JPH0138843B2 - - Google Patents
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- Publication number
- JPH0138843B2 JPH0138843B2 JP50153686A JP50153686A JPH0138843B2 JP H0138843 B2 JPH0138843 B2 JP H0138843B2 JP 50153686 A JP50153686 A JP 50153686A JP 50153686 A JP50153686 A JP 50153686A JP H0138843 B2 JPH0138843 B2 JP H0138843B2
- Authority
- JP
- Japan
- Prior art keywords
- carbon
- converter
- fuel
- amount
- charge
- 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
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 63
- 229910052799 carbon Inorganic materials 0.000 description 63
- 239000000446 fuel Substances 0.000 description 56
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 46
- 239000007788 liquid Substances 0.000 description 40
- 239000004449 solid propellant Substances 0.000 description 34
- 229910000831 Steel Inorganic materials 0.000 description 26
- 239000010959 steel Substances 0.000 description 26
- 238000004519 manufacturing process Methods 0.000 description 23
- 239000007787 solid Substances 0.000 description 23
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 19
- 239000007769 metal material Substances 0.000 description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 15
- 229910052760 oxygen Inorganic materials 0.000 description 15
- 239000001301 oxygen Substances 0.000 description 15
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 14
- 239000000463 material Substances 0.000 description 13
- 238000007254 oxidation reaction Methods 0.000 description 12
- 238000007664 blowing Methods 0.000 description 11
- 230000003647 oxidation Effects 0.000 description 11
- 229910052751 metal Inorganic materials 0.000 description 10
- 239000002184 metal Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 10
- 239000007800 oxidant agent Substances 0.000 description 10
- 230000001590 oxidative effect Effects 0.000 description 10
- 238000010438 heat treatment Methods 0.000 description 9
- 239000007791 liquid phase Substances 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 238000009628 steelmaking Methods 0.000 description 9
- 229910052742 iron Inorganic materials 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 239000003345 natural gas Substances 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 5
- 239000003830 anthracite Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000002844 melting Methods 0.000 description 4
- 230000008018 melting Effects 0.000 description 4
- 235000013980 iron oxide Nutrition 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- 239000010687 lubricating oil Substances 0.000 description 2
- 239000010814 metallic waste Substances 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910001018 Cast iron Inorganic materials 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 238000012552 review Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910000859 α-Fe Inorganic materials 0.000 description 1
Landscapes
- Carbon Steel Or Casting Steel Manufacturing (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Cyclones (AREA)
Description
請求の範囲
１ Fe含有固体金属材を原料とする塩基性酸素
吹転炉製鋼法であつて、炭素含有固体燃料、炭素
含有液体燃料、および炭素含有気体燃料を燃焼さ
せることによつて該Fe含有固体金属材を予熱お
よび溶解しながら、転炉に装入された該Fe含有
固体金属材と該炭素含有固体燃料に酸化体を流通
させる塩基性酸素吹転炉製鋼法において、該炭素
含有液体燃料として密度が800〜1100Kg／m3の炭
素含有液体燃料を用い、該Fe含有固体金属材お
よび該炭素含有固体燃料を予熱する前に、転炉に
装入された該Fe含有固体金属材および該炭素含
有固体燃料の表面上に該炭素含有液体燃料の膜を
形成するように該炭素含有液体燃料を転炉に供給
することを特徴とする塩基性酸素吹転炉製鋼法。Claim 1 A basic oxygen blown converter steel manufacturing method using a Fe-containing solid metal material as a raw material, wherein the Fe-containing solid fuel is produced by burning a carbon-containing solid fuel, a carbon-containing liquid fuel, and a carbon-containing gaseous fuel. In a basic oxygen-blown converter steel manufacturing method in which an oxidant is passed through the Fe-containing solid metal material charged into a converter and the carbon-containing solid fuel while preheating and melting the solid metal material, the carbon-containing liquid fuel Using a carbon-containing liquid fuel with a density of 800 to 1100 Kg/ m3 , before preheating the Fe-containing solid metal material and the carbon-containing solid fuel, the Fe-containing solid metal material and the A basic oxygen-blown converter steel manufacturing method comprising supplying the carbon-containing liquid fuel to a converter so as to form a film of the carbon-containing liquid fuel on the surface of the carbon-containing solid fuel.
２ 前記炭素含有液体燃料の量を前記炭素含有固
体燃料の量の20〜40％とすることを特徴とする請
求の範囲第１項記載の塩基性酸素吹転炉製鋼法。2. The basic oxygen blown converter steel manufacturing method according to claim 1, wherein the amount of the carbon-containing liquid fuel is 20 to 40% of the amount of the carbon-containing solid fuel.
技術分野
本発明は冶金技術に関し、更に詳しくは製鋼法
に関し、特に塩基性酸素吹転炉における製鋼法に
関する。TECHNICAL FIELD The present invention relates to metallurgy, and more particularly to a steel manufacturing method, and in particular to a steel manufacturing method in a basic oxygen blown converter furnace.
背景技術
今日、治金技術における最も重要な課題の一つ
は、全世界的に量の増え続けているスクラツプの
再溶解である。汎用鋼の基本的な製造方法は酸素
製鋼法である。塩基性酸素吹転炉における古典的
な製鋼法は30％までのスクラツプを使える。BACKGROUND ART Today, one of the most important challenges in metallurgy technology is the remelting of scrap, which continues to increase in volume worldwide. The basic manufacturing method for general-purpose steel is the oxygen steelmaking method. Classical steelmaking processes in basic oxygen blown converters can use up to 30% scrap.
現在、工業先進国では、100％スクラツプチヤ
ージの酸素製鋼法が多数開発されつつある。これ
までに行なわれた酸素吹転炉の実操業の経験から
は、従来法にくらべて、転炉の生産速度が極めて
低く50％止まりであり、転炉ライニングの耐損耗
性と溶鋼の収量も極めて低いことがわかつてい
る。 Currently, in industrially advanced countries, many 100% scrap-charge oxygen steel manufacturing processes are being developed. From the experience of actual operation of oxygen-blown converters conducted so far, compared to conventional methods, the production rate of converters is extremely low at only 50%, and the wear resistance of the converter lining and the yield of molten steel are also poor. known to be extremely low.
塩基性酸素吹転炉における従来公知の製鋼法は
Fe含有固体金属材、特に金属スクラツプを装入
原料とする（参考文献：典型的な集録として
“Reviews of Science and Technology”、シリ
ーズ“Iron and Steelmaking Practice”，v.14，
1983，VINITI出版社（モスクワ）、pp.73〜74、
ロシア語）。この方法では、炭素含有固体燃料、
炭素含有液体燃料、および炭素含有気体燃料を燃
焼させることによつてFe含有固体金属材を加熱
および溶解しながら、転炉に装入されたFe含有
固体金属材に酸化体を流通させる。固体金属を含
有する装入物は、炭化水素を含有する液体または
気体の燃料が下記の発熱反応に従つて燃焼すると
きに発生する熱によつて、酸化体のジエツト流が
装入物に衝突する位置に液相が出現するまで予熱
される。 The conventionally known steelmaking method in a basic oxygen blowing furnace is
Fe-containing solid metal material, especially metal scrap, is used as a charging material (References: Typical collections include “Reviews of Science and Technology”, series “Iron and Steelmaking Practice”, v.14,
1983, VINITI Publishing House (Moscow), pp.73-74,
Russian). In this method, carbon-containing solid fuel,
While heating and melting the Fe-containing solid metal material by burning the carbon-containing liquid fuel and the carbon-containing gaseous fuel, the oxidant is passed through the Fe-containing solid metal material charged into the converter. The solid metal-containing charge is exposed to the heat generated when the hydrocarbon-containing liquid or gaseous fuel burns in accordance with the exothermic reaction described below. It is preheated until a liquid phase appears at the location.
CnHm＋2n＋ｍ／４O2＝nCO2＋ｍ／２H2O
酸化性雰囲気下では、金属装入物の鉄と転炉ラ
イニングの炭素含有成分は、下記反応によつて酸
化される。 CnHm+2n+m/4O 2 =nCO 2 +m/2H 2 O Under an oxidizing atmosphere, the iron of the metal charge and the carbon-containing components of the converter lining are oxidized by the following reaction.
〔Fe〕＋１／２｛O2｝＝（FeO）
Ｃ＋｛O2｝＝｛CO2｝
燃焼反応の本質的生成物は酸化鉄と共にCO2と
H2Oである。液相が出現したら、予め微粉状に
壊変された炭素含有固体燃料（コークス、石炭）
が転炉内に供給される。同時に、炭素含有液体燃
料および炭素含有気体燃料の供給比率を使用する
酸化体の量の10〜12％にまで徐々に減少させ、そ
れによつてランスおよびそれに隣接するライニン
グを保護する。 [Fe] + 1/2 {O 2 } = (FeO) C + {O 2 } = {CO 2 } The essential products of the combustion reaction are CO 2 and iron oxide.
It is H2O . When the liquid phase appears, the carbon-containing solid fuel (coke, coal) that has been disintegrated into fine powder
is fed into the converter. At the same time, the feed ratio of carbon-containing liquid fuel and carbon-containing gaseous fuel is gradually reduced to 10-12% of the amount of oxidant used, thereby protecting the lance and the lining adjacent to it.
次に、下記反応で発生する熱によつて更に予熱
し、溶解し、そして最終的に所定温度にまで加熱
する。 Next, the material is further preheated by the heat generated in the reaction described below, melted, and finally heated to a predetermined temperature.
〔Ｃ〕＋１／２｛O2｝＝｛CO｝ 併行して、硫黄と燐が溶湯から除去される。 [C]+1/2{O 2 }={CO} At the same time, sulfur and phosphorus are removed from the molten metal.
溶湯の化学組成と温度が所定値になつたら、溶
湯をレードル内に出湯し、そこで脱酸および合金
添加、そして必要に応じた炉外処理を行なう。 When the chemical composition and temperature of the molten metal reach predetermined values, the molten metal is tapped into a ladle, where it is deoxidized, alloyed, and treated outside the furnace as necessary.
微粉状炭素含有燃料を供給する前の、初期加熱
中に転炉の円筒部分は炉口および炉底が著しく損
耗するのが観察される。鉄の酸化によつて生ずる
酸化物が炉底に降下し、耐火物中のCaOおよび
MgOと相互作用して低融点のカルシウムフエラ
イトおよびマグネシウムフエライトが形成され
る。 During the initial heating, before feeding the pulverized carbon-containing fuel, the cylindrical part of the converter is observed to be severely worn at the mouth and bottom. Oxides produced by iron oxidation fall to the bottom of the furnace, causing CaO and
It interacts with MgO to form low melting point calcium and magnesium ferrites.
転炉の作用領域の耐火物ライニングの炭素の酸
化によつて、上記の反応が起こる位置に空洞が生
じ、その中に溶解工程中に酸化されたスラグが充
填される。結局これがライニングを破損し、転炉
の作用領域のライニングの早期損耗の主因とな
る。 The oxidation of the carbon in the refractory lining in the working area of the converter creates cavities at the location where the above reaction takes place, into which the oxidized slag is filled during the melting process. This eventually damages the lining and is the main cause of premature wear of the lining in the working area of the converter.
その上、Fe含有固体金属材の酸化は溶鋼の収
量を低下させる。この場合、金属装入物の「見
掛」加熱効果が観察される。すなわち、金属装入
物が発熱反応である鉄の酸化によつて加熱され、
排出ガスの温度上昇と熱含量の上昇とによつて熱
利用係数が低下する。鉄の還元過程は微粉状の炭
素含有固体燃料の供給中に下記反応によつて起こ
る。 Moreover, oxidation of Fe-containing solid metal materials reduces the yield of molten steel. In this case, an "apparent" heating effect of the metal charge is observed. That is, the metal charge is heated by the oxidation of iron, which is an exothermic reaction,
The heat utilization coefficient decreases due to the increased temperature and heat content of the exhaust gas. The iron reduction process occurs during the supply of finely powdered carbon-containing solid fuel through the following reaction.
（FeO）＋Ｃ＝〔Fe〕＋｛CO｝
この反応は吸熱そして溶湯の冷却を伴つて進行
する。その結果、燃料消費量が増加し、転炉の生
産速度が低下する。 (FeO) + C = [Fe] + {CO} This reaction progresses with endotherm and cooling of the molten metal. As a result, fuel consumption increases and the production rate of the converter decreases.
微粉状炭素含有燃料が必要なので、その準備と
運搬のため製鋼コストが上昇する。更に、公知方
法では転炉内でのスクラツプ予熱の段階で鉄の損
失がかなり生ずる。 The need for pulverized carbon-containing fuel increases steelmaking costs due to its preparation and transportation. Furthermore, in the known process, considerable iron losses occur during the scrap preheating stage in the converter.
塩基性酸素吹転炉におけるもう一つの公知の製
鋼法は塊状炭素含有材（コークスまたは石炭）を
用いる方法であつて（参考文献：特許出願第
2729983号、Int.C1.C21C ５／28、ドイツ連邦共
和国、公開1981.2.12.）、転炉に装入されたFe含有
材と炭素含有固体燃料とに酸化体を流通させなが
ら、固体、液体、および気体の炭素含有燃料を燃
焼させることによつて、金属Fe含有材を加熱し
て溶解する。 Another known method for making steel in basic oxygen blown converters is using bulk carbon-containing material (coke or coal) (Reference: Patent Application No.
No. 2729983, Int.C1.C21C 5/28, Federal Republic of Germany, Published on February 12, 1981), solid and liquid , and a gaseous carbon-containing fuel to heat and melt the metallic Fe-containing material.
Fe含有材と一緒に装入される固体燃料はスク
ラツプの酸化を低減して酸化鉄の形成を制限す
る。 Solid fuel charged with Fe-containing material reduces oxidation of the scrap and limits the formation of iron oxides.
酸化鉄の量が減少することによつて、転炉ライ
ニングにとつて好ましい操業条件となるためライ
ニングの損耗が低減する。しかし、転炉内の気体
相の酸化ポテンシヤルが高まり、それによつて転
炉ライニングの一部を成す炭素の酸化反応の発生
が促進されて損耗が速まる。 The reduced amount of iron oxide provides favorable operating conditions for the converter lining and reduces wear on the lining. However, the oxidation potential of the gas phase within the converter is increased, which accelerates the occurrence of oxidation reactions in the carbon forming part of the converter lining, leading to faster wear and tear.
炉修１回当りの溶解チヤージ数で表した転炉ラ
イニングの寿命は1.5〜２倍短縮し、そのため転
炉の生産速度は結局大巾に低下する。 The life of the converter lining in terms of the number of melt charges per furnace repair is reduced by a factor of 1.5 to 2, and the production rate of the converter is therefore significantly reduced.
発明の開示
本発明の基本的かつ本質的な目的は、炭素含有
固体燃料の着火前に転炉の作用領域において気体
相の酸化ポテンシヤルを低下させることによつ
て、転炉ライニングの寿命を延長し、それによつ
て転炉の生産速度を高めることができる、Fe含
有固体金属材を原料とする塩基性酸素吹転炉製鋼
法を提供することである。DISCLOSURE OF THE INVENTION The basic and essential object of the present invention is to extend the life of the converter lining by reducing the oxidation potential of the gas phase in the working region of the converter prior to ignition of the carbon-containing solid fuel. An object of the present invention is to provide a basic oxygen-blown converter steel manufacturing method using an Fe-containing solid metal material as a raw material, thereby increasing the production rate of the converter.
上記の目的は、Fe含有固体金属材を原料とす
る塩基性酸素吹転炉製鋼法であつて、炭素含有固
体燃料、炭素含有液体燃料、および炭素含有気体
燃料を燃焼させることによつて該Fe含有固体金
属材を予熱および溶解しながら、転炉に装入され
た該Fe含有固体金属材と該炭素含有固体燃料に
酸化体を流通させる塩基性酸素吹転炉製鋼法にお
いて、該炭素含有液体燃料として密度が800〜
1100Kg／m3の炭素含有液体燃料を用い、該Fe含
有固体金属材および該炭素含有固体燃料を予熱す
る前に、転炉に装入された該Fe含有固体金属材
および該炭素含有固体燃料の表面上に該炭素含有
液体燃料の膜を形成するように該炭素含有液体燃
料を転炉に供給することを特徴とする塩基性酸素
吹転炉製鋼法によつて達成される。 The above object is a basic oxygen blown furnace steelmaking method using Fe-containing solid metal material as a raw material, and by burning carbon-containing solid fuel, carbon-containing liquid fuel, and carbon-containing gaseous fuel, In a basic oxygen-blown converter steel manufacturing method in which an oxidant is passed through the Fe-containing solid metal material and the carbon-containing solid fuel charged into a converter while preheating and melting the Fe-containing solid metal material, the carbon-containing liquid As a fuel, the density is 800~
Using 1100 kg/m 3 of carbon-containing liquid fuel, before preheating the Fe-containing solid metal material and the carbon-containing solid fuel, the Fe-containing solid metal material and the carbon-containing solid fuel charged into the converter were heated. This is achieved by a basic oxygen-blown converter steelmaking process characterized in that the carbon-containing liquid fuel is fed to a converter so as to form a film of the carbon-containing liquid fuel on the surface.
炭素含有液体燃料の量を炭素含有固体燃料の量
の20〜40％とすることが望ましい。 It is desirable that the amount of carbon-containing liquid fuel be 20 to 40% of the amount of carbon-containing solid fuel.
転炉に装入され且つFe含有固体金属材と炭素
含有固体燃料を含有する装入物の表面上に形成さ
れた炭素含有液体燃料の膜は、加熱時に、炭素含
有固体燃料がまだ十分に予熱されないために燃焼
炎の酸化ポテンシヤルが高い最も有害な初期に、
装入物を気体相から隔離する。これによつて、
Fe含有固体金属材の過剰酸化と転炉ライニング
の焼損とを防止し、ライニングの寿命が1.5〜２
倍に増加する。 The carbon-containing liquid fuel film formed on the surface of the charge charged to the converter and containing the Fe-containing solid metal material and the carbon-containing solid fuel is such that the carbon-containing solid fuel is still sufficiently preheated during heating. At the beginning, when the oxidation potential of the combustion flame is high, the most harmful
Separate the charge from the gas phase. By this,
Prevents excessive oxidation of Fe-containing solid metal materials and burnout of the converter lining, increasing the lifespan of the lining from 1.5 to 2.
increase twice.
上記の隔離膜によつて、固体燃料は酸化が軽微
になり、予熱されて液相に若干の遅れで、すなわ
ち液相が既に出現しているときに、その中に溶け
入ることができる。更に、固体燃料に含有されて
いる炭素は、鋳鉄に含有されている炭素と同様の
仕方で酸化される、すなわち燃料利用係数が高
い。また、固体燃料の表面上に形成された液体燃
料の膜は固体燃料の着火に好ましい条件を提供す
るので、熱供給時間が短縮されて転炉の生産速度
が高める。 Owing to the above-mentioned separator membrane, the solid fuel is only lightly oxidized and can be preheated and dissolved into the liquid phase with a slight delay, ie when the liquid phase has already appeared. Furthermore, the carbon contained in solid fuels is oxidized in a similar manner to the carbon contained in cast iron, ie the fuel utilization factor is high. In addition, the liquid fuel film formed on the surface of the solid fuel provides favorable conditions for ignition of the solid fuel, thereby shortening the heat supply time and increasing the production rate of the converter.
発明を実施するための最良の態様
Fe含有固体金属材を原料とする塩基性酸素吹
転炉製鋼法は以下のように実施される。BEST MODE FOR CARRYING OUT THE INVENTION A basic oxygen-blown converter steel manufacturing method using Fe-containing solid metal material as a raw material is carried out as follows.
Fe含有固体金属材と石炭のような炭素含有固
体燃料とを転炉内に装入する。次に炭素含有固体
燃料を転炉に供給する。この液体燃料としては、
密度が800〜1100Kg／m3の従来公知の液体燃料が
使える。このような燃料としては、たとえば、可
燃成分が平均組成＝炭素86.7％、水素12.6％、密
度950Kg／m3の重油；密度900Kg／m3の原油；可燃
成分が平均組成＝炭素90％、水素７％、密度1100
Kg／m3のコールタール樹脂；可燃成分が平均組成
＝炭素86.0％、水素11％、密度920Kg／m3の廃潤
滑油；可燃成分が平均組成＝炭素86.5％、水素
11.0％、密度900Kg／m3のソーラー油軽油；可燃
成分が平均組成＝炭素85.8％、水素13.95％、密
度800Kg／m3のリグロイン；可燃成分が平均組成
＝炭素86.0％、水素13.7％、密度880Kg／m3のケ
ロシン等がある。微粉炭を上記のいずれかの燃料
と、または可燃成分が平均組成＝炭素85％、水素
5.67％、密度750Kg／m3のガソリンと混合して用
いてもよい。 A Fe-containing solid metal material and a carbon-containing solid fuel such as coal are charged into a converter. Next, the carbon-containing solid fuel is fed to the converter. This liquid fuel is
Conventionally known liquid fuels with a density of 800 to 1100 Kg/m 3 can be used. Such fuels include, for example, heavy oil with an average composition of combustible components = 86.7% carbon and 12.6% hydrogen, and a density of 950 kg/ m3 ; crude oil with a density of 900 kg/ m3 ; average composition of combustible components = 90% carbon, hydrogen 7%, density 1100
Coal tar resin with Kg/ m3 ; average composition of combustible components = 86.0% carbon, 11% hydrogen; waste lubricating oil with density 920Kg/ m3 ; average composition of combustible components = 86.5% carbon, hydrogen
Solar oil diesel oil with a density of 11.0% and 900Kg/ m3 ; average composition of combustible components = carbon 85.8%, hydrogen 13.95%, density 800Kg/ m3 ; average composition of combustible components = carbon 86.0%, hydrogen 13.7%, density There is 880Kg/m 3 of kerosene, etc. Pulverized coal with any of the above fuels or combustible components with average composition = 85% carbon, hydrogen
5.67%, density 750Kg/ m3 .
先に装入したFe含有材および炭素含有固体燃
料の上方から、これらの表面上に膜を形成するよ
うに液体燃料を転炉内に供給する。この供給を行
なうには、転炉装入物の表面上に液体燃料を均一
に展延できる従来公知の方法および装置（たとえ
ば噴霧などによる）を用いる。その結果、装入物
は濡らされ、その上に炭素含有液体燃料の膜が形
成される。密度が800Kg／m3未満の液体燃料は転
炉装入物の表面から非常に急速に、実際上瞬間的
に、蒸発してしまうので、酸化体から装入物を隔
離することが、特に液相が出現する前の予熱初期
における隔離ができない。 Liquid fuel is supplied into the converter from above the previously charged Fe-containing material and carbon-containing solid fuel so as to form a film on these surfaces. This supply is accomplished using conventionally known methods and devices capable of uniformly spreading liquid fuel over the surface of the converter charge (eg, by spraying, etc.). As a result, the charge is wetted and a film of carbon-containing liquid fuel forms thereon. Since liquid fuels with a density less than 800 Kg/ m3 evaporate from the surface of the converter charge very rapidly, practically instantaneously, isolating the charge from the oxidants is particularly important for liquid fuels. Isolation in the early stage of preheating before the phase appears is not possible.
密度が1100Kg／m3を超える液体燃料は粘性が大
きいため装入物の表面上に連続的な膜を形成でき
ない。更に、高密度の液体燃料を従来公知の方法
および装置によつて転炉装入物表面上に均一に展
延させることはかなり困難である。 Liquid fuels with a density exceeding 1100 Kg/m 3 cannot form a continuous film on the surface of the charge due to their high viscosity. Furthermore, it is quite difficult to spread dense liquid fuel uniformly over the converter charge surface by methods and apparatus known in the art.
転炉に装入されたFe含有材および固体燃料の
全表面を覆うために、炭素含有液体燃料の量は炭
素含有固体燃料の量の20〜40％とする。液体燃料
の量はFe含有材の嵩密度に応じて選択する。す
なわち、嵩密度が低いほど、装入物の表面上に連
続した膜を形成するに必要な液体燃料の量は多く
なる。また、液体燃料の密度が高いほどその消費
量は多くなることに注目すべきである。 In order to cover the entire surface of the Fe-containing material and solid fuel charged into the converter, the amount of carbon-containing liquid fuel is 20-40% of the amount of carbon-containing solid fuel. The amount of liquid fuel is selected depending on the bulk density of the Fe-containing material. That is, the lower the bulk density, the greater the amount of liquid fuel required to form a continuous film on the surface of the charge. It should also be noted that the higher the density of liquid fuel, the greater its consumption.
たとえば、Fe含有材の嵩密度が1000Kg／m3で
あれば、密度が950Kg／m3の液体燃料を固体燃料
の量の30％の量で使う。 For example, if the bulk density of the Fe-containing material is 1000 Kg/m 3 , liquid fuel with a density of 950 Kg/m 3 is used in an amount that is 30% of the amount of solid fuel.
次に酸化体を気体燃料と一緒に転炉に供給し始
める。酸化体としては酸素または酸素と窒素の混
合体を用いる。気体燃料は現実的には天然ガスで
ある。転炉への酸化体の供給はどのような吹込方
法によつてもよく、すなわち底吹、上吹、横吹、
組合せ吹込のいずれでもよい。組合せ吹込の場合
には、転炉ライニングの同軸ランス取付部分およ
びランス自体を保護するために、気体または液体
の炭火水素を用いる。 The oxidant is then started to be fed to the converter along with the gaseous fuel. As the oxidant, oxygen or a mixture of oxygen and nitrogen is used. The gaseous fuel is actually natural gas. The supply of oxidant to the converter may be by any blowing method, i.e. bottom blowing, top blowing, side blowing,
Either combination blowing may be used. In the case of combined blowing, gaseous or liquid hydrocarbons are used to protect the coaxial lance attachment part of the converter lining and the lance itself.
転炉に供給された酸化体は液体燃料蒸気と反応
を開始する。転炉装入物の表面上の炭素含有液体
燃料の膜は、この瞬間から固体燃料の着火までの
間、Fe含有材を隔離してその酸化を防止する。 The oxidant supplied to the converter begins to react with the liquid fuel vapor. A film of carbon-containing liquid fuel on the surface of the converter charge isolates the Fe-containing material and prevents its oxidation from this moment until ignition of the solid fuel.
更に、転炉の作用領域における気体相の酸化ポ
テンシヤルが低下し、それによつて装入物予熱の
初期におけるFe含有材の過剰酸化およびライニ
ングの焼損が防止される。 Furthermore, the oxidation potential of the gas phase in the working region of the converter is reduced, which prevents overoxidation of the Fe-containing material and burnout of the lining during the early stages of charge preheating.
本発明が更に理解されるために、以下に1000Kg
塩基性酸素吹転炉における推奨される製鋼法の実
施例を説明する。 For a better understanding of the invention, below 1000Kg
An example of a recommended steel manufacturing method in a basic oxygen blowing furnace will be described.
実施例 １
組合せ吹転炉での製鋼を行なうための装入物と
して嵩密度ρ＝1000Kg／m3のスクラツプ1100Kg、
無煙炭70Kg、および20℃での密度が950Kg／m3の
重油21Kg（すなわち固体燃料の量の30％）を用い
た。炉口を通して転炉の固体装入物の上方からそ
の表面に、気体液体ジエツトアトマイザーによつ
て液体燃料を供給した。次に酸化体を底部および
上部のランスから供給し始めた。同時に、天然ガ
スを底部ランスから供給した。酸素の上吹量は１
m3／min.t、酸素の底吹量は2.25m3／min.tであつ
た。１チヤージ当りの気体燃料（天然ガス）の量
は９m3であつた。鋼中炭素量が0.1％になるまで
の時間は40分であつた。１チヤージ当りの燃料当
量は110.3Kgであつた。溶鋼の収量は999.6Kgであ
つた。加熱開始から13〜14分後の液相中のFeOの
比率は全量の15％であつた。転炉の生産速度は
1500Kg／ｈであつた。Example 1 1100 kg of scrap with bulk density ρ = 1000 Kg/m 3 was used as a charge for steel making in a combined blowing converter.
70 Kg of anthracite and 21 Kg of heavy oil with a density of 950 Kg/m 3 at 20° C. (ie 30% of the amount of solid fuel) were used. Liquid fuel was supplied from above the solid charge of the converter through the furnace mouth onto its surface by a gas-liquid jet atomizer. Oxidant was then started to be fed from the bottom and top lances. At the same time, natural gas was supplied through the bottom lance. The top blowing amount of oxygen is 1
m 3 /min.t, and the bottom flow rate of oxygen was 2.25 m 3 /min.t. The amount of gaseous fuel (natural gas) per charge was 9 m 3 . It took 40 minutes for the carbon content in the steel to reach 0.1%. The fuel equivalent per charge was 110.3 kg. The yield of molten steel was 999.6 kg. The proportion of FeO in the liquid phase 13 to 14 minutes after the start of heating was 15% of the total amount. The production rate of converter is
It was 1500Kg/h.
実施例 ２
装入物は、嵩密度ρ＝1300Kg／m3のスクラツプ
1100Kg、無煙炭80Kg、および75％の量のソーラー
油と25％の量のコールタール樹脂とを含有し密度
950Kg／m3の液体燃料16Kg（固体燃料の量の20％）
である。天然ガスの消費量は９m3であつた。鋼中
炭素量が0.1％になるまでの時間は42分であつた。
１チヤージ当りの燃料消費当量は113.1Kgであつ
た。溶鋼の収量は1002Kgであつた。転炉の生産速
度は1430Kg／ｈであつた。加熱開始から13〜14分
後の液相中のFeOの比率は16％の量であつた。Example 2 The charge was scrap with bulk density ρ = 1300Kg/m 3
1100Kg, anthracite 80Kg, and containing 75% amount of solar oil and 25% amount of coal tar resin
950Kg/ m3 liquid fuel 16Kg (20% of solid fuel amount)
It is. Natural gas consumption was 9m3 . It took 42 minutes for the carbon content in the steel to reach 0.1%.
The equivalent fuel consumption per charge was 113.1 kg. The yield of molten steel was 1002 kg. The production rate of the converter was 1430 Kg/h. The proportion of FeO in the liquid phase 13 to 14 minutes after the start of heating was 16%.
実施例 ３
装入物は、嵩密度ρ＝800Kg／m3のスクラツプ
1100Kg、無煙炭67.8Kg、および５％の量の微粉炭
と43.5％の量のリグロインと51.5％の量の廃潤滑
油とを含有し密度950Kg／m3の液体燃料27.2Kg
（固体燃料の量の40％）である。天然ガスの消費
量は９m3であつた。鋼中炭素量が0.1％になるま
での時間は41分であつた。１チヤージ当りの燃料
消費量は116.9Kgであつた。溶鋼の収量は997Kgで
あつた。転炉の生産速度は1460Kg／ｈ、加熱開始
から13〜14分後の液相中のFeOの比率は14％であ
つた。Example 3 The charge was scrap with a bulk density ρ = 800 Kg/m 3
1100 Kg, anthracite 67.8 Kg and 27.2 Kg liquid fuel containing 5% amount of pulverized coal, 43.5% amount of ligroin and 51.5% amount of waste lubricating oil and having a density of 950 Kg/m 3
(40% of the amount of solid fuel). Natural gas consumption was 9m3 . It took 41 minutes for the carbon content in the steel to reach 0.1%. Fuel consumption per charge was 116.9 kg. The yield of molten steel was 997Kg. The production rate of the converter was 1460 kg/h, and the ratio of FeO in the liquid phase 13 to 14 minutes after the start of heating was 14%.
実施例 ４
装入物は、嵩密度ρ＝1000Kg／m3のスクラツプ
1100Kg、無煙炭71Kg、および密度800Kg／m3のリ
グロイン21.3Kg（固体燃料の量の30％）である。
天然ガスの消費量は９m3であつた。鋼中炭素量が
0.1％になるまでの時間は41分であつた。燃料消
費当量は111.7Kgであつた。溶鋼の収量は998Kgで
あつた。転炉の生産速度は1460Kg／ｈであつた。
加熱開始から13〜14分後の液相中のFeOの比率は
16％の量であつた。Example 4 The charge is scrap with bulk density ρ=1000Kg/m 3
1100Kg, anthracite 71Kg and 21.3Kg of ligroin (30% of the amount of solid fuel) with a density of 800Kg/ m3 .
Natural gas consumption was 9m3 . Carbon content in steel
It took 41 minutes to reach 0.1%. The fuel consumption equivalent was 111.7Kg. The yield of molten steel was 998Kg. The production rate of the converter was 1460 Kg/h.
The proportion of FeO in the liquid phase 13-14 minutes after the start of heating is
The amount was 16%.
実施例 ５
装入物は、嵩密度ρ＝1000Kg／m3のスクラツプ
1100Kg、無煙炭72Kg、および12.4％の量の微粉炭
と43.8％の量のケロシンと33.8％の量の原油とを
含有し密度1100Kg／m3の液体燃料21.6Kg（固体燃
料の量の30％）である。天然ガスの消費量は９m3
であつた。Example 5 The charge is scrap with bulk density ρ=1000Kg/ m3
1100Kg, anthracite 72Kg and 21.6Kg of liquid fuel with a density of 1100Kg/ m3 containing 12.4% amount of pulverized coal, 43.8% amount of kerosene and 33.8% amount of crude oil (30% of the amount of solid fuel) It is. Natural gas consumption is 9m3
It was hot.
鋼中炭素量が0.1％になるまでの時間は42分で
あつた。燃料消費当量は113.1Kgであつた。溶鋼
の収量は1001Kgであつた。転炉の生産速度は1430
Kg／ｈであつた。加熱開始から13〜14分後の液相
中のFeOの比率は14％の量であつた。 It took 42 minutes for the carbon content in the steel to reach 0.1%. The fuel consumption equivalent was 113.1Kg. The yield of molten steel was 1001 kg. The production rate of converter is 1430
It was Kg/h. The proportion of FeO in the liquid phase 13 to 14 minutes after the start of heating was 14%.
産業上の利用可能性
本発明の塩基性酸素吹転炉製鋼法は、金属廃材
（スクラツプ、エンドクロツプ、鋳物工業や機械
工業の金属廃材）、高鉄量ペレツト、スポンジ鉄
のようなFe含有固体金属材を100％チヤージ原料
とする製鋼法に適用できる。Industrial Applicability The basic oxygen blowing furnace steelmaking method of the present invention can be applied to metal waste materials (scrap, end crops, metal waste materials from the foundry industry and machinery industry), high iron content pellets, and Fe-containing solid metals such as sponge iron. It can be applied to steel manufacturing methods that use 100% charged raw materials.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/US1985/000098 WO1985003586A1 (en) | 1984-02-03 | 1985-01-22 | Aircraft flight data recorder data acquisition system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63501880A JPS63501880A (en) | 1988-07-28 |
| JPH0138843B2 true JPH0138843B2 (en) | 1989-08-16 |
Family
ID=22188558
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP50538585A Granted JPS63502368A (en) | 1985-01-22 | 1985-12-09 | Circulating fluidized bed reactor and method for separating solids from flue gas |
| JP50153686A Granted JPS63501880A (en) | 1985-01-22 | 1985-12-17 | Basic oxygen blown converter steel manufacturing method |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP50538585A Granted JPS63502368A (en) | 1985-01-22 | 1985-12-09 | Circulating fluidized bed reactor and method for separating solids from flue gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (2) | JPS63502368A (en) |
-
1985
- 1985-12-09 JP JP50538585A patent/JPS63502368A/en active Granted
- 1985-12-17 JP JP50153686A patent/JPS63501880A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0325684B2 (en) | 1991-04-08 |
| JPS63502368A (en) | 1988-09-08 |
| JPS63501880A (en) | 1988-07-28 |
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