JPS63171804A - Utilization of oxygen blast furnace gas - Google Patents
Utilization of oxygen blast furnace gasInfo
- Publication number
- JPS63171804A JPS63171804A JP62001851A JP185187A JPS63171804A JP S63171804 A JPS63171804 A JP S63171804A JP 62001851 A JP62001851 A JP 62001851A JP 185187 A JP185187 A JP 185187A JP S63171804 A JPS63171804 A JP S63171804A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- blast furnace
- oxygen blast
- furnace gas
- reaction
- 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
- 239000007789 gas Substances 0.000 title claims abstract description 59
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 33
- 239000001301 oxygen Substances 0.000 title claims abstract description 32
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000012535 impurity Substances 0.000 claims abstract description 9
- 239000000428 dust Substances 0.000 claims abstract description 6
- 239000003345 natural gas Substances 0.000 claims abstract description 5
- 238000000034 method Methods 0.000 claims description 9
- 239000000571 coke Substances 0.000 claims description 4
- 239000002737 fuel gas Substances 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 2
- 230000000630 rising effect Effects 0.000 abstract 1
- 238000006467 substitution reaction Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 150000002926 oxygen Chemical class 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
Landscapes
- Blast Furnaces (AREA)
Abstract
Description
【発明の詳細な説明】 「発明の目的」 （産業上の利用分野） 酸素高炉から発生する高炉ガスの処理利用技術。[Detailed description of the invention] "Purpose of invention" (Industrial application field) Technology for processing and utilizing blast furnace gas generated from oxygen blast furnaces.
（従来の技術）
高濃度の酸素を高炉羽口から吹込んで操業することによ
って有利な操業をなすことが可能であり、斯うした方法
については特開昭６０−１５９１０４号公報に記載され
ている。(Prior art) Advantageous operations can be achieved by injecting high-concentration oxygen through the blast furnace tuyere, and such a method is described in JP-A-60-159104. .
（発明が解決しようとする問題点）
上記のような従来の酸素高炉から発生する高炉ガスは、
一般的には１３００〜２０００Ｋｃａ１７Ｎｎｆとカロ
リーが普通高炉から発生する高炉ガスより高いので、こ
の酸素高炉ガスを普通高炉ガスの回収利用系において利
用することは極めて運用上の困難性を伴う。(Problems to be solved by the invention) The blast furnace gas generated from the conventional oxygen blast furnace as described above is
Generally, it has a calorific value of 1,300 to 2,000 Kcal and 17 Nnf, which is higher than that of blast furnace gas generated from an ordinary blast furnace, so it is extremely difficult to use this oxygen blast furnace gas in a recovery and utilization system for ordinary blast furnace gas.
そこでこの酸素高炉ガスを全く別個の貯蔵ないし配管設
備を設けて利用することも考えられるが、そのための設
備費ないし機器費が莫大となり実質的に困難である。Therefore, it is conceivable to utilize this oxygen blast furnace gas by providing a completely separate storage or piping facility, but this would require enormous equipment costs and would be practically difficult.
「発明の構成」
（問題点を解決するための手段）
本発明は上記したような従来のものの問題点を解消する
ように創案されたもので、酸素高炉ガスを粗集塵してか
ら脱ＣＯおよび脱Ｓ処理し、次いでＨ２／ＣＯ比を調整
したものを反応塔に送って反応せしめ、不純分を除去し
て代替天然ガスを得ることを特徴とする酸素高炉ガスの
利用方法である。"Structure of the Invention" (Means for Solving the Problems) The present invention was devised to solve the problems of the conventional products as described above. This is a method of utilizing oxygen blast furnace gas, which is characterized in that it undergoes S removal treatment, and then sends the gas with an adjusted H2/CO ratio to a reaction tower for reaction, removes impurities, and obtains an alternative natural gas.
（作用）
粗菓じんされた酸素高炉ガスを脱ＣＯ即ちＣ調整をなし
且つ脱Ｓすることによって、後段反応塔における反応触
媒の被毒による活性度低下を回避する。(Function) By removing CO, that is, adjusting C, and removing S from the oxygen blast furnace gas which has been reduced to coarse dust, a reduction in activity due to poisoning of the reaction catalyst in the latter reaction tower is avoided.
又Ｈ２ガス、コークス炉ガス、スチームなどによりＣＯ
とＨ２の比を調整することにより例えばＨ２／ＣＯ比が
大きいと、メタン生成に有利であり、この比が小さくな
るとエタン、プロパン等の０２の炭化水素が生成しやす
くなると云うように、生成ガスのコントロールが可能で
ある。Also, CO is removed by H2 gas, coke oven gas, steam, etc.
By adjusting the ratio of H2 and H2, for example, if the H2/CO ratio is large, it is advantageous for methane production, and if this ratio is small, it becomes easier to produce 02 hydrocarbons such as ethane and propane. control is possible.
更に反応塔で、例えば２０〜３０ｋｇ／ａＪ、３００〜
５００℃の操作条件により反応させることにより炭化水
素化反応 ＧＯ＋３Ｈｚ −’ＣＨ４＋Ｈ２０，２ＣＯ
＋２Ｈ！ −ＣＨ４＋ｃｏ＊、Ｃｏ２＋４Ｈ２−’ＣＨ
４＋２Ｈ！Ｏ、ＣＯ＋Ｈ！０−４ＣＯ２＋）（、の進行
を速めると共に熱量を更に高める。Furthermore, in a reaction tower, for example, 20 to 30 kg/aJ, 300 to
Hydrocarbonization reaction by reacting under operating conditions of 500℃ GO+3Hz -'CH4+H20,2CO
+2H! -CH4+co*, Co2+4H2-'CH
4+2H! O, CO+H! 0-4CO2+)(,) and further increases the amount of heat.
反応塔出口ガス中のＣ０１ＣＯ□、Ｎｚ ｓ Ｈｚのよ
うな不純物を除（ことにより１００００〜１１０００
Ｋｃａｌ ／Ｎｒｒｒ程度の好ましい代替燃料ガスが得
られる。Removal of impurities such as CO1CO□ and Nz s Hz in the reaction tower outlet gas (possibly 10,000 to 11,000
A preferable alternative fuel gas of about Kcal/Nrrr is obtained.
即ち本発明者等は上記したような酸素高炉ガスの好まし
い利用法について種々の検討を重ねた結果、上記酸素高
炉ガスにおいてはＮｉ分が少く、Ｃｏ、ｃｏ、、Ｈ２が
主成分であり、このような酸素高炉ガス成分のうちでＣ
Ｏおよび８分を除去し、しかもＨ２ガス、コークス炉ガ
ス、スチームなどによりＣＯとＨ２の比率を調整するこ
とにより容易に代替天然ガス化し得ることを確認した。That is, as a result of various studies on the preferable use of the oxygen blast furnace gas as described above, the present inventors found that the oxygen blast furnace gas has a low Ni content and the main components are Co, co, and H2. Among the oxygen blast furnace gas components, C
It was confirmed that natural gas can be easily substituted by removing O and 8% and adjusting the ratio of CO and H2 using H2 gas, coke oven gas, steam, etc.
前記したＣＯ除去は吸着法、溶液吸着法などによって適
切に実施することができる。又脱Ｓは水添吸着法などに
よって的確に達成し得る。ＣｏとＨ２の比率に関しては
一般的にＨｚ／Ｃｏ比を２゜６〜４．５程度とする。即
ちＨ，／Ｃｏが２６６以下では触媒の表面に炭素質の析
出２ＣＯ→ＣＯ□＋Ｃを生じ触媒の活性を著しく低下さ
せる。又このＨｔ／Ｃｏが４．５を越えるときは生成ガ
スが目標とするカロリー（１１０００Ｋｃａｌ／Ｎｒｒ
ｒ）よりも低く、カロリーアップ用のＬＰＧの使用量が
多くなり、製造コストのアップにつながる。反応塔にお
ける操作条件は一般的に２０〜３０ｋＪｒ／−で、且つ
３００〜５００℃である。即ち２０−／−未満であれば
炭素質の析出が、又、圧力が高いと動力費がかさみ、高
製造コストとなる。５００℃以上であると、炭化水素化
反応の進行が遅くなる。The above-mentioned CO removal can be appropriately carried out by an adsorption method, a solution adsorption method, or the like. Further, the removal of S can be accurately achieved by a hydrogenation adsorption method or the like. Regarding the ratio of Co and H2, the Hz/Co ratio is generally set to about 2.6 to 4.5. That is, when H,/Co is less than 266, carbonaceous deposits 2CO→CO□+C are formed on the surface of the catalyst, which significantly reduces the activity of the catalyst. Also, when this Ht/Co exceeds 4.5, the generated gas has the target calorie (11000Kcal/Nrr
r), and the amount of LPG used to increase calories increases, leading to an increase in manufacturing costs. The operating conditions in the reaction tower are generally 20-30 kJr/- and 300-500°C. That is, if the pressure is less than 20 -/-, carbonaceous substances will precipitate, and if the pressure is high, the power cost will increase, leading to high manufacturing costs. If the temperature is 500°C or higher, the progress of the hydrocarbonization reaction will be slow.
又、３００℃以下にするためには、多量の冷却水が必要
となり、動力コストがかさむ。なお反応塔においてはＮ
ｉ系、Ｒｕ系、Ｃｏ系などの触媒を用いて反応させる。Further, in order to lower the temperature to 300° C. or lower, a large amount of cooling water is required, which increases the power cost. Note that in the reaction tower, N
The reaction is carried out using an i-based, Ru-based, or Co-based catalyst.
上記したような本発明方法を実施する設備の概要を添附
図面について説明すると、酸素高炉１０の炉頂から得ら
れる酸素高炉ガス１は粗菓しん機２で除塵された後、そ
の一部は燃焼器３で適宜に酸素などが添加燃焼されて高
温化されてから前記酸素高炉ｌＯのシャフト部に供給さ
れ、該酸素高炉１０に装入された原料を予熱するように
成っている。前記酸素高炉１０から排出され粗菓塵され
た酸素高炉ガス１の残部は圧送機構４を介して脱Ｓ機構
５および脱ＣＯ機構６に順次供給され、脱ＣＯ機構６は
コンプレッサーのような昇圧機構７及びＨ２源導入装置
１６を介して反応塔８に接続されている。反応塔８は冷
却機構９を介して不純分除去器１５に接続され、製品ガ
ス１１が得られるように成っている。The outline of the equipment for carrying out the method of the present invention as described above will be explained with reference to the attached drawings. After the oxygen blast furnace gas 1 obtained from the top of the oxygen blast furnace 10 is removed by the coarse confectionery machine 2, a part of it is combusted. Oxygen and the like are suitably added and combusted in the vessel 3 to raise the temperature and then supplied to the shaft portion of the oxygen blast furnace 10 to preheat the raw material charged into the oxygen blast furnace 10. The remainder of the oxygen blast furnace gas 1 discharged from the oxygen blast furnace 10 and crushed into dust is sequentially supplied to a de-S mechanism 5 and a de-CO mechanism 6 via a pressure-feeding mechanism 4, and the de-CO mechanism 6 is a pressure increasing mechanism such as a compressor. 7 and a reaction tower 8 via an H2 source introduction device 16. The reaction tower 8 is connected to an impurity remover 15 via a cooling mechanism 9, so that a product gas 11 can be obtained.
なお前記した脱ＣＯ機構６は部分燃焼器１２にも接続さ
れ、酸素の如きを添加して部分燃焼せしめたものは炉頂
ガス発電機１３において電力を得しめ、しかも前記部分
燃焼器１２において通常の高炉ガス（８００Ｋｃａｊ２
／Ｎｏ？）レベルまでカロリー低下されたガスは前記炉
頂ガス発電機１３から既存の通常高炉ガス利用ライン１
４に供給されるように構成しである。The above-mentioned CO removal mechanism 6 is also connected to a partial combustor 12, and the partially combusted material by adding oxygen or the like generates electric power in the furnace top gas generator 13. blast furnace gas (800Kcaj2
/No? ) The gas whose calorie has been reduced to the level of
4.
（実施例）
前記したような設備を利用して具体的に操業した結果に
ついて説明すると、出銑量５ＱＯＯｔ／ｄａｙの高炉１
０に鉱石およびコークスを装入し、羽口から９５％程度
の純度をもった酸素ガス６８８０ （Ｈ’ｊｒｒｒ／ｈ
ｒと微粉炭６２５００ ｋｇ／ｈｒを吹込み、又炉頂か
らの高炉ガスを燃焼器３で空気を吹込みながら燃焼し約
１０００℃とされたものをシャフト部に吹込んで装入原
料を予熱しながら操業した。即ちこのときの高炉ガスの
組成はｃ。(Example) To explain the results of a concrete operation using the above-mentioned equipment, a blast furnace 1 with an iron output of 5QOOt/day
Oxygen gas with a purity of about 95% (6880 H'jrrr/h) was charged from the tuyeres.
62,500 kg/hr of pulverized coal and 62,500 kg/hr of pulverized coal were blown into the furnace, and the blast furnace gas from the top of the furnace was combusted in the combustor 3 while blowing air, and the resulting mixture was brought to about 1000°C and then blown into the shaft to preheat the charging material. It was operated while That is, the composition of the blast furnace gas at this time is c.
が４８．５％、ＣＯ，が３６．８％であって、１７４０
Ｋｃａｊ！／Ｎｎｆのものである。is 48.5%, CO is 36.8%, and 1740
Kcaj! /Nnf.
上記高炉ガスの燃焼器３に送られた以外のもの１０００
０ Ｎｒｒｒ／ｈｒは脱ＣＯおよび脱Ｓ処理されてから
Ｈ２源導入装置１６からＨ２ガス３８０ＯＮｒｒｒ／ｈ
ｒ導入し、Ｈｘ ／Ｃｏ比を３．５に調整し、これを昇
圧機構７で２５ｋｇ／ａｊ程度に昇圧して反応塔８に送
り込んだ。Items other than those sent to the blast furnace gas combustor 3 1000
0 Nrrr/hr is H2 gas 380ONrrr/h from the H2 source introducing device 16 after CO and S removal processing.
The Hx /Co ratio was adjusted to 3.5, the pressure was increased to about 25 kg/aj by the pressure increasing mechanism 7, and the pressure was increased to the reaction tower 8.
反応塔８においては２３ｋｇ／ｃｄ、３８０℃でＮｉ触
媒を用い反応処理され、４９０℃の反応塔出口ガスは冷
却器９において４０℃に冷却されてから不純分除去器１
５で、ＣＯ！ 、Ｎｔ 、Ｈｚ 、Ｇ Ｏなどの不純分
を吸着法により除去して１０５００ＫｃａｌｌＮｒｄの
熱量を有する製品燃料ガスを得た。In the reaction tower 8, reaction treatment is carried out using a Ni catalyst at 23 kg/cd and 380°C, and the reaction tower outlet gas at 490°C is cooled to 40°C in the cooler 9, and then sent to the impurity remover 1.
At 5, CO! , Nt , Hz , and G 2 O were removed by adsorption to obtain a product fuel gas having a calorific value of 10,500 KcallNrd.
なおこの場合において、昇圧機構７に入るガスに対し、
４５５０ Ｋｃａｊ！／Ｎｎｆのコークス炉ガス５００
０ Ｎｒｒｆ／ｈｒ及び水蒸気２３００ｋｇ／Ｈの添加
した場合には、得られる製品ガスの熱量は１１０８０Ｋ
ｃａｌ／Ｎｒｒｒとなり、又その量は３５８０ Ｎｒｒ
ｒ／ｈｒとなった。製品ガスの組成は、ＣＨ４８２，５
％、ＣａＨ２１３，５％、Ｃ３Ｈ１１２，５％、Ｃ４Ｈ
Ｉ０１．０％、Ｈｚｏ、５％であった。In this case, for the gas entering the pressure boosting mechanism 7,
4550 Kcaj! /Nnf coke oven gas 500
When adding 0 Nrrf/hr and water vapor of 2300 kg/H, the calorific value of the product gas obtained is 11080 K.
cal/Nrrr, and the amount is 3580 Nrr
It became r/hr. The composition of the product gas is CH482,5
%, CaH213.5%, C3H112.5%, C4H
I01.0%, Hzo, 5%.
又前記酸素高炉ガス１３２１００Ｎｒｒｆ／ｈｒを部分
燃焼器１２で０２を１４９００ Ｎｒｒｒ／ｈｒの割合
で添加し部分燃焼させてから炉頂ガス発電機１３で発電
させることにより１４３００ Ｋｗ／ｈｒの電力が得ら
れ、しかも８００ Ｋｃａｌ／Ｎｒｒｒ程度とされた普
通高炉ガスレベルのガスを３５４００ＯＮＩＴｒ／ｈｒ
得ることができ、このガスは既設の高炉ガス設備に混入
して使用できた。In addition, 132,100 Nrrf/hr of the oxygen blast furnace gas is added to the oxygen blast furnace gas at a rate of 14,900 Nrrf/hr in the partial combustor 12 and partially combusted, and then the furnace top gas generator 13 generates electricity, thereby generating 14,300 Kw/hr of electric power. Moreover, the gas at the level of normal blast furnace gas, which is about 800 Kcal/Nrrr, is 35400ONITr/hr.
This gas could be used by mixing it into the existing blast furnace gas equipment.
「発明の効果」
以上説明したような本発明によるときは酸素高炉から発
生するガスを用いて代替天然ガスを得しめ、これを燃料
ガスとして各種の用途に利用し得るものであって、酸素
高炉を燃料ガス製造目的にも利用したものと言うべきで
あって、有利な酸素高炉操業をなし得ることは当然であ
り、工業的にその効果の大きい発明である。"Effects of the Invention" According to the present invention as explained above, gas generated from an oxygen blast furnace can be used to obtain alternative natural gas, and this can be used as a fuel gas for various purposes. It should be said that this invention is also used for the purpose of producing fuel gas, and it is natural that an advantageous oxygen blast furnace operation can be achieved, and this invention is industrially highly effective.
図面は本発明の技術的内容を示すものであって、本発明
方法を実施する設備の概要を示した説明図である。
然してこの図面において、■は酸素高炉ガス、２は粗菓
塵機、３は燃焼機、４は圧送機構、５は脱Ｓ機構、６は
脱ＣＯ機構、７は昇圧機構、８は反応塔、９は冷却器、
ｌＯは酸素高炉、１１は製品ガス、１２部分燃焼器、１
３は炉頂ガス発電機、１４は通常高炉ガス利用ライン、
１５は不純分除去機構、１６はＨ２源導入機構を示すも
のである。The drawings show the technical content of the present invention, and are explanatory diagrams showing an outline of equipment for implementing the method of the present invention. However, in this drawing, ■ is oxygen blast furnace gas, 2 is a coarse powder, 3 is a combustion machine, 4 is a pressure feeding mechanism, 5 is a de-S mechanism, 6 is a de-CO mechanism, 7 is a pressure boosting mechanism, 8 is a reaction tower, 9 is a cooler;
1O is the oxygen blast furnace, 11 is the product gas, 12 is the partial combustor, 1
3 is a furnace top gas generator, 14 is a normal blast furnace gas utilization line,
15 is an impurity removal mechanism, and 16 is an H2 source introduction mechanism.
Claims (2)
処理し、次いでＨ＿２／ＣＯ比を調整したものを反応塔
に送って反応せしめ、不純分を除去して代替天然ガスを
得ることを特徴とする酸素高炉ガスの利用方法。(1) CO and S removal after rough dust collection of oxygen blast furnace gas
1. A method of utilizing oxygen blast furnace gas, which comprises treating the gas, and then sending the gas with an adjusted H_2/CO ratio to a reaction tower for reaction to remove impurities and obtain alternative natural gas.
を添加したものを反応塔に送って反応させる特許請求の
範囲第１項に記載した酸素高炉ガスの利用方法。(2) A method for utilizing oxygen blast furnace gas as set forth in claim 1, in which the H_2/CO ratio is adjusted and coke oven gas is added and sent to a reaction tower for reaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62001851A JPS63171804A (en) | 1987-01-09 | 1987-01-09 | Utilization of oxygen blast furnace gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62001851A JPS63171804A (en) | 1987-01-09 | 1987-01-09 | Utilization of oxygen blast furnace gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63171804A true JPS63171804A (en) | 1988-07-15 |
Family
ID=11513052
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62001851A Pending JPS63171804A (en) | 1987-01-09 | 1987-01-09 | Utilization of oxygen blast furnace gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63171804A (en) |
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|---|---|---|---|---|
| WO2021106579A1 (en) * | 2019-11-29 | 2021-06-03 | Ｊｆｅスチール株式会社 | Method for operating blast furnace, and facility equipped with blast furnace |
| WO2021106578A1 (en) * | 2019-11-25 | 2021-06-03 | Ｊｆｅスチール株式会社 | Blast furnace operation method and blast furnace ancillary equipment |
| WO2021215059A1 (en) * | 2020-04-24 | 2021-10-28 | Ｊｆｅスチール株式会社 | Blast furnace operation method and auxiliary facility for blast furnace |
| WO2023162344A1 (en) * | 2022-02-24 | 2023-08-31 | Ｊｆｅスチール株式会社 | Method for operating blast furnace, method for producing hot metal, and auxiliary facility for blast furnace |
-
1987
- 1987-01-09 JP JP62001851A patent/JPS63171804A/en active Pending
Cited By (8)
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|---|---|---|---|---|
| WO2021106578A1 (en) * | 2019-11-25 | 2021-06-03 | Ｊｆｅスチール株式会社 | Blast furnace operation method and blast furnace ancillary equipment |
| JPWO2021106578A1 (en) * | 2019-11-25 | 2021-12-02 | Ｊｆｅスチール株式会社 | Blast furnace operation method and blast furnace ancillary equipment |
| TWI775216B (en) * | 2019-11-25 | 2022-08-21 | 日商杰富意鋼鐵股份有限公司 | Blast furnace operation method and blast furnace accessory equipment |
| WO2021106579A1 (en) * | 2019-11-29 | 2021-06-03 | Ｊｆｅスチール株式会社 | Method for operating blast furnace, and facility equipped with blast furnace |
| JPWO2021106579A1 (en) * | 2019-11-29 | 2021-12-02 | Ｊｆｅスチール株式会社 | Blast furnace operation method and blast furnace ancillary equipment |
| WO2021215059A1 (en) * | 2020-04-24 | 2021-10-28 | Ｊｆｅスチール株式会社 | Blast furnace operation method and auxiliary facility for blast furnace |
| JP7028367B1 (en) * | 2020-04-24 | 2022-03-02 | Ｊｆｅスチール株式会社 | Blast furnace operation method and blast furnace ancillary equipment |
| WO2023162344A1 (en) * | 2022-02-24 | 2023-08-31 | Ｊｆｅスチール株式会社 | Method for operating blast furnace, method for producing hot metal, and auxiliary facility for blast furnace |
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