JPS6347307A - Smelting and reducing method - Google Patents
Smelting and reducing methodInfo
- Publication number
- JPS6347307A JPS6347307A JP18968886A JP18968886A JPS6347307A JP S6347307 A JPS6347307 A JP S6347307A JP 18968886 A JP18968886 A JP 18968886A JP 18968886 A JP18968886 A JP 18968886A JP S6347307 A JPS6347307 A JP S6347307A
- Authority
- JP
- Japan
- Prior art keywords
- furnace
- exhaust gas
- preheating
- smelting
- reducing
- 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 34
- 238000000034 method Methods 0.000 title claims description 17
- 239000007789 gas Substances 0.000 claims abstract description 69
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910052742 iron Inorganic materials 0.000 claims abstract description 25
- 239000003245 coal Substances 0.000 claims abstract description 17
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000001301 oxygen Substances 0.000 claims abstract description 9
- 230000003647 oxidation Effects 0.000 claims abstract description 4
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 4
- 239000002994 raw material Substances 0.000 claims abstract description 4
- 238000002844 melting Methods 0.000 claims description 10
- 230000008018 melting Effects 0.000 claims description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 2
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract description 5
- 235000011941 Tilia x europaea Nutrition 0.000 abstract description 5
- 239000004571 lime Substances 0.000 abstract description 5
- 239000003638 chemical reducing agent Substances 0.000 abstract description 4
- 239000000446 fuel Substances 0.000 abstract description 3
- 239000002893 slag Substances 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 2
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 239000008246 gaseous mixture Substances 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 description 44
- 239000003575 carbonaceous material Substances 0.000 description 7
- 239000006227 byproduct Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- 230000006399 behavior Effects 0.000 description 5
- 238000007664 blowing Methods 0.000 description 5
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010459 dolomite Substances 0.000 description 2
- 229910000514 dolomite Inorganic materials 0.000 description 2
- SZVJSHCCFOBDDC-UHFFFAOYSA-N ferrosoferric oxide Chemical compound O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- -1 ore Substances 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000012546 transfer 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、石炭を燃料および還元剤として用い、鉄鉱
石を転炉型炉内において溶融状態で還元する溶融還元法
、特にそのプロセスフローの簡素化およびその制御の容
易化に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a smelting reduction method in which iron ore is reduced in a molten state in a converter type furnace using coal as a fuel and a reducing agent, and particularly to the process flow thereof. It concerns simplification and ease of control.
この種の溶融還元法としては、例えば、特公昭４５−１
７０４６号公報に示された方法が知られている。As this type of melt reduction method, for example,
A method disclosed in Japanese Patent No. 7046 is known.
これは、溶融還元炉に炭化水素流体と酸素とを、該溶融
還元炉の排ガスと熱交換器を介して熱交換させながら供
給し、該炭化水素流体を該溶融還元炉内で燃焼させろと
共に、また、該溶融還元炉外においては、脱炭酸、脱水
処理したガスと該１容融還元炉の排ガスとの混合ガスで
鉄鉱石を予熱予備還元した該鉄鉱石を該溶融還元炉に装
入し、該鉄鉱石を該溶融還元炉内のＣＯガスで還元する
ものである。This involves supplying a hydrocarbon fluid and oxygen to a smelting reduction furnace while exchanging heat with the exhaust gas of the smelting reduction furnace through a heat exchanger, and combusting the hydrocarbon fluid within the smelting reduction furnace. In addition, outside the smelting reduction furnace, the iron ore is preheated and pre-reduced using a mixed gas of decarbonated and dehydrated gas and the exhaust gas of the one-volume smelting reduction furnace, and then the iron ore is charged into the smelting reduction furnace. , the iron ore is reduced with CO gas in the smelting reduction furnace.
上記のような従来の溶融還元法では、還元剤として炭化
水素系流体を使用しているため、製造コストが高くなる
という問題を有している。The conventional smelting reduction method described above uses a hydrocarbon fluid as a reducing agent, and therefore has the problem of high manufacturing costs.
また、脱炭酸、脱水処理をしたガスを溶融通元炉ガスと
混ぜて吹き込むために、予備還元率は上がり溶融還元炉
の負担は軽くなるが、プロセスが複雑になり、かつ製造
コストが高くなるという問題点を別に有している。In addition, since the decarbonated and dehydrated gas is mixed with the melting furnace gas and blown in, the preliminary reduction rate increases and the load on the melting reduction furnace is reduced, but the process becomes complicated and the manufacturing cost increases. There is another problem.
さらに、酸素および炭化水素流体の吹き込み前に排ガス
との熱交換器を設けているので、設備費がかかるばかり
でなく、実用上配管の損耗や炭化水素の分解による配管
づまり等を生ずるという問題点があった。Furthermore, a heat exchanger with the exhaust gas is installed before the oxygen and hydrocarbon fluids are blown in, which not only increases equipment costs, but also causes problems such as wear and tear on the pipes and clogging of the pipes due to hydrocarbon decomposition. was there.
この発明は、かかる問題点を解決するためになされたも
ので、プロセスが簡単で設備費がかからず、設備トラブ
ルを生じない溶融還元法を確立することを目的としてい
るものである。This invention was made in order to solve these problems, and aims to establish a melting reduction method that is a simple process, does not require equipment costs, and does not cause equipment trouble.
この発明は、上述の目的を達成するために検討の結果完
成したものであって、溶融還元炉内に石炭と酸素とを供
給してこれ等を燃焼させつつ、該溶融還元炉の外で予熱
予備還元した原料鉱石（鉄鉱石）を該溶融還元炉内に装
入して、該溶融還元炉内の炭酸ガスでこれを溶融還元す
るプロセスからなり、該溶融還元炉から発生する排ガス
の酸化度（ＯＤ比）を０．５〜０．９９となるように調
節し、該排ガスに予熱予Ｗｉｊｚ元に使用した後の冷却
排ガスを混合してこの混合排ガスを所定昌度にし、該混
合排ガスで該鉄鉱石を予熱予備還元することからなる溶
融還元法、に関するものである。This invention was completed as a result of studies to achieve the above-mentioned object, and while supplying coal and oxygen into a smelting reduction furnace and burning them, preheating is carried out outside the smelting reduction furnace. The process consists of charging pre-reduced raw material ore (iron ore) into the smelting reduction furnace and melting and reducing it with carbon dioxide gas in the smelting reduction furnace, and the degree of oxidation of the exhaust gas generated from the smelting reduction furnace (OD ratio) is adjusted to 0.5 to 0.99, and the cooled exhaust gas that has been used as a preheating source is mixed with the exhaust gas to make the mixed exhaust gas a predetermined degree. The present invention relates to a smelting reduction method comprising preheating and pre-reducing the iron ore.
なお、ＯＤ比とは、
ＯＤ ＝ （ＣｚＯ”ＨｔＯ） ／ （ＣＯ＋ＣＯ１＋
Ｉ［２＋Ｈ，Ｏ）で表される値である。In addition, the OD ratio is OD = (CzO”HtO) / (CO+CO1+
It is a value expressed as I[2+H,O).
溶融還元炉を制御するための主たるパラメーターとして
は、
■ 反応の系に投入する炭材と鉱石（媒溶剤、石灰、ド
四マイトなどを含む）の比率、■ 反応系に吹き込む酸
素の流量（すなわち、ＯＤ比の調節）、
■ 予熱予！／ｌｊ還元用ガス量およびガス温度の調節
、
■ 余熱エネルギー量の調節、
の４項目に大きく分類することができる。The main parameters for controlling a smelting reduction furnace are: ■ The ratio of carbonaceous material and ore (including solvent, lime, dotemite, etc.) introduced into the reaction system, ■ The flow rate of oxygen blown into the reaction system (i.e. , OD ratio adjustment), ■ Preheating! /lj Adjustment of the amount of reducing gas and gas temperature; (1) Adjustment of the amount of residual heat energy.
前述の■〜■の挙動を定性的に示すと第２図〜第４図と
なるが、このうち第２図は導入酸素量によるＯＤ比の変
化の挙動を、炭材と鉱石の部用量比を変更させた場合に
ついて示したものであり、第３図はＯＤ比と導入炭材量
の関係を示したものであり（実線は炭材供給量ｋｇ ／
ｔ％破線は生成ガスｍＮｒｎ’／ ｔ） 、まｔこ、
第４図は、ｍ ｍｌ １１における鉱石予熱温度が与え
る炭材消費量への影響を示したものである。Figures 2 to 4 qualitatively illustrate the behavior of the above-mentioned ■ to ■. Of these, Figure 2 shows the behavior of changes in the OD ratio depending on the amount of introduced oxygen. Fig. 3 shows the relationship between the OD ratio and the amount of carbon material introduced (the solid line is the amount of carbon material supplied kg/kg).
The t% broken line is the generated gas mNrn'/t), Matoko,
FIG. 4 shows the influence of the ore preheating temperature on the carbon material consumption at m ml 11.
これらのグラフの挙動から、ＯＤ比の値が、およそ０．
５〜０，９９の範囲にあるとき、および、鉱石予熱１度
は、およそ８００〜１１００℃程度であるときが灯まし
い領域となる。From the behavior of these graphs, the value of the OD ratio is approximately 0.
When the temperature is in the range of 5 to 0.99 degrees Celsius, and when the ore preheating temperature is about 800 to 1100 degrees Celsius, it becomes a bright region.
これらの予備的知見を利用して構成した１実施例が、第
１図に示したようなものであり、０．５〜１．５Ｇｃａ
ｌ ／ Ｌ程度の範囲で操業する際に±０．１Ｇｃａｌ
／ ｔの精度で実施することが可能なように設計して
いるものである。One example constructed using these preliminary findings is shown in Fig.
±0.1Gcal when operating in the range of l/L
It is designed to be able to be performed with an accuracy of /t.
基本的には、１５００〜１６５０℃程度の溶湯温度と、
予備還元率０．１％程度、余熱温度７００〜１１００℃
、導入ガス温度最高温度で１３５０℃である流！！：！
Ｉ＋層タイプの予熱予備還元炉の運転条件を使用し、そ
の他スクラバー、コンプレッサーキャリアガス、予ｍ還
元炉温度調節用ガスおよび回収ガスのラインなどのシス
テムから構成しているものである。Basically, the molten metal temperature is about 1500-1650℃,
Preliminary reduction rate approximately 0.1%, residual heat temperature 700-1100℃
, a flow whose maximum temperature of the introduced gas is 1350°C! ! :!
It uses the operating conditions of an I+ layer type preheating pre-reducing furnace, and also consists of systems such as a scrubber, compressor carrier gas, pre-reducing furnace temperature control gas, and recovery gas line.
以上に述べた予備的な技術背景を踏まえた上で、さらに
本発明の構成と効果について具体的な実施例を用いて詳
細に説明する。Based on the preliminary technical background described above, the structure and effects of the present invention will be further explained in detail using specific examples.
実施例 １
第１図は、この発明を実施するための設備の一実施例を
示す説明図であり、１は溶融還元炉（溶湯潤度１５００
〜１６５０℃）、２は流動層タイプの予熱予備還元炉（
予備還元率０．１程度、予熱温度７００〜１１００℃、
装入ガス温度７００〜１１００℃（最高で１３５０℃程
度）、それ以上ではクラッキングなどの問題がある）、
３は蒸気回収装置（ガス顕熱回収）、４はスクラバー、
５はコンプレッサー、６は炭材、石灰等吹き込み用キャ
リアガス、７は予熱予備還元炉吹き込みガス温度調節用
ガス、８は回収ガスである。Example 1 FIG. 1 is an explanatory diagram showing an example of equipment for carrying out the present invention, and 1 is a melting reduction furnace (molten metal moisture 1500
~1650℃), 2 is a fluidized bed type preheating pre-reduction furnace (
Preliminary reduction rate about 0.1, preheating temperature 700-1100℃,
Charging gas temperature: 700 to 1100°C (maximum 1350°C), above which problems such as cracking may occur)
3 is a steam recovery device (gas sensible heat recovery), 4 is a scrubber,
5 is a compressor, 6 is a carrier gas for blowing carbonaceous material, lime, etc., 7 is a gas for adjusting the temperature of the gas blown into the preheating pre-reducing furnace, and 8 is a recovered gas.
上記のように構成された設備を運転するにあたっては、
先ず、溶融還元Ｐｌ内に石炭および工業用純酸素（純度
７０％以上）を供給し、供給された該石炭を溶融還元炉
１内で燃焼させ、また、溶融還元炉ｌ外の予熱予備還元
Ｆ２において鉄鉱石および／またＺよ石灰石と接触せし
めて鉄鉱石を部分的に低級酸化物および遊離の鉄まで予
熱予＋！ｉ還元し、石灰石を予熱し、予熱予備還元され
た該鉄鉱石を調節された温度にて溶融還元炉１内に装入
し、装入された該鉄鉱石を溶融還元炉１内のＣＯガスで
還元することになる。When operating equipment configured as above,
First, coal and industrial pure oxygen (purity 70% or more) are supplied into the smelting reduction Pl, and the supplied coal is burned in the smelting reduction furnace 1, and the preheating preliminary reduction F2 outside the smelting reduction furnace 1 is Contact with iron ore and/or limestone to partially preheat the iron ore to lower oxides and free iron! The iron ore that has been preheated and pre-reduced is charged into the smelting reduction furnace 1 at a controlled temperature, and the charged iron ore is heated with CO gas in the smelting reduction furnace 1. It will be refunded.
このとき、溶融還元炉１から発生する排ガスのＯＤ比が
０．５〜０．９９となるようにコントロールし、該排ガ
スに予熱予備還元に使用した後の冷却排ガスを混合して
この混合排ガス７を所定温度にし、混合排ガス７で該鉄
鉱石を予熱予備還元する。At this time, the OD ratio of the exhaust gas generated from the melting reduction furnace 1 is controlled to be 0.5 to 0.99, and the exhaust gas is mixed with the cooled exhaust gas after being used for preheating and preliminary reduction, and this mixed exhaust gas 7 is brought to a predetermined temperature, and the iron ore is preheated and pre-reduced using the mixed exhaust gas 7.
上記の方法においては、系内から得られる余剰エネルギ
ー（生成ガス、顕熱、潜熱、ｙ！Ｅ、気、回収を力等）
が、−貫製鉄プロセスである高炉・転炉法における、焼
結・コークス炉・高炉より得られる余剰エネルギー（０
、７〜１ 、３ Ｇ ｃ ａ ｌ ／生成鉄量）とほぼ
同じとなるように操業する。In the above method, surplus energy obtained from within the system (produced gas, sensible heat, latent heat, y!E, gas, recovered power, etc.)
- Surplus energy (0
, 7-1, 3 G c a /amount of iron produced).
ここで、炉の制御要因としての主なるパラメータとして
は、以下のものがある。Here, the main parameters as control factors for the furnace include the following.
１、投入、炭材／鉱石比、石炭、鉱石、溶媒剤石灰また
は石灰石、軽ドロマイｌ−、生ドロマイトの投入速度、
インプットした全エネルギーは石炭史用量によって定ま
り、余剰エネルギーは副生エネルギーとなる。1. Input, carbonaceous material/ore ratio, coal, ore, solvent lime or limestone, light dolomite l-, raw dolomite input rate,
The total energy input is determined by the historical amount of coal, and the surplus energy becomes by-product energy.
２、吹き込み酸素量、ＯＤ比コントロールプロセス全系
のグロスエネルギー、鉱石／石炭比、０□吹き込み景が
ＯＤ比と関係してくる。2. Blowing oxygen amount, OD ratio control The gross energy of the entire process system, ore/coal ratio, and 0□ blowing pattern are related to the OD ratio.
プロセス系内／＼のイングツ１−エネルギーは。Ingts 1-energy of /\ in the process system is.
プロセス内で使用したエネルギーと、残りピートロス（
余剰エネルギ〜）との和となる。The energy used in the process and the remaining peat loss (
surplus energy ~).
３、予熱予備還元炉用ガス量及びガス温度コントロール
ＤＲＣガス扁度とメタル温度の差が伝熱効率に影響する
。3. Preheating Prereduction Furnace Gas Amount and Gas Temperature Control The difference between DRC gas flatness and metal temperature affects heat transfer efficiency.
４、余剰エネルギー量コントロール
実施例 ２
第１図に示した構成を有する溶融還元炉装置を（走用し
てつぎのような実験を行った。4. Surplus Energy Amount Control Example 2 The following experiment was conducted using a melting reduction furnace apparatus having the configuration shown in FIG. 1.
先ず、流動層２の上部から鉱石１４７０ｋｇ（水分３％
外数）および炭酸カルシウム１５１ｋｇを装入し、流動
層２の下部から１３５０℃のガスを吹き込ませたところ
、８００℃の四三酸化鉄（Ｆｃ３０４）が得られたが、
このときのヒートロスは、３０Ｘ１０’ｋｅａｌであっ
た。First, 1470 kg of ore (moisture 3%
When 151 kg of calcium carbonate and 151 kg of calcium carbonate were charged and gas at 1350°C was blown from the bottom of the fluidized bed 2, triiron tetroxide (Fc304) at 800°C was obtained.
The heat loss at this time was 30×10'keal.
乙のＦｅ３Ｏ４を石炭７００ｋｇ、酸素４９０ Ｎ ｎ
ｔと’４ ｆＡｌ、 ５０４ Ｘ １０３ｋｃａｌ、Ｃ
Ｏ３０，０％、Ｃ０２４９，１％、）ｉ、１２．５％、
Ｈ２Ｏ７゜０％およびＮ２０，８％からなる副生ガス４
０ＯＮ ｒｎ’と共に、溶融還元加工に装入して溶融還
元反応を起こさせたが、この時の１８融還元炉内を温度
は１７８９℃であった。B's Fe3O4 is mixed with 700 kg of coal and 490 N of oxygen.
t and '4 fAl, 504 x 103kcal, C
O30.0%, C0249.1%, )i, 12.5%,
By-product gas 4 consisting of H2O7°0% and N20.8%
0ON rn' was charged into melt reduction processing to cause a melt reduction reaction, and the temperature inside the No. 18 melt reduction furnace at this time was 1789°C.
以上のようにして１りた溶融金属（よ、１５００℃の温
度で１０００ ｋｇあり、そのうち、鉄ｉ：ｆ り ７
０ｋｇ、炭素は３０ｋｇ、スラグは２００ｋｇであった
。The molten metal produced as above (1000 kg at a temperature of 1500°C, of which iron i: f 7
0 kg, carbon was 30 kg, and slag was 200 kg.
また、このときの熱の損失量は、５０Ｘ１０’ｋｃａｌ
であった。Also, the amount of heat loss at this time is 50X10'kcal
Met.
一方、流ｅＪＭ２を出た排ガス１よ、１９０５Ｎｍ’、
１７０４℃の状態で取出されるが、これｌ、を蒸気回収
装置３で水魚％ １０３５ ｋｇの形で回収され、また
、スクラバー（４）ではゲス）・を除去し副生ガスとし
て貯蔵するラインに導いた。On the other hand, the exhaust gas 1 that came out of the flow eJM2, 1905 Nm',
It is taken out at a temperature of 1,704°C, but it is recovered in the form of 1,035 kg of aquatic fish in the steam recovery device 3, and in the scrubber (4), it is sent to a line where it is removed and stored as a by-product gas. lead.
この副生ガスは、１１９９Ｎｍ、潜熱１５０４ｘｉｏ３
１ｃｃａｌ 、ＣＯ３０，９％、Ｃｏ２４９． 。This by-product gas has a latent heat of 1199Nm and 1504xio3
1 ccal, CO30.9%, Co249. .
１％、Ｉ！、１２．５％、ｔ［２０７゜０％、Ｎ２０゜
８％であった。1%, I! , 12.5%, t[207°0%, N20°8%.
この副生ガスの一部を、コンプレッサー（５）で圧縮し
、そのうちの４０ＯＮｍ’を溶融還元Ｐ（１）の排ガス
に混むして排ガスを１３５０℃まで冷却し、これを流動
層２に吹き込ませることは前述の通りである。A part of this by-product gas is compressed by the compressor (5), and 40ONm' of it is mixed with the exhaust gas of the melt reduction P (1), the exhaust gas is cooled to 1350°C, and this is blown into the fluidized bed 2. This is as stated above.
また、石炭装入のために使用するギヤリヤーガスとして
、１７ＯＮｒｒｉ’程度の副生ガスを別途に１東用した
。In addition, about 17 ONrri' of by-product gas was separately used as a gear gas for charging coal.
実施例 ３
第１図における流動層２で予備還元の程度を替え、かつ
ＯＤ比の値を変化させた条件下で各種の測定を行い、数
表のその結果をまとめて示したが、それと共にこれらの
挙動を第５図〜第１０図にグラフとして示した。Example 3 Various measurements were carried out under conditions in which the degree of preliminary reduction was changed in the fluidized bed 2 in Fig. 1 and the value of the OD ratio was changed, and the results are summarized in a numerical table. These behaviors are shown as graphs in FIGS. 5 to 10.
なお、表中におけるガス成分として、予（Ｉ！還元０％
、室温導入、排ガス温度１５００℃の場合を例としてそ
の成分を以下に示す。In addition, the gas components in the table are preliminarily (I! reduction 0%
The components are shown below, taking as an example the case of room temperature introduction and exhaust gas temperature of 1500°C.
ＯＤ比 ０．２ ０，３ ０，５Ｃｏ Ｎゴ
１５１２ ９９２ ４８７ＣＯａ ｌ／
３７８ ４２５ ４ｇ７Ｈ，ｌ／３７９
２１８ ８６Ｈ２０１３４３３３８３１３
Ｎ 、 ｌ／２３９ ２０９ １８１合
計 １ ２８４９ ２１８１
１５５５〔発明の効果〕
この発明は以上説明したとおり、溶融還元炉から発生す
る排ガスのＯＤ比が０．５〜０．９９となるようにコン
トロールし、該排ガスに予熱予備還元に使用した後の冷
却排ガスを混合してこの混合排ガスを所定；帛度にし、
該混合排ガスで該鉄鉱石を予熱予備還元することにより
、設備をコンパクトにし、その制御性を良好にするとい
う効果がある。OD ratio 0.2 0.3 0.5Co Ngo 1512 992 487COa l/
378 425 4g7H, l/379
218 86H201343338313 N, l/239 209 181
Total 1 2849 2181
1555 [Effect of the Invention] As explained above, this invention controls the OD ratio of the exhaust gas generated from the smelting reduction furnace to be 0.5 to 0.99, and controls the OD ratio of the exhaust gas generated from the smelting reduction furnace to Mixing the cooled exhaust gas and making this mixed exhaust gas a predetermined strength,
Preheating and pre-reducing the iron ore with the mixed exhaust gas has the effect of making the equipment more compact and improving its controllability.
第１図はこの発明を実施するための設備の一実施例を示
す説明図、第２図〜第１０図はグラフでありそのうち第
２図は導入酸素景によるＯＤ比の変化の挙動、第３図は
ＯＤ比と炭材の関係をしめしたものであり、第４図は鉱
石予熱温度と炭材消費量の関係を示したもの、第５図は
ＯＤ比と石炭使用量の挙動を示したもの、第６図はＯＤ
比と酸素」ｌの関係を示したもの、第７図はＯＤ比と生
成スラグ量の関係を示したもの、第８図はＯＤ比と総排
ガス量の関係を示したもの、第９図はＯＤ比と排ガス潜
熱を、第１０図はＯＤ比と排ガス顕熱の関係を示したも
のである。
１・・・溶融還元炉、２・・・流ｒｊＪＪ層タイプの予
熱予備還元炉、３・・蒸気回収装置、４・−スクラバー
、５・・コンプレッサー、６・・炭材、石灰等吹き込み
用キャリアガス、７・・予熱予備還元炉吹き込みガス温
度調節用ガス、８・・・回収ガス。Fig. 1 is an explanatory diagram showing an example of equipment for carrying out the present invention, Figs. The figure shows the relationship between OD ratio and coal material, Figure 4 shows the relationship between ore preheating temperature and coal consumption, and Figure 5 shows the behavior of OD ratio and coal consumption. Figure 6 is OD
Figure 7 shows the relationship between the OD ratio and the amount of slag produced, Figure 8 shows the relationship between the OD ratio and the total amount of exhaust gas, and Figure 9 shows the relationship between the OD ratio and the total amount of exhaust gas. FIG. 10 shows the relationship between the OD ratio and the exhaust gas latent heat, and FIG. 10 shows the relationship between the OD ratio and the exhaust gas sensible heat. 1... Melting reduction furnace, 2... Flow RJJJ layer type preheating pre-reduction furnace, 3... Steam recovery device, 4... Scrubber, 5... Compressor, 6... Carrier for blowing carbonaceous material, lime, etc. Gas, 7... Gas for preheating and preliminary reduction furnace blowing gas temperature adjustment, 8... Recovery gas.
Claims (1)
せつつ、該溶融還元炉の外で予熱予備還元した原料鉱石
（鉄鉱石）を該溶融還元炉内に装入して、該溶融還元炉
内の炭酸ガスでこれを溶融還元するプロセスからなり、
該溶融還元炉から発生する排ガスの酸化度（ＯＤ比）を
０．５〜０．９９となるように調節し、該排ガスに予熱
予備還元に使用した後の冷却排ガスを混合してこの混合
排ガスを所定温度にし、該混合排ガスで該鉄鉱石を予熱
予備還元することからなる溶融還元法。While supplying coal and oxygen into the smelting reduction furnace and burning them, raw material ore (iron ore) that has been preheated and pre-reduced outside the smelting reduction furnace is charged into the smelting reduction furnace. It consists of a process of melting and reducing it with carbon dioxide gas in a melting reduction furnace.
The degree of oxidation (OD ratio) of the exhaust gas generated from the smelting reduction furnace is adjusted to 0.5 to 0.99, and the cooled exhaust gas after being used for preheating and preliminary reduction is mixed with the exhaust gas to produce this mixed exhaust gas. A smelting reduction method comprising bringing the iron ore to a predetermined temperature and preheating and pre-reducing the iron ore with the mixed exhaust gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18968886A JPS6347307A (en) | 1986-08-14 | 1986-08-14 | Smelting and reducing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18968886A JPS6347307A (en) | 1986-08-14 | 1986-08-14 | Smelting and reducing method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6347307A true JPS6347307A (en) | 1988-02-29 |
Family
ID=16245516
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP18968886A Pending JPS6347307A (en) | 1986-08-14 | 1986-08-14 | Smelting and reducing method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6347307A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5183495A (en) * | 1989-12-04 | 1993-02-02 | Nkk Corporation | Method for controlling a flow rate of gas for prereducing ore and apparatus therefor |
-
1986
- 1986-08-14 JP JP18968886A patent/JPS6347307A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5183495A (en) * | 1989-12-04 | 1993-02-02 | Nkk Corporation | Method for controlling a flow rate of gas for prereducing ore and apparatus therefor |
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