction amount m facility capable of reducing power for coal pulverization and stably implementing smelting reduction operation.
［問題点を解決するための手段］
この発明に係る溶融還元精錬設備は、溶融還元炉と、こ
の溶融還元炉の排ガスからその顕熱の一部を回収する熱
回収手段と、この熱回収手段から出た排ガスを導入し排
ガスの顕熱により石炭を乾燥する乾燥装置と、を有し、
乾燥装置により乾燥された石炭を溶融還元炉に供給する
ことを特徴とする。[Means for Solving the Problems] The smelting reduction refining equipment according to the present invention includes a smelting reduction furnace, a heat recovery means for recovering a part of the sensible heat from the exhaust gas of the smelting reduction furnace, and this heat recovery means. A drying device that introduces the exhaust gas emitted from the coal and dries the coal using the sensible heat of the exhaust gas,
It is characterized by supplying the coal dried by the drying device to the melting reduction furnace.
［作用コ
溶融還元炉にて精錬中に発生する排ガスの組成は、炭酸
ガス（ＣＯ２ガス）が約２０乃至５０％、水素ガス（Ｈ
２ガス）が約５乃至２０％、及び−酸化炭素ガス（Ｃｏ
ガス）が３０乃至５０％である。つまり、この排ガスは
酸素ガス（０２ガス）を含有していないか、又はその含
有量が少ないので、この排ガスを石炭の乾燥に利用して
も、石炭との反応が起きるおそれがない。また、この排
ガスを熱回収手段に通してその顕熱の一部を回収し、排
ガスを冷却した後、石炭の乾燥に利用することにより、
任意の温度で石炭を乾燥することができる。これにより
、石炭の水分を所定値に調整することができる。[Effects] The composition of the exhaust gas generated during refining in the smelting reduction furnace is approximately 20 to 50% carbon dioxide gas (CO2 gas) and hydrogen gas (H2 gas).
2 gas) about 5 to 20%, and - carbon oxide gas (Co
gas) is 30 to 50%. In other words, since this exhaust gas does not contain oxygen gas (02 gas) or its content is small, even if this exhaust gas is used for drying coal, there is no risk of reaction with coal. In addition, by passing this exhaust gas through a heat recovery means to recover a part of its sensible heat and cooling the exhaust gas, it is used for drying coal.
Coal can be dried at any temperature. Thereby, the moisture content of the coal can be adjusted to a predetermined value.
［実施例］
第１図はこの発明の実施例に係る溶融還元精錬役儀を示
すブロック図である。溶融還元炉１にてｙＩｇｌ中に発
生する排ガスは、予備還元炉２に導入され、予備還元炉
２にて鉱石の予備還元に利用される。予備還元炉２を出
た排ガスは、集ａ区３により除「された後、高温熱回収
部４に供給される。[Embodiment] FIG. 1 is a block diagram showing a melting reduction refining apparatus according to an embodiment of the present invention. The exhaust gas generated in yIgl in the smelting reduction furnace 1 is introduced into the preliminary reduction furnace 2, and is used in the preliminary reduction furnace 2 for preliminary reduction of ore. The exhaust gas exiting the preliminary reduction furnace 2 is removed by the collection section 3 and then supplied to the high-temperature heat recovery section 4.
この高温熱回収部４は排ガスの顕熱を高温高圧の蒸気と
して回収する熱交換器等により構成され、排ガスの顕熱
はこの熱回収部４にて蒸気の加熱等に使用される。熱回
収部４を出た排ガスは、約１８０乃至２００℃まで降温
しており、この排ガスの一部が石炭乾燥装置６に供給さ
れ、残部は低温熱回収部５に供給される。The high-temperature heat recovery section 4 includes a heat exchanger and the like that recovers the sensible heat of the exhaust gas as high-temperature, high-pressure steam, and the sensible heat of the exhaust gas is used in the heat recovery section 4 to heat the steam. The temperature of the exhaust gas exiting the heat recovery section 4 has decreased to approximately 180 to 200° C., and a portion of this exhaust gas is supplied to the coal drying device 6 and the remainder is supplied to the low temperature heat recovery section 5.
低温熱回収部５にて、排ガスの持つ顕熱は更に回収され
、次いで、排ガスは下工程に送られる。Sensible heat possessed by the exhaust gas is further recovered in the low-temperature heat recovery section 5, and then the exhaust gas is sent to a lower process.
石炭乾燥装置６は、公知の乾燥装置で構成することがで
き、例えば、流動層タイプ、固定層タイプ又は多管式タ
イプ等、のちのを使用すればよいが、乾燥効率上は流動
層タイプのものが好ましい。この流動層タイプのものは
、図示のように、ホッパの底部に多数の孔を開設した仕
切り板６１を配設し、このホッパの上部から生石炭を投
入すると共に、仕切り板６１の下方から仕切り板６１の
孔を介して排ガスをホッパ内に吹込む。石炭は吹き込み
ガスにより浮遊状態におかれ、この状態で乾燥されてホ
ッパ下部の排出口から排出される。The coal drying device 6 can be configured with a known drying device, such as a fluidized bed type, fixed bed type, or multi-tube type, but in terms of drying efficiency, a fluidized bed type is preferable. Preferably. As shown in the figure, in this fluidized bed type, a partition plate 61 with many holes is provided at the bottom of the hopper, raw coal is charged from the top of the hopper, and the partition plate 61 is inserted from below the partition plate 61. The exhaust gas is blown into the hopper through the holes in the plate 61. The coal is suspended by the blown gas, dried in this state, and discharged from the outlet at the bottom of the hopper.
乾燥装置６から排出された乾燥石炭は、ホッパ７に一旦
貯留された後、次工程の粉砕工程に送られる。この粉砕
工程で微粉状に粉砕された石炭は、溶融還元炉１に送ら
れて精錬に供される。乾燥装［６内に吹き込まれたガス
はそのホッパ内を・上昇し、ブロア９により吸引されて
上部のガス排出口から排出される。乾燥装置６とブロア
９・との間には、集Ｗｉ機８が配設されており、乾燥装
置６を出た排ガス中の微粉炭はこの集塵機８によりガス
流から分離されて集められる。集ｍｍ８により回収され
た微粉炭はホッパ７に供給され、微粉炭が除去された排
ガスは低温熱回収部５により熱回収された排ガスと共に
、下工程に送られる。The dry coal discharged from the drying device 6 is once stored in a hopper 7, and then sent to the next pulverization process. The coal pulverized into fine powder in this pulverization process is sent to the melting reduction furnace 1 and subjected to refining. The gas blown into the drying device [6 rises in the hopper, is sucked by the blower 9, and is discharged from the gas outlet at the top. A collector 8 is disposed between the dryer 6 and the blower 9, and the pulverized coal in the exhaust gas exiting the dryer 6 is separated from the gas flow and collected by the dust collector 8. The pulverized coal collected by the collector mm8 is supplied to the hopper 7, and the exhaust gas from which the pulverized coal has been removed is sent to the lower process together with the exhaust gas whose heat has been recovered by the low-temperature heat recovery section 5.
このように構成された溶融還元ｖｉ錬設６７ｇにおいて
は、溶融還元炉１にて発生した排ガスは予備還元炉２に
供給されて鉱石の予備還元に使用された後、栗塁機３に
より除塵されて高温熱回収部４に送られる。排ガスは高
温熱回収部４の入口で約７００℃の温度を有しており、
この顕熱は、例えば、高圧高温の蒸気として回収される
。高温熱回収部４を出た排ガスは約２００℃の温度を有
しており、この比較的低温の排ガスの一部は乾燥装置６
に供給される。In the smelting reduction VI smelting facility 67g configured in this manner, the exhaust gas generated in the smelting reduction furnace 1 is supplied to the preliminary reduction furnace 2 and used for preliminary reduction of ore, and then dust is removed by the chestnut machine 3. and sent to the high-temperature heat recovery section 4. The exhaust gas has a temperature of about 700°C at the inlet of the high-temperature heat recovery section 4,
This sensible heat is recovered as, for example, high-pressure, high-temperature steam. The exhaust gas leaving the high-temperature heat recovery section 4 has a temperature of approximately 200°C, and a portion of this relatively low-temperature exhaust gas is transferred to the drying device 6.
is supplied to
この排ガスは酸素を含まないから、乾燥装置６内に直接
吹き込むことができ、乾燥装置６内に吹ぎ込まれた排ガ
スは石炭の乾燥に利用された後、ブロア９により吸引さ
れて乾燥装置６の頂部のガス排出口から排出される。こ
のガスは集晧機８により、ガス中の微粉炭が除去され、
回収された微粉炭はホッパ７に供給される。乾燥装置６
においては、その頭部から生石炭が投入され、底部から
吹き込まれる排ガスにより浮遊した状態で乾燥される。Since this exhaust gas does not contain oxygen, it can be directly blown into the drying device 6. After being used for drying the coal, the exhaust gas blown into the drying device 6 is sucked by the blower 9 and is sucked into the drying device 6. The gas is discharged from the gas outlet at the top of the unit. The pulverized coal in the gas is removed from this gas by a collector 8.
The recovered pulverized coal is supplied to a hopper 7. Drying device 6
Raw coal is fed into the top of the coal mine and dried while suspended by the exhaust gas blown in from the bottom.
この乾燥後の石炭は乾燥装置６の底部からホッパ７に移
装される。ホッパ７内の乾燥石炭は、次工程の粉砕装＠
（図示せず）に搬入され、この粉砕装置により微粉状に
粉砕される。この微粉炭は溶融還元炉１に供給され、精
錬に供される。高温熱回収部４を出た排ガスの残部は、
低温熱回収部５により熱回収されて下工程に送られる。This dried coal is transferred from the bottom of the drying device 6 to the hopper 7. The dry coal in hopper 7 is sent to the pulverizer for the next process.
(not shown) and is pulverized into a fine powder by this pulverizer. This pulverized coal is supplied to the smelting reduction furnace 1 and subjected to refining. The remainder of the exhaust gas leaving the high temperature heat recovery section 4 is
The heat is recovered by the low-temperature heat recovery section 5 and sent to the lower process.
この発明においては、溶融還元炉１に吹きこむ石炭は、
予め乾燥されており、水分が極めて少ないと共に、その
水分の変動量も少ない。このため、？Ｉ？融還元炉１内
で水分の分解に消費される熱量が減少し、熱源としての
所要石炭量を削減することができる。また、水分の変動
が少ないから、安定して溶融還元精錬操業することがで
きる。また、石炭を予め乾燥させた後粉砕するから、石
炭の粉砕のための動力を低減することができる。この発
明においては、高温高圧の蒸気等として排ガスの顕熱を
回収した後、約２００℃以下に降温して熱回収が困Ｈな
比較的低温の排ガスを利用して石炭を乾燥する。従って
、排ガスの顕熱を極めて有効に利用することができる。In this invention, the coal blown into the melting reduction furnace 1 is
It has been dried in advance and has extremely low moisture content, as well as small fluctuations in moisture content. For this reason,? I? The amount of heat consumed for decomposing water in the fusion furnace 1 is reduced, and the amount of coal required as a heat source can be reduced. Furthermore, since there is little variation in moisture content, stable smelting reduction refining operations can be performed. In addition, since the coal is pulverized after being dried in advance, the power required for pulverizing the coal can be reduced. In this invention, the sensible heat of the exhaust gas is recovered as high-temperature, high-pressure steam, etc., and then the temperature is lowered to about 200° C. or less, and the relatively low-temperature exhaust gas, which is difficult to recover, is used to dry the coal. Therefore, the sensible heat of the exhaust gas can be used extremely effectively.
なお、溶融還元炉１の排ガスを予備還元炉２を経由せず
、直接高温熱回収部４に供給してもよいことは勿論であ
る。It goes without saying that the exhaust gas from the melting reduction furnace 1 may be directly supplied to the high temperature heat recovery section 4 without passing through the preliminary reduction furnace 2.
［発明の効果〕
この発明によれば、溶融還元炉に吹きこむ石炭を予め乾
燥して水分を除去するので、水分の分解に要する熱量が
不要で熱源としての石炭量を低減することができる。ま
た、水分が少ないので、石炭の粉砕に要する動力を軽減
することができる。[Effects of the Invention] According to the present invention, since the coal blown into the smelting reduction furnace is dried in advance to remove moisture, the amount of heat required to decompose the moisture is unnecessary, and the amount of coal used as a heat source can be reduced. Furthermore, since the water content is low, the power required for pulverizing the coal can be reduced.
更に、熱回収が困難な低温の排ガスを石炭の乾燥に使用
するので、溶融還元炉の排ガスを有効に使用することが
できると共に、排ガス中には酸素が含有されていないの
で、乾燥装置内に直接吹きこむことができ、石炭の加熱
効率が高い。Furthermore, since low-temperature exhaust gas, which is difficult to recover, is used to dry the coal, the exhaust gas from the smelting reduction furnace can be used effectively, and since the exhaust gas does not contain oxygen, it is possible to It can be blown directly into the coal and has high heating efficiency.
第１図はこの発明の実施例に係る溶融還元精錬設備を示
すブロック図である。FIG. 1 is a block diagram showing a smelting reduction refining facility according to an embodiment of the present invention.
Claims (1)
一部を回収する熱回収手段と、この熱回収手段から出た
排ガスを導入し排ガスの顕熱により石炭を乾燥する乾燥
装置と、を有し、乾燥装置により乾燥された石炭を溶融
還元炉に供給することを特徴とする溶融還元精錬設備。A smelting reduction furnace, a heat recovery means for recovering a part of the sensible heat from the exhaust gas of the smelting reduction furnace, a drying device for introducing the exhaust gas emitted from the heat recovery means and drying the coal using the sensible heat of the exhaust gas, A smelting reduction refining facility characterized in that it has a drying device and supplies coal dried by a drying device to a smelting reduction furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19246686A JPS6347311A (en) | 1986-08-18 | 1986-08-18 | Smelting, reducing and refining equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19246686A JPS6347311A (en) | 1986-08-18 | 1986-08-18 | Smelting, reducing and refining equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6347311A true JPS6347311A (en) | 1988-02-29 |
Family
ID=16291764
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP19246686A Pending JPS6347311A (en) | 1986-08-18 | 1986-08-18 | Smelting, reducing and refining equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6347311A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02175808A (en) * | 1988-12-28 | 1990-07-09 | Nkk Corp | Smelting reduction iron-making equipment |
| JPH03280645A (en) * | 1990-03-28 | 1991-12-11 | Matsushita Electric Ind Co Ltd | Data phase modulation circuit |
| CN112725556A (en) * | 2021-01-19 | 2021-04-30 | 付光明 | Method and device for heating pulverized coal by using blast furnace molten iron dedusting circulating hot flue gas |
-
1986
- 1986-08-18 JP JP19246686A patent/JPS6347311A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02175808A (en) * | 1988-12-28 | 1990-07-09 | Nkk Corp | Smelting reduction iron-making equipment |
| JPH03280645A (en) * | 1990-03-28 | 1991-12-11 | Matsushita Electric Ind Co Ltd | Data phase modulation circuit |
| CN112725556A (en) * | 2021-01-19 | 2021-04-30 | 付光明 | Method and device for heating pulverized coal by using blast furnace molten iron dedusting circulating hot flue gas |
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