JP5565150B2 - Blast furnace operation method - Google Patents
Blast furnace operation method Download PDFInfo
- Publication number
- JP5565150B2 JP5565150B2 JP2010151590A JP2010151590A JP5565150B2 JP 5565150 B2 JP5565150 B2 JP 5565150B2 JP 2010151590 A JP2010151590 A JP 2010151590A JP 2010151590 A JP2010151590 A JP 2010151590A JP 5565150 B2 JP5565150 B2 JP 5565150B2
- Authority
- JP
- Japan
- Prior art keywords
- blast furnace
- ammonia
- reducing material
- tuyere
- blown
- 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.)
- Active
Links
- 238000000034 method Methods 0.000 title claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 77
- 239000000463 material Substances 0.000 claims description 37
- 229910021529 ammonia Inorganic materials 0.000 claims description 36
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 239000000571 coke Substances 0.000 claims description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 238000011017 operating method Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 14
- 238000007664 blowing Methods 0.000 description 14
- 239000002184 metal Substances 0.000 description 12
- 229910052751 metal Inorganic materials 0.000 description 12
- 239000001257 hydrogen Substances 0.000 description 11
- 229910052739 hydrogen Inorganic materials 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 7
- 239000003949 liquefied natural gas Substances 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 4
- 235000011130 ammonium sulphate Nutrition 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Landscapes
- Manufacture Of Iron (AREA)
Description
本発明は羽口から補助還元材を吹き込む高炉操業に関する。 The present invention relates to a blast furnace operation in which an auxiliary reducing material is blown from a tuyere.
近年、炭酸ガス排出量の増加による地球温暖化が問題となっており、製鉄業においても排出ＣＯ2の抑制は重要な課題である。これを受け、最近の高炉操業では低還元材比操業においてＣＯ2排出量を削減する方法が強力に推進されている。高炉は主にコークスおよび微粉炭を還元材として使用しており、低還元材比、ひいては炭酸ガス排出抑制を達成するためにはコークス等を廃プラスチック、ＬＮＧ（Liquefied Natural Gas：液化天然ガス）、重油等の水素含有率の高い還元材で置換する方策が有効である。炭素の代わりに水素を還元材として利用することにより、発生するＣＯ2を大幅に削減することが可能と考えられている。水素含有率の高い還元材を高炉で用いる技術として、高炉にＬＮＧを羽口より吹き込み、製銑工程で排出される炭酸ガスを低減させる低炭酸ガス排出製鉄法が知られている（例えば、特許文献１、特許文献２参照。）。
In recent years, global warming due to an increase in carbon dioxide emissions has become a problem, and the suppression of emitted CO 2 is an important issue even in the steel industry. In response, recent blast furnace operations are strongly promoting methods for reducing CO 2 emissions in operations with a low reducing material ratio. Blast furnaces mainly use coke and pulverized coal as reducing materials. In order to achieve a low reducing material ratio, and in order to reduce carbon dioxide emission, coke is used as waste plastic, LNG (Liquefied Natural Gas), It is effective to replace with a reducing material having a high hydrogen content such as heavy oil. It is considered that CO 2 generated can be significantly reduced by using hydrogen as a reducing material instead of carbon. As a technique for using a reducing material having a high hydrogen content in a blast furnace, a low carbon dioxide exhaust iron manufacturing method is known in which LNG is blown into the blast furnace from the tuyere to reduce the carbon dioxide discharged in the ironmaking process (for example, patents).
また、水素ガスを補助還元材として利用する方法も知られている（例えば、特許文献３参照。） A method of using hydrogen gas as an auxiliary reducing material is also known (see, for example, Patent Document 3).
上記のように、水素含有率の高い還元材を高炉の羽口から補助還元材として吹き込むことで、コークス、微粉炭等の炭素系還元材を削減し、排出ＣＯ2を抑制することが可能となるが、例えばＬＮＧの主成分はメタン（ＣＨ4）であり、ＣＨ4由来の炭素も還元材として利用されることから、大幅な炭酸ガス削減量は期待できない。これに対して、水素ガス単体を補助還元材として用いれば、炭酸ガス削減量を大幅に増やすことができることになる。 As described above, by blowing a reducing material with a high hydrogen content from the tuyere's tuyere as an auxiliary reducing material, it is possible to reduce carbon-based reducing materials such as coke and pulverized coal, and to suppress exhaust CO 2 However, for example, the main component of LNG is methane (CH 4 ), and since carbon derived from CH 4 is also used as a reducing material, a significant reduction in carbon dioxide gas cannot be expected. On the other hand, if hydrogen gas alone is used as an auxiliary reducing material, the carbon dioxide gas reduction amount can be greatly increased.
しかし、水素は輸送が困難であるという問題がある。気体還元材として用いるものであっても、気体の状態での輸送は体積が大きく効率的でないため、ＬＮＧのように液体の状態で輸送することが望ましいが、このためには低温の貯蔵タンクが必要となる。ＬＮＧの場合、主成分のＣＨ4の沸点が−１６２℃であるのに対し、水素の沸点は−２５３℃であるため、水素の輸送には極低温の貯蔵タンクが必要となり、このようなタンクを用いてトラック等で輸送を行なうことは非常にコスト高であり現実的でない。したがって、水素ガスの利用は、製鉄所内に水素ガスの発生設備があるような、限られた場合にのみ有効な手段であり、炭素を含まない補助還元材を高炉の羽口から大量に吹き込み、排出ＣＯ2を抑制することは現状では困難である。 However, there is a problem that hydrogen is difficult to transport. Even if it is used as a gas reducing material, it is desirable to transport in a liquid state such as LNG because transportation in a gas state is large and inefficient, but for this purpose, a low-temperature storage tank is used. Necessary. In the case of LNG, the boiling point of CH 4 as a main component is −162 ° C., whereas the boiling point of hydrogen is −253 ° C. Therefore, a cryogenic storage tank is required for transporting hydrogen, and such a tank It is very expensive and unrealistic to transport the vehicle using a truck or the like. Therefore, the use of hydrogen gas is an effective means only in a limited case where there is a hydrogen gas generation facility in the steelworks, and a large amount of auxiliary reducing material containing no carbon is blown from the tuyere's tuyere, It is difficult to suppress the exhausted CO 2 at present.
したがって本発明の目的は、このような従来技術の課題を解決し、補助還元材の少なくとも一部として炭素を含有しない還元材を羽口から吹き込む高炉操業であって、補助還元材の輸送や吹き込みのためのコストを大幅に増加させること無く、従来以上に炭酸ガスの削減効果の大きい、高炉操業方法を提供することにある。 Accordingly, an object of the present invention is to solve such a problem of the prior art, and is a blast furnace operation in which a reducing material containing no carbon is blown from the tuyere as at least a part of the auxiliary reducing material, and transportation and blowing of the auxiliary reducing material. An object of the present invention is to provide a method for operating a blast furnace that has a greater effect of reducing carbon dioxide gas than before without significantly increasing the cost for the operation.
上記の課題を解決するために、本発明では極低温で液化させる必要がないため輸送が容易であり、炭素を含有しないアンモニア（ＮＨ3）を補助還元材として用いることに想到し、本発明を完成した。アンモニアは沸点が−３３℃であるため水素に比較して液化がはるかに容易であり、ＬＮＧに比較しても液化が容易である。液化したアンモニアは、輸送が容易であり、貯蔵の際の設備も低コストで建設することができる。またＨ2に比較して、単位体積あたりの水素含有率が高いという特徴もある。アンモニアガス１モル当たり水素ガスの１．５倍の水素を含有する。 In order to solve the above problems, the present invention does not need to be liquefied at a very low temperature and is therefore easy to transport, and has been conceived to use ammonia containing no carbon (NH 3 ) as an auxiliary reducing material. completed. Ammonia has a boiling point of −33 ° C., so it is much easier to liquefy than hydrogen, and liquefaction is also easier than LNG. Liquefied ammonia can be easily transported and equipment for storage can be constructed at low cost. In addition, the hydrogen content per unit volume is higher than that of H 2 . It contains 1.5 times as much hydrogen as hydrogen gas per mole of ammonia gas.
本発明はこのような知見に基づきなされたもので、その特徴は以下の通りである。
（１）鉄含有原料とコークスとを高炉の炉頂から装入し、羽口から空気または酸素富化空気を送風する高炉操業において、
補助還元材として、アンモニアを前記羽口から吹き込むことを特徴とする高炉操業方法。
（２）前記酸素富化空気の酸素富化率を３０体積％以下として、前記アンモニアの吹き込み量を１３０ｋｇ／ｔ−ｐ以下とすることを特徴とする（１）に記載の高炉操業方法。
（３）前記アンモニアはコークス炉ガス中のアンモニアであることを特徴とする（１）または（２）に記載の高炉操業方法。
The present invention has been made based on such findings, and the features thereof are as follows.
(1) In blast furnace operation in which iron-containing raw material and coke are charged from the top of the blast furnace and air or oxygen-enriched air is blown from the tuyere,
A blast furnace operating method, wherein ammonia is blown from the tuyere as an auxiliary reducing material.
(2) The blast furnace operating method according to (1), characterized in that an oxygen enrichment rate of the oxygen-enriched air is set to 30% by volume or less, and an ammonia blowing amount is set to 130 kg / tp or less.
(3) The method for operating a blast furnace according to (1) or (2), wherein the ammonia is ammonia in coke oven gas.
本発明によれば、炭素を含有しない還元材を用いて羽口からの補助還元材吹き込みを行なうことで、高炉のコークス比を低減すると共に、排出ＣＯ2量を大幅に削減することが可能となる。 According to the present invention, it is possible to reduce the coke ratio of the blast furnace and greatly reduce the amount of CO 2 emission by blowing the auxiliary reducing material from the tuyere using a reducing material that does not contain carbon. Become.
本発明では上記のように、補助還元材としてアンモニア（ＮＨ3）を高炉の羽口から吹き込むものである。高炉の羽口からは空気または酸素富化空気が送風されるが、通常は補助還元材として微粉炭等の固体還元材が同時に吹き込まれる。本発明では固体還元材に追加して、または固体還元材の少なくとも一部と代替して、高炉の羽口から、ランス等を用いてアンモニアの吹き込みを行なう。固体還元材とアンモニアとは、同一の羽口に複数本のランスを装着して吹き込んでも良く、羽口ごとに吹きこみ還元材の種類を変えても構わない。さらに、重油等の液体還元材を同時に吹き込むことも可能である。 In the present invention, as described above, ammonia (NH 3 ) is blown from the tuyere of the blast furnace as an auxiliary reducing material. Air or oxygen-enriched air is blown from the tuyere of the blast furnace, but usually a solid reducing material such as pulverized coal is blown simultaneously as an auxiliary reducing material. In the present invention, in addition to the solid reducing material or in place of at least part of the solid reducing material, ammonia is blown from the blast furnace tuyere using a lance or the like. The solid reducing material and ammonia may be blown in by attaching a plurality of lances to the same tuyere, and the type of blowing reducing material may be changed for each tuyere. Furthermore, it is possible to simultaneously blow in liquid reducing material such as heavy oil.
本発明の一実施形態を図１を用いて説明する。 An embodiment of the present invention will be described with reference to FIG.
高炉１では、羽口２から送風３と、補助還元材として微粉炭４の吹き込みを行なっている。羽口から高炉内にアンモニア５の吹き込みを行なうが、このためには、貯蔵タンク６に貯蔵された液体アンモニアを気化して、高炉内に吹込み可能な圧力まで昇圧機７で昇圧後、羽口２に接続したブローパイプを貫通させて設置したランスを用いて炉内に吹き込む。吹き込まれたアンモニアは炉内の高温で分解されてＨ2が生成し、還元材として作用する。
In the
アンモニアを高炉内に吹き込んだ場合、炉内ガス組成（ボッシュ部でのガス組成で、計算値を用いる。）は通常の操業に比較して、水素濃度が高くなる。分解により生成したＨ2は高炉内で発生するＣＯ、ＣＯ2やＮ2に比較してガス密度が低く、通常の微粉炭吹込み高炉操業に比較して高炉内での通気性を良好とする。 When ammonia is blown into the blast furnace, the gas concentration in the furnace (the gas composition in the Bosch section, using the calculated value) has a higher hydrogen concentration than in normal operation. H 2 produced by cracking has a lower gas density than CO, CO 2 and N 2 generated in the blast furnace, and better air permeability in the blast furnace compared to normal pulverized coal injection blast furnace operation. .
アンモニアの吹き込み量は、ＣＯ2の発生量を少なくできるので多いほど好ましいが、吹込み量が多くなるほど、羽口先理論燃焼温度を維持するために酸素富化率を高くする必要が生じる。そのため、通常の送風機の酸素濃度管理値から３０体積％程度の酸素富化率が安全上上限となり、アンモニアの吹き込み量は１３０ｋｇ／ｔ−ｐ（溶銑）程度が現実的な上限となる。尚、酸素富化率とは、「（熱風中酸素量＋酸素供給量）／（送風量）×１００−熱風中酸素濃度（％）」で定義され、送風量は「熱風量（空気）＋酸素供給量」である。例えば、熱風量が１０００Ｎｍ3／ｔ−ｐ、酸素供給量が５０Ｎｍ3／ｔ−ｐであれば、（１０００×０．２１＋５０）／（１０００＋５０）×１００−２１＝３．７６％となる。ｋｇ／ｔ−ｐ（溶銑）とは、溶銑１ｔ製造当たりに吹き込まれるアンモニアの質量を示している。 The ammonia blowing amount is preferably as large as possible because the amount of CO 2 generated can be reduced. However, as the blowing amount increases, it is necessary to increase the oxygen enrichment rate in order to maintain the tuyere theoretical combustion temperature. Therefore, an oxygen enrichment rate of about 30% by volume is an upper limit for safety from the oxygen concentration management value of a normal blower, and the practical upper limit is about 130 kg / tp (molten metal) for the ammonia blowing amount. The oxygen enrichment rate is defined as “(hot air oxygen amount + oxygen supply amount) / (air flow rate) × 100−hot air oxygen concentration (%)”, and the air flow rate is “hot air amount (air) + Oxygen supply amount ". For example, the hot air amount 1000Nm 3 / t-p, if the oxygen supply amount 50Nm 3 / t-p, the (1000 × 0.21 + 50) / (1000 + 50) × 100-21 = 3.76%. kg / tp (molten metal) indicates the mass of ammonia blown per 1 ton of molten iron.
アンモニアとして、コークス炉でコークス製造の際に発生するコークス炉ガス（ＣＯＧ）に含まれるアンモニアを回収して用いることが好ましい。通常、コークス炉から発生するガス中には６〜１０ｇ／Ｎｍ3のアンモニアが含有されており、希硫酸で洗浄し、硫安として回収されて、硫安肥料として販売されている。しかしながら、硫安肥料の需要が減少した場合、他に適当な用途も無いため、硫安の市場価値が大幅に低落し、採算性が著しく悪くなる恐れがある。また、アンモニアを燃焼し、単純に熱として回収することも可能であるが、燃焼過程でフーエルＮＯX、サーマルＮＯXが発生しやすく、ＮＯX発生を抑制する燃焼制御が必要である。したがって、コークス炉ガスに含まれるアンモニアを高炉羽口から吹き込む補助還元材として用いることで、製鉄所内で発生する副生成物を安定的に、ＮＯX発生の問題もなく、有効に利用することが可能となる。ＣＯＧからのアンモニアの回収方法としては、例えばカールスチル法を用いることができる（例えば、非特許文献１参照。）。ＣＯＧ中のアンモニアを水またはアンモニア水で吸収し、次に、アンモニア水を蒸留してアンモニア蒸気とする方法である。 As ammonia, it is preferable to recover and use ammonia contained in coke oven gas (COG) generated during coke production in a coke oven. Normally, the gas generated from the coke oven contains 6 to 10 g / Nm 3 of ammonia, washed with dilute sulfuric acid, recovered as ammonium sulfate, and sold as ammonium sulfate fertilizer. However, when the demand for ammonium sulfate fertilizer decreases, there is no other suitable use, so the market value of ammonium sulfate is greatly reduced, and the profitability may be significantly deteriorated. In addition, ammonia can be burned and simply recovered as heat, but fuel NO x and thermal NO x are likely to be generated in the combustion process, and combustion control is required to suppress NO x generation. Thus, by using as an auxiliary reducing agent blowing ammonia contained in the coke oven gas from the blast furnace tuyeres, stable by-products generated in the steelworks, without problems of the NO X generation, it is used effectively It becomes possible. As a method for recovering ammonia from COG, for example, the Karl Still method can be used (see, for example, Non-Patent Document 1). In this method, ammonia in COG is absorbed with water or aqueous ammonia, and then the aqueous ammonia is distilled into ammonia vapor.
または、使用済みプラスチック等の廃棄物を原料として製造したリサイクル品のアンモニアを用いることが好ましい。 Alternatively, it is preferable to use ammonia, which is a recycled product manufactured using waste such as used plastic as a raw material.
アンモニアはそれ自体がＣ成分を含まない点で高炉操業におけるＣＯ2排出量削減に効果があるが、原料を含めてカーボンフリーのクリーンなアンモニアを用いることがさらに好ましい。すなわち、アンモニアを製造する段階でも、カーボンに由来しない原料を用い、ＣＯ2を発生させていないものを用いることで、完全に地球全体としてのＣＯ２排出量削減に貢献できることになる。 Ammonia itself is effective in reducing CO 2 emissions in blast furnace operation in that it does not contain a C component, but it is more preferable to use carbon-free clean ammonia including raw materials. That is, even at the stage of producing ammonia, by using a material that does not originate from carbon and that does not generate CO 2 , it is possible to completely contribute to CO 2 emission reduction as a whole of the earth.
図１に示すものと同様の、炉内容積約５０００ｍ3の高炉において、条件１〜５の操業試験を実施した。アンモニア以外の補助還元材としては微粉炭を１３０ｋｇ／ｔ−ｐ（溶銑）とし、羽口先理論燃焼温度が２２４９℃になるように酸素富化率を調整した。表１に各操業条件と結果を示す。条件１は比較例であり、アンモニア（ＮＨ3）吹込みを行なわない従来の操業の場合である。アンモニア吹込み量は条件２で２５ｋｇ／ｔ−ｐ（溶銑）、条件３は５０ｋｇ／ｔ−ｐ（溶銑）、条件４は１００ｋｇ／ｔ−ｐ（溶銑）、条件５で１３０ｋｇ／ｔ−ｐ（溶銑）である。送風圧力は３．４×１０5Ｐａとし、アンモニアを吹き込む際の吹込み圧力は３．９×１０5Ｐａとした。
In a blast furnace having a furnace internal volume of about 5000 m 3 similar to that shown in FIG. As an auxiliary reducing material other than ammonia, pulverized coal was 130 kg / tp (molten metal), and the oxygen enrichment rate was adjusted so that the theoretical combustion temperature at the tuyere became 2249 ° C. Table 1 shows the operating conditions and results.
アンモニアを吹き込むことで、還元材比（ＲＡＲ）は上昇するが、Ｃ投入量は減少する。これに伴い、条件２ではＣＯ2発生削減量は１６ｋｇ−ＣＯ2／ｔ−ｐ（溶銑）、条件３では３２ｋｇ−ＣＯ2／ｔ−ｐ（溶銑）、条件４では６３ｋｇ−ＣＯ2／ｔ−ｐ（溶銑）、条件５では８２ｋｇ−ＣＯ2／ｔ−ｐ（溶銑）となり、ＣＯ2発生量を大幅に削減することができた。 By blowing ammonia, the reducing material ratio (RAR) increases, but the amount of C input decreases. Accordingly, the CO 2 generation reduction amount is 16 kg-CO 2 / tp (hot metal) in condition 2 , 32 kg-CO 2 / tp (hot metal) in condition 3, and 63 kg-CO 2 / t- in condition 4. Under p (molten metal) and condition 5, the amount was 82 kg-CO 2 / tp (molten metal), and the amount of generated CO 2 could be greatly reduced.
また、炉内ボッシュ部での各種ガスの合計のガス密度（ボッシュガス密度）は、条件１（比較例）で１．１７ｋｇ／Ｎｍ3、条件２で１．１３ｋｇ／Ｎｍ3、条件３で１．０９ｋｇ／Ｎｍ3、条件４で１．００ｋｇ／Ｎｍ3、条件５で０．９４ｋｇ／Ｎｍ3となり、ガス密度の低下から炉内通気性が改善されたものと考えられる。 The gas density (Bosch gas density) of the total various gases in the furnace Bosch unit, condition 1 (Comparative Example) 1.17 kg / Nm 3, condition 2 by 1.13 kg / Nm 3, in condition 3 1 0.09 kg / Nm 3 , Condition 4 is 1.00 kg / Nm 3 , Condition 5 is 0.94 kg / Nm 3 , and it is considered that the air permeability in the furnace was improved due to the decrease in gas density.
１ 高炉
２ 羽口
３ 送風
４ 補助還元材
５ アンモニア
６ 貯蔵タンク
７ 昇圧機
８ 高炉ガス
1
Claims (2)
補助還元材として、液体アンモニアを気化させた、カーボンフリーの気化アンモニアを前記羽口から吹き込むことを特徴とする高炉操業方法。 In blast furnace operation in which iron-containing raw material and coke are charged from the top of the blast furnace and air or oxygen-enriched air is blown from the tuyere,
A method for operating a blast furnace, wherein carbon-free vaporized ammonia obtained by vaporizing liquid ammonia is blown from the tuyere as an auxiliary reducing material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2010151590A JP5565150B2 (en) | 2010-07-02 | 2010-07-02 | Blast furnace operation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2010151590A JP5565150B2 (en) | 2010-07-02 | 2010-07-02 | Blast furnace operation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2012012678A JP2012012678A (en) | 2012-01-19 |
| JP5565150B2 true JP5565150B2 (en) | 2014-08-06 |
Family
ID=45599452
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2010151590A Active JP5565150B2 (en) | 2010-07-02 | 2010-07-02 | Blast furnace operation method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP5565150B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20220062628A (en) * | 2019-11-29 | 2022-05-17 | 제이에프이 스틸 가부시키가이샤 | Blast furnace operation method and blast furnace auxiliary equipment |
| CN115478122A (en) * | 2022-10-10 | 2022-12-16 | 北京首钢国际工程技术有限公司 | Ammonia-rich raw fuel for blast furnace iron making and blast furnace iron making method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5154095A (en) * | 1974-11-01 | 1976-05-12 | Texaco Development Corp | Kangengasuno seizohoho |
| JPH03215613A (en) * | 1990-01-19 | 1991-09-20 | Nkk Corp | Operation of blast furnace |
| JPH04268003A (en) * | 1991-02-21 | 1992-09-24 | Nippon Steel Corp | Method for operating blast furnace |
| JP2004309067A (en) * | 2003-04-09 | 2004-11-04 | Nippon Steel Corp | Method of using blast furnace gas |
| JP5605828B2 (en) * | 2010-03-03 | 2014-10-15 | 国立大学法人北海道大学 | Iron making method and iron making system |
-
2010
- 2010-07-02 JP JP2010151590A patent/JP5565150B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| JP2012012678A (en) | 2012-01-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP6229863B2 (en) | Oxygen blast furnace operation method | |
| CN102037145B (en) | Method for melting raw iron while recirculating blast furnace gas by adding hydrocarbons | |
| JP4661890B2 (en) | Blast furnace operation method | |
| CN113999945A (en) | Method for operating blast furnace | |
| KR20140043385A (en) | System and method for reducing iron oxide to metallic iron using coke oven gas and oxygen steelmaking furnace gas | |
| JP2015510030A (en) | Blast furnace for recirculating furnace top gas | |
| EP3687941B1 (en) | Method for producing hot synthesis gas, in particular for use in blast furnace operation | |
| WO2023240753A1 (en) | Low-carbon smelting system and method based on blast furnace-steelmaking furnace process coupled carbon cycle | |
| JP5509676B2 (en) | How to operate a vertical furnace | |
| JP5593883B2 (en) | How to reduce carbon dioxide emissions | |
| JP5565150B2 (en) | Blast furnace operation method | |
| CN108430914A (en) | Make the method for carbon dioxide decomposition and recycling using hot-blast stove | |
| JP5315732B2 (en) | Blast furnace operation method | |
| JP5851828B2 (en) | Method for producing combustible gas | |
| JP2009509905A (en) | Method for producing hydrogen and / or other gases from steel plant waste and waste heat | |
| JP5884156B2 (en) | Blast furnace operation method | |
| JP2012067326A (en) | Reduced iron manufacturing method | |
| US20230366050A1 (en) | Device to inject a reducing gas into a shaft furnace | |
| JP5614517B1 (en) | Blast furnace operation method | |
| CN103740873B (en) | A kind of system for blast furnace ironmaking | |
| JP2011190471A (en) | Method for operating blast furnace | |
| JP2020045508A (en) | Operation method of blast furnace | |
| JP7131698B2 (en) | Blast Furnace Operation Method and Blast Furnace Incidental Equipment | |
| US20230366047A1 (en) | Blast furnace for ironmaking production | |
| US20230366049A1 (en) | Device to inject a reducing gas into a shaft furnace |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| RD03 | Notification of appointment of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7423 Effective date: 20120321 |
|
| RD04 | Notification of resignation of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7424 Effective date: 20120327 |
|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20130419 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20140131 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20140218 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20140418 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20140520 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20140602 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 5565150 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |