JP4250472B2 - Method for producing reduced iron and reducing gas for blast furnace charge, method for using reduced iron, and method for using reducing gas - Google Patents

Method for producing reduced iron and reducing gas for blast furnace charge, method for using reduced iron, and method for using reducing gas Download PDF

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JP4250472B2
JP4250472B2 JP2003201216A JP2003201216A JP4250472B2 JP 4250472 B2 JP4250472 B2 JP 4250472B2 JP 2003201216 A JP2003201216 A JP 2003201216A JP 2003201216 A JP2003201216 A JP 2003201216A JP 4250472 B2 JP4250472 B2 JP 4250472B2
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reducing gas
gas
furnace
reduced iron
iron
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JP2005042142A (en
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正己 小野田
晴是 汐田
隆文 河村
泰 高本
卓夫 重久
俊一 矢内
正明 田村
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Kobe Steel Ltd
Nippon Steel Corp
Nippon Steel Engineering Co Ltd
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Kobe Steel Ltd
Nippon Steel Corp
Nippon Steel Engineering Co Ltd
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00Combustion technologies with mitigation potential
    • Y02E20/16Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00Combustion technologies with mitigation potential
    • Y02E20/16Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/30Fuel from waste, e.g. synthetic alcohol or diesel
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/10Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00Technologies for solid waste management
    • Y02W30/20Waste processing or separation
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00Technologies for solid waste management
    • Y02W30/50Reuse, recycling or recovery technologies
    • Y02W30/62Plastics recycling; Rubber recycling

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  • Manufacture Of Iron (AREA)
  • Industrial Gases (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Processing Of Solid Wastes (AREA)

Description

【0001】
【発明の属する技術分野】
本発明は、石炭等の炭素質資源をガス化して還元性ガスを製造し、この還元性ガスを用いて還元鉄、水素、電力を効率的に併産する方法に関する。
【0002】
【従来の技術】
固体還元炉内でCOガスやH2ガスを主成分とする還元性ガスを用いて還元鉄を作る方法が知られている。固体還元炉としてはシャフト炉や流動層が用いられる。図2にシャフト炉を用いた還元方法の一例を示す。還元性ガス発生装置1にて天然ガスを水蒸気で改質してH2ガスとCOガスを主成分とする700〜900℃の還元性ガスを製造し、固体還元炉4内で鉄鉱石2と還元性ガスが直接接触して、CO、H2がCO2、H2Oに変化して鉄鉱石中の酸素を除去して還元する。鉄鉱石を還元したガスは、まだ温度が高く、鉄粉ダストを含み、CO、H2をまだ含むことから、熱回収装置5で熱回収、集塵装置6で脱塵、ガス冷却装置7で冷却、脱炭酸装置9で脱炭酸された後、ガス加熱炉10で再加熱されて還元性ガスとして再利用される。
【0003】
還元性ガスを製造する原料として、天然ガスのかわりに石炭が使用できると好適である。石炭は埋蔵量の豊富さ、供給の安定性、価格の低廉性から長期にわたり安定して使用できるからである。図3には、石炭を原料として還元鉄を製造する方法の一例を示す。還元性ガスの製造には石炭ガス化炉12が用いられる。石炭15を粉砕した微粉炭をガス化バーナーから酸素ガス16(必要に応じて蒸気17を添加する)とともにガス化炉12に吹き込んでガス化する。ガス化温度は、石炭中の灰分を溶融して分離するため1400〜1700℃の高温で行うのが一般的である。ガス化したガスは、ガス化炉上部を通って冷却炉13にはいる。石炭中の灰分の大部分は、溶融してガス化炉下部から落下して固化スラグになる。冷却炉13では、内部に輻射ボイラーを配置して輻射伝熱でガスを冷却し、あるいは冷却炉から排出したガスを熱回収、集塵、冷却した後に冷却炉に吹き込んでガスを冷却する。
【0004】
特許文献1には、石炭ガス化による還元性ガスの製造と、そのガスを利用して行う鉄鉱石還元を効率的に組み合わせた発明が記載されている。天然ガスから製造した還元性ガスを用いた場合には、還元に使用したガスを熱回収、脱塵、冷却、脱炭酸した後、再加熱して還元性ガスとして再利用していた。それに対し、石炭ガス化による還元性ガスを用いる場合には、還元に使用したガスを図3に示すように還元炉4から排出した還元性ガスの一部を熱回収装置5で熱回収、集塵装置6で脱塵、ガス冷却装置7で冷却、脱炭酸装置9で脱炭酸された後、再加熱せず、冷却炉に吹き込む。ガス化炉でガス化された高温のガスとリサイクルされた低温の還元性ガスが冷却炉で混合され、鉄鉱石還元に好適な700〜900℃の温度に調整することができる。
【0005】
特許文献1に記載の発明において、還元に使用したガスを脱炭酸した後、その一部を系外に取り出すようにしている。石炭をガス化して還元性ガスを製造する場合、石炭中の硫黄が転化した硫化水素ガスが含有される。そのため、系外に抜き出すガスの処理については、ガス中の硫黄を除去する脱硫装置等を必要に応じて設置することが好ましいとしている。
【0006】
特許文献2には、図4に示すように、石炭をガス化して還元性ガスを含む合成ガスを生成し、前記還元性ガスを利用して鉄鉱石を還元して還元鉄を製造する石炭ガス化直接還元製鉄法が記載されている。石炭ガス化炉ガスに含まれるH2S等の硫黄化合物の還元鉄品質に与える影響を考えると、石炭ガス化炉ガスの脱硫をすることが望ましく、石炭ガス化炉ガスは熱間脱硫を行うことが望ましいとしている。そのため、還元炉の手前に脱硫装置20を設けている。また、鉄鉱石を還元した400〜500℃のガスは、ガス化原料の石炭の乾燥に利用している。
【0007】
非特許文献1には、石炭ガス化炉ガスで製造したガスを燃料とする石炭ガス化複合発電について記載されている。一例を図5に示す。石炭ガス化還元性ガスは、サイクロンで粗集塵された後に熱回収装置5で熱回収、集塵装置6で脱塵、ガス冷却装置7で冷却を行い、さらに脱硫装置21での脱硫により清浄化された後に、ガスタービン、蒸気タービンの複合発電装置22に供される。
【0008】
【特許文献1】
特開2000−212620号公報
【特許文献2】
特開2002−146420号公報
【特許文献3】
特開平8−253801公報
【非特許文献1】
「ガス化複合サイクル発電」 火力原子力発電 Vol.52, No.10 (2001), pp1244-1252
【0009】
【発明が解決しようとする課題】
石炭ガス化炉やその周辺設備はその建設費が高いため、石炭ガス化直接還元製鉄あるいは石炭ガス化複合発電を商業化する上での障害となっている。本発明は、設備投資効率を向上して石炭ガス化直接還元製鉄や石炭ガス化複合発電を商業化可能とすることを第1の目的とする。
【0010】
石炭をガス化したガス中には硫黄分が含まれる。一方、還元製鉄で製造された還元鉄は、一般的に電気炉原料として用いられ、不純物としての硫黄分が低いことが要請される。そのため、石炭ガス化直接還元製鉄においては、特許文献2に記載のように、還元炉の手前にガスの脱硫装置20を設けることが必要とされる。そのために、脱硫が可能な400〜500℃の温度まで一旦冷却して脱硫した後に約900℃まで再加熱してから還元炉に投入せざるを得なかった。石炭ガス化複合発電においても、非特許文献1に記載のように、複合発電に供される前に脱硫装置21によってガスの脱硫が行われる。石炭ガス化直接還元製鉄で用いられた還元性ガスを系外に抜き出して再利用するに際しても、特許文献1に記載のようにガス中の硫黄を除去する脱硫装置を設置すると好ましいとされている。このように、石炭ガス化ガスを用いるに際しては必ず脱硫装置の設置が不可欠であり、これが石炭ガス化炉周辺設備の建設費を高める要因となっていた。本発明は、石炭ガス化直接還元製鉄あるいは石炭ガス化複合発電において、脱硫設備の設置を不要とすることを第2の目的とする。併せて、脱硫設備以外の付帯設備についてもその簡素化を図ることを目的とする。
【0011】
地球温暖化問題への対応は、新エネルギーの開発・実用化、低二酸化炭素発生エネルギーへのシフト、原子力比率の向上、既存一次エネルギーの効率的かつ合理的利用、未利用エネルギーや廃棄物エネルギーの利用等で進められている。特にバイオマスはカーボンニュートラルであり、積極的に利用して石油、石炭等を代替すべき資源であるといえる。また廃プラスチックについても、積極的に利用して石油、石炭等を代替すべき資源であるといえる。本発明は、バイオマスや廃プラスチックを石炭の代替として使用し、二酸化炭素の排出量を削減することを第3の目的とする。
【0012】
【課題を解決するための手段】
即ち、本発明の要旨とするところは以下の通りである。
(1)石炭に加えてバイオマスと廃プラスチックの一方若しくは両方を含む炭素質原料15、又は、石炭を酸素16により部分燃焼させて還元性ガス11を製造し、該還元性ガス11を冷却した後、冷却後の700〜900℃の還元性ガスを鉄鉱石2が充填されているシャフト炉4に送り込み、該還元性ガス11が該シャフト炉4内を上昇する過程で、該還元性ガス11と該鉄鉱石2を該シャフト炉4中で接触させて鉄鉱石を還元し、硫黄分を0.14〜1.4質量%の範囲で含有し、金属鉄を含む固体の還元鉄3を製造すると共に、該還元性ガス11を脱硫して該シャフト炉から400〜500℃の還元性ガスを排出して、脱硫された還元性ガス11を製造することを特徴とする高炉装入原料用還元鉄及び還元性ガスの製造方法。
(2)前記硫黄分を含有する固体の還元鉄の金属化率を40〜80%とすることを特徴とする上記(1)記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。
(3)シャフト炉4から排出された還元性ガス11と、還元性ガス11に同伴して排出された鉄鉱石および還元鉄の硫黄分を含有する微粉とを分離し、更に脱硫された還元性ガスとすることを特徴とする上記(1)又は(2)に記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。
(4)還元性ガス11に含まれる硫黄分を還元鉄3に移動することによって脱硫された還元性ガス11を得ることを特徴とする上記(1)乃至(3)のいずれかに記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。
(5)還元性ガス11を製造するガス化炉12に引き続いて冷却炉13を有し、バイオマスと廃プラスチックの一方又は両方を含む炭素質原料を冷却炉13中に投入することを特徴とする上記(1)乃至(4)のいずれかに記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。
(6)(1)乃至(5)のいずれかの方法に記載の硫黄分を含有する固体の還元鉄3を、高炉に投入することを特徴とする還元鉄の利用方法。
(7)(1)乃至(6)のいずれかの方法に記載の脱硫された還元性ガス11を、水素ガス製造及び/又は複合発電に利用することを特徴とする還元性ガスの利用方法。
(8)前記脱硫された還元性ガス11に水及び/又は水蒸気を添加し、該還元性ガスの顕熱を熱源として利用して還元性ガス中のCOガスをHガスとCO2ガスに改質し、該CO2ガスを吸収分離することにより水素ガスを製造することを特徴とする上記(7)に記載の還元性ガスの利用方法。
【0013】
本発明において、硫黄分を含有する炭素質原料、特に石炭を用いて製造した還元性ガス中の硫黄について、シャフト炉4で還元性ガスから還元鉄に移動し、硫黄分を含有する固体の還元鉄を製造し、結果としてシャフト炉4から排出された還元性ガスは脱硫されてなることを特徴とする。そのため、シャフト炉4から排出された還元性ガスを水素ガス製造原料や複合発電燃料として利用するに際しても、還元性ガスから硫黄分を除去するための脱硫設備を設置する必要がない。また、還元性ガス中の硫黄分は還元鉄中に移動するので、シャフト炉投入前の還元性ガスから硫黄分を除去するための脱硫設備も設置する必要がない。
【0014】
本発明で好ましくは、製造した固体の還元鉄を高炉装入原料として高炉に投入する。高炉はそれ自体で脱硫機能を有しているので、装入された還元鉄中に硫黄が含まれていても、高炉で製造される銑鉄の硫黄分の上昇は極めて僅かである。そのため、本発明によって製造した硫黄分を含有する還元鉄であっても、何ら問題なく製鉄原料として使用することができる。
【0015】
高炉内で鉄鉱石を還元する還元剤はコークスであり、コークス製造用の石炭には安価な一般炭はほとんど用いることができない。それに対し、石炭ガス化直接還元製鉄には安価な一般炭を用いることが可能である。従って、本発明の石炭ガス化還元製鉄で製造した還元鉄を高炉に装入することにより、全体として製鉄に使用する石炭のコストを低減することが可能になる。
【0016】
本発明において、炭素質原料をガス化して製造した還元性ガスについて、まずシャフト炉中で鉄鉱石を還元するのに使用し、その後水素ガス製造や複合発電に使用される。そのため、還元性ガスの熱回収装置、集塵装置等を共用することができる。従って、還元製鉄と複合発電を別々に実施する設備に比較し、付帯設備を効率的に使用することが可能になる。
【0017】
【発明の実施の形態】
図1に基づいて本発明の説明を行う。
【0018】
まず、硫黄分を含有する炭素質原料を酸素により部分燃焼させて還元性ガスを製造するためのガス化炉について説明する。特に炭素質原料が石炭である場合について説明を行うので、石炭ガス化炉12と呼ぶことがある。
【0019】
石炭15を粉砕した微粉炭をガス化バーナーから酸素ガス16に必要に応じて蒸気17を加えたガスとともにガス化炉12に吹き込む。ガス化温度は、石炭中の灰分を溶融して分離するため1400〜1700℃の温度とする。これにより、ガス化炉内においてCO、H2を主成分とする還元性ガスを製造する。生成した還元性ガス11には、石炭から持ち込まれる硫黄に起因するH2S(一部COS)が500〜5000ppm含まれる。ガス化したガスは、ガス化炉上部を通って冷却炉13に入る。石炭中の灰分の大部分は、溶融してガス化炉下部から落下し、水槽で固化スラグになる。
【0020】
冷却炉13では、内部に輻射ボイラーを配置して輻射伝熱でガスを冷却し、あるいは冷却炉に生成したガスや還元炉から排出された還元性ガスの一部を熱回収、集塵、ガス冷却したガスの一部を冷却炉に吹き込んでガスを冷却する。冷却炉にバイオマスや廃プラスチックを含む炭素質原料を吹き込む本発明については、後で詳述する。
【0021】
ガス中には若干の固形分が残存しているために、必要に応じてサイクロン14にて固形分を除去する。固形分はガス化原料として利用される。
【0022】
次に、ガス化炉12で生成した還元性ガス11と鉄鉱石2を接触させて鉄鉱石を還元する固体シャフト炉4について説明する。
【0023】
シャフト炉4の内部にはペレット状の鉄鉱石または鉄鉱石塊が充填され、順次シャフト炉4を下降する過程で還元性ガス11によって還元され、シャフト炉下端から還元鉄3として排出される。シャフト炉4の上端から鉄鉱石2が投入され、シャフト炉内の鉄鉱石を補充する。一方、シャフト炉4の下端から約900℃の還元性ガス11が送り込まれ、シャフト炉内を上昇する過程で鉄鉱石と還元性ガスが直接接触し、還元性ガス中のCO、H2がCO2、H2Oに変化して鉄鉱石中の酸素を除去して還元する。還元性ガスは還元反応を進行させつつシャフト炉内を上昇し、シャフト炉上端から排出される。
【0024】
シャフト炉下端から送り込む還元性ガスの温度は700〜900℃とし、シャフト炉下端における固体(還元鉄、鉄鉱石)の温度も当該ガス温度よりやや低い温度に保たれる。シャフト炉内での還元反応を効率的に行うために上記温度が選定される。シャフト炉内上下方向の温度分布については、上方に行くほど還元性ガス、固体(還元鉄、鉄鉱石)ともに温度が低くなる。シャフト炉上端におけるガスと固体の温度は、固体の流量(kg/h)と固体の比熱(kcal/kg/deg)の積Wsとガスの流量(kg/h)とガスの比熱(kcal/kg/deg)の積Wgとの比(Ws/Wg)とシャフト炉下端から送り込む還元性ガスの温度を調整することによって調整することができる。
【0025】
従来、石炭ガス化直接還元製鉄で製造された還元鉄は、電炉製鋼原料として主に用いられていた。電炉で製造する鋼は低い硫黄含有量とすることが要請されるので、原料としての還元鉄も当然低い硫黄含有量とすることが要請される。
【0026】
そのため、従来は還元炉に入る前に脱硫設備を設け、還元性ガス中の硫黄分を除去する必要があった。
【0027】
一方、還元炉前に脱硫設備を設けない場合における炉内での硫黄分の反応について述べる。還元炉内で還元性ガス中のH2Sが鉄鉱石と反応してFeSとなる反応は、400〜600℃の温度範囲で進行する。従来は、この反応の進行を極力阻止するため、シャフト炉内で400〜600℃の温度範囲となる領域をできるだけ回避するような温度分布が採用されていた。具体的には、シャフト炉上端における還元性ガス温度を550〜700℃の温度範囲程度としていた。これにより、シャフト炉に送り込む還元性ガス中の硫黄分の50%程度が還元鉄中に移動し、残りの50%が還元性ガス中に残存したままで還元炉から排出されていた。
【0028】
本発明においては、シャフト炉4に送り込む還元性ガス中の硫黄分のできるだけ多くを還元鉄中に移動させる。そのため本発明においては、シャフト炉上端における還元性ガスの温度を400〜600℃とする。400〜500℃とするとより好ましい。これにより、還元性ガスから還元鉄中に硫黄分が移動する脱硫が進行する400〜600℃の温度範囲となる領域を広げることができる。その結果、シャフト炉に送り込む還元性ガス中の硫黄分の90%程度が還元鉄中に移動し、還元性ガス中に残存したままで還元炉から排出される硫黄分を10%以下まで抑えることが可能になる。
【0029】
シャフト炉4から排出された還元性ガス11には鉄鉱石及び還元鉄の微粉が同伴する。還元性ガス11は集塵装置6に導かれ、還元性ガス中の上記微粉は、集塵装置6によって集塵される。ところで、シャフト炉4の上端から集塵装置6までの間、還元性ガス11の温度は400℃以上の高温に保たれ、還元性ガス中に含まれる鉄鉱石や還元鉄の微粉温度も同じ温度に保たれる。この温度は還元性ガスの脱硫をさらに進行させる温度域であるので、還元性ガス中に残存したH2Sは、集塵装置6に到達するまでの間に還元性ガス中の鉄鉱石や還元鉄微粉に移動し、この微粉が集塵装置6で集塵されるので、集塵装置6を通過した後の還元性ガスの硫黄分をさらに低減することができる。
【0030】
以上のように、本発明においては、還元性ガスに含まれる硫黄分を還元鉄に移動することによって脱硫された還元性ガスを得ることを特徴とするので、シャフト炉から排出された還元性ガスを脱硫するための脱硫設備を必要としない。
【0031】
本発明で硫黄分を含有する炭素質原料とは、硫黄分を0.1%以上含有する炭素質原料をいう。硫黄分を含有する炭素質原料の代表例は石炭である。これに、後述するようにバイオマスと廃プラスチックの一方又は両方を含有させることができる。石炭チャーを使用することもできる。これらの炭素質資源を微粉状または粒状にして用いる。CO、H2ガスが生成されれば、炭素質資源の種類は問わない。従って各種の炭素質資源が利用できる。
【0032】
また、本発明で硫黄分を含有する固体の還元鉄とは、硫黄分を0.03%以上含有する固体の還元鉄をいう。
【0033】
さらに、脱硫された還元性ガスとは、還元性ガス中の硫黄分が70ppm以下のものをいう。これにより、そのまま、燃焼炉用の燃料として利用することが可能になる。硫黄分が50ppm以下であればより好ましい。これにより、複合発電用燃料として利用することが可能になる。ただし、硫黄分を数%含むような高硫黄石炭を用いる場合には脱硫装置が必要な場合もあるが、その能力は著しく軽減できる。
【0034】
本発明においては、炭素質原料として、石炭に加えて、バイオマスと廃プラスチックの一方又は両方を含むこととすることができる。本発明では、バイオマスのうちで気流搬送が容易な木質系および農業系バイオマスを対象としている。バイオマスについての定義はFAO(国連食糧農業機関)の定義に準ずる。即ち、木質系バイオマスとは、FAO定義における林業系バイオマスと、廃棄物系バイオマスの一部を指し、製紙廃棄物、製材廃材、除間伐材、薪炭林、庭木、木材などの建設廃材、などが該当する。また農業系バイオマスとは、麦わら、もみがら等の農業系廃棄物および菜種、大豆等の農業系エネルギー作物、などが該当する。これを使用するのは、含有水分が少なく(〜50質量%)湿分基準の発熱量が高く、気流搬送が可能な粒子に容易に加工できるためである。また廃プラスチックとは、例えば、ポリエチレン(PE)、ポリプロピレン(PP)、ポリスチレン(PS)等のパラフィン系の高分子化合物やポリ塩化ビニル(PVC)を含む物質である。ただし、PVCは設備の腐食を回避するために極力低減する必要があり、石炭を除く炭素質原料のうちの10%以下に抑えることが好ましい。バイオマスや廃プラスチックを炭素質原料として用いることにより、石炭の代替として二酸化炭素の排出量を削減することができ、地球温暖化に対応することができる。
【0035】
バイオマスや廃プラスチックを石炭に加えてガス化炉に送り込むに際しては、粒径を5mm以下に加工または造粒することが必要である。
【0036】
前述のとおり、石炭ガス化炉12において1400〜1700℃の温度で石炭のガス化を行って還元性ガスを生成した後、生成した還元性ガスは冷却炉13へ送られ、冷却炉13において還元性ガスを1000℃程度まで冷却する。通常冷却炉13では、前述のとおり内部に輻射ボイラーを配置して輻射伝熱でガスを冷却し、あるいは冷却炉13で生成したガスやシャフト炉から排出された還元性ガスの一部を熱回収、集塵、ガス冷却したガスの一部を冷却炉13に吹き込んでガスを冷却する。
【0037】
本発明においては、冷却炉13にバイオマスや廃プラスチックを含む炭素質原料を吹き込んで冷却を行うと好ましい。冷却炉内の温度領域においても、炭素質原料のガス化を進行させることができ、この反応進行時にガスから熱を奪うので冷却を行うことができる。一方、冷却炉内の温度においては灰分が固化するので、灰分含有量の多い炭素質原料、例えば石炭は冷却炉内に吹き込む炭素質原料としては好ましくない。それに対し、バイオマスや廃プラスチックは灰分の含有量が少なく、冷却炉内に吹き込んでも灰分に起因する問題が発生しないので、冷却炉内に吹き込む炭素質原料としては最も好ましい。即ち、バイオマスと廃プラスチックの一方又は両方を含む炭素質原料を冷却炉中に投入することにより、灰分の問題を起こすことなく、還元性ガスを冷却すると同時に還元性ガスを増産することができる。
【0039】
本発明で製造した硫黄分を含有する固体の還元鉄3は、高炉に投入することとすると特に好ましい。前述のとおり、高炉はそれ自体で脱硫機能を有しているので、装入された還元鉄中に硫黄が含まれていても、高炉で製造される銑鉄の硫黄分の上昇は極めて僅かである。そのため、本発明によって製造した硫黄分を含有する還元鉄であっても、何ら問題なく製鉄原料として使用することができるからである。また、高炉装入原料とするので、特許文献3に述べられているように、還元炉における金属化率(金属鉄量/鉄鉱石中の総鉄量×100(%))は90%以上である必要はない。本発明においては金属化率は40〜80%を狙いとすると好ましい。
【0040】
また高炉内で鉄鉱石を還元する還元剤はコークスであり、コークス製造用の石炭としては高価な粘結炭が使用され、安価な一般炭の使用割合は制限される。それに対し、石炭ガス化直接還元製鉄には安価な一般炭のみを用いることが可能である。従って、本発明の石炭ガス化還元製鉄で製造した還元鉄を高炉に装入することにより、全体として製鉄に使用する石炭のコストを低減することが可能になる。
【0041】
本発明で製造した脱硫された還元性ガスを、水素ガス製造及び/又は複合発電に利用することとすると特に好ましい。還元性ガス中の硫黄分が低いので、脱硫設備を通さなくてもこのままの状態で水素ガス製造や複合発電に利用することができる。また、冷却の過程で大部分の水蒸気は除去され、脱炭酸装置を通過することで還元性ガス中のCO2が除去され、CO及びH2を主成分とする還元性ガスとすることができる。このような成分の還元性ガスは、水素ガス製造及び/又は複合発電に用いるガスとして好適である。
【0042】
本発明において、脱硫された還元性ガスに水及び/又は水蒸気を添加し、該還元性ガスの顕熱を熱源として利用して還元性ガス中のCOガスをH2ガスとCO2ガスに改質し、該CO2ガスを吸収分離することにより水素ガスを製造することとすると好ましい。
【0043】
脱硫された還元性ガスは、シャフト炉4から排出された時点で400℃前後以上の高温であり、集塵装置6で集塵を行った後にシフト反応器24において水や水蒸気を添加すれば、還元性ガスの顕熱を熱源として利用し、触媒反応によりシフト反応を起こさせ、還元性ガス中のCOガスをH2ガスとCO2ガスに改質することができる。次いで熱回収装置5で還元性ガスを冷却し、さらに脱炭酸装置9を通してCO2ガスを吸収分離すれば、結果として水素ガスを製造することができる。鉄鉱石還元後の還元性ガス中のCO2濃度は20%以上あり、さらにシフト反応後のCO2は50%以上の高濃度となるため、アミン吸収法等により高効率でCO2分離が可能である。吸収液の再生に必要な熱はプロセスの熱回収から生成した低圧蒸気、または都市ゴミ等を燃焼させて生成する低圧蒸気を活用することができる。
【0044】
このようにして製造した水素ガスは、そのまま製鉄所においては鉄鋼製品の熱処理用の還元性ガスとして、また燃料電池用の原料として使用することができる。さらに水素ガスを圧縮して複合発電に供することも可能である。なお、シフト反応を行わない場合でも、ガスを圧縮した後複合発電に供することができる。
【0045】
即ち、シャフト炉から排出された還元性ガスの用途としては、還元性ガスをシフト反応−脱炭酸したあとに水素製造または複合発電に用いる方法、還元性ガスを脱炭酸したあとに複合発電に用いる方法、還元性ガスをそのまま複合発電に用いる方法のいずれをも採用することができる。もちろん、シャフト炉4から排出された還元性ガスの一部又は全部を、冷却炉13に戻して還元性ガスを冷却すると共に、再度シャフト炉4における還元性ガスとして用いることとしてもよい。
【0046】
本発明において、炭素質原料をガス化して製造した還元性ガスについて、まずシャフト炉中で鉄鉱石を還元するのに使用し、その後水素ガス製造や複合発電に使用される。そのため、還元性ガスの熱回収装置、集塵装置等を共用することができる。従って、還元製鉄と複合発電を別々に実施する設備に比較し、付帯設備を効率的に使用することが可能になる。特に設備投資額が高額になる石炭ガス化炉については、還元性ガス製造能力が大きくなるほど還元性ガス製造量あたりの設備投資額が小さくなる。従って、還元製鉄と複合発電とのために別々に石炭ガス化炉を建設する場合に比較し、より大きな規模のひとつの石炭ガス化炉を用いて還元製鉄と複合発電を共に行う本発明は、全体の設備投資効率を向上させることができる。
【0047】
以上のように、本発明においては、石炭を主成分とする炭素質資源から還元鉄、水素、電力を効率的に併産することができる。
【0048】
【実施例】
図1に示すように、シャフト炉式還元炉を用い、還元鉄(DRI)を製造した。還元性ガス11は、ガス化炉12と冷却炉13を有する2段ガス化炉を用いて製造した。下段のガス化炉12にインドネシア産亜瀝青炭を平均粒径が50μmに粉砕した微粉炭0.67ton/t−DRIと酸素560Nm3/t−DRIを投入して部分燃焼により1500℃、5ataの条件下でガス化して製造した。更に、上段の冷却炉13において1500℃となった高温還元性ガス中に5mm以下に破砕したバイオマス(建築廃材チップ)0.3ton/t−DRIを投入して1000℃に冷却するとともに熱分解させることにより還元性ガス生成量を増加させた。還元性ガス量の20〜30%をカーボンニュートラルなバイオマスや廃プラ等で賄うことが可能である。還元性ガス中には35g/Nm3の炭素固形分が存在したが、サイクロン14により5g/Nm3以下に除塵した後、シャフト炉4に装入した。
【0049】
シャフト炉4においては、金属化率(金属鉄量/鉄鉱石中の総鉄量×100(%))が80%になるように、還元性ガス量や還元性ガス温度等の条件を設定した。還元鉄3は焼結鉱とともに高炉に装入されて溶銑の原料に利用することが狙いであることから、60〜90%の還元率であれば十分に目的は達成できる。
【0050】
還元性ガスの量、シャフト炉入口、出口のガス性状と温度を表1示す。
【0051】
【表1】

Figure 0004250472
【0052】
シャフト炉入口における還元性ガス中にはH2Sが520ppm(COSが20ppm)が含まれていたが、シャフト炉出口の除塵装置後にはH2Sは30ppm(COSは変化なし)に低減していた。一方、鉄鉱石2には極微量であったS分が還元鉄3中には0.15質量%に上昇しており、還元性ガス中のS分が還元鉄に移ったものと確認された。通常、還元鉄中の含有S分に対する市場の要求レベルは約0.015質量%であるが、本実施例においては、還元鉄は脱硫機能を持つ高炉に装入して利用したために、問題なく利用できた。本実施例において、シャフト炉出口におけるガス温度を420℃という温度に設定したため、還元性ガス中のH2Sが還元鉄と反応し、硫黄分が還元性ガスから還元鉄に移動したものである。
【0053】
尚、シャフト炉後の集塵装置6から得られたダスト中のS濃度が0.3質量%あった。シャフト炉4を出た後も400℃以上の温度が保たれていたことから還元性ガス中の鉄粉と残存H2Sとの反応が継続していたものと判断される。
【0054】
シャフト炉4から排出後の還元性ガス11は、シャフト炉前に保有していた潜熱の約1/3がシャフト炉で消費されたに過ぎず、十分に高いエネルギーを保持していた。ここでは、還元性ガス11がシフト反応(CO+H2O→H2+CO2)に有効な400℃の温度を有していることを利用し、還元性ガス11を集塵装置6で集塵した後に冷却せずにシフト反応器24に導入し、ここで水素と炭酸ガスに変換し、水素を分離利用した。その結果、水素は1400Nm3/t−DRI、CO2は2.4ton/t−DRIを回収できた。シフト反応により、CO2濃度は50%を越える高濃度となり、アミン法による吸収効率がCO2濃度10%程度のボイラー排ガスに比べて5〜10%向上した。今後のCO2固定化技術開発の進展とともに、地球温暖化対策の有望な技術になる可能性があることが判った。分離された水素ガス25は、製鉄所の熱処理用ガスとして利用した。更に、加圧して複合発電が可能なこと、および本プロセス内で循環し、鉄鉱石還元性ガスに利用できることも確認した。
【0055】
次に比較例として、シャフト炉出口における還元性ガス温度を550℃とした。これ以外の条件は上記実施例と同様である。シャフト炉出口の集塵装置後における還元性ガス中のH2Sは200ppm(COSは変化なし)までしか低減していなかった。一方、鉄鉱石には極微量であったS分が還元鉄中には0.08質量%に上昇しており、還元性ガス中のSの一部が還元鉄に移ったものと確認された。シャフト炉から排出された還元性ガス中の硫黄分は十分に低減していないので、このままでは水素ガスとしてあるいは複合発電用として用いることができない。一方、還元鉄中の硫黄分も高いので、高炉装入原料として使用することは可能であるが、電炉製鉄用の主原料として使用することは困難である。
【0056】
【発明の効果】
本発明は、還元鉄、水素、電力を効率的に併産できるので、設備投資効率を向上して石炭ガス化直接還元製鉄や石炭ガス化複合発電を商業化可能とすることができる。
【0057】
本発明はまた、石炭ガス化直接還元製鉄あるいは石炭ガス化複合発電において、脱硫設備の設置を不要とすることができる。
【0058】
本発明はさらに、バイオマスや廃プラスチックを石炭の代替として使用し、二酸化炭素の排出量を削減することができる。
【図面の簡単な説明】
【図1】本発明の炭素質資源の効率的活用方法を示す図である。
【図2】従来の還元鉄製造方法を示す図である。
【図3】従来の還元鉄製造方法を示す図である。
【図4】従来の還元鉄製造方法を示す図である。
【図5】従来の石炭ガス化複合発電方法を示す図である。
【符号の説明】
1 還元性ガス発生装置
2 鉄鉱石
3 還元鉄
シャフト炉
5 熱回収装置
6 集塵装置
7 ガス冷却装置
8 圧縮機
9 脱炭酸装置
10 ガス加熱炉
11 還元性ガス
12 石炭ガス化炉
13 冷却炉
14 サイクロン
15 炭素質原料(石炭)
16 酸素
17 水蒸気
18 石炭調湿装置
19 ガス洗浄冷却装置
20、21 脱硫装置
22 発電装置
23 電力
24 シフト反応器
25 水素ガス
26 炭素質物質
27 系外排出ガス[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method for producing a reducing gas by gasifying carbonaceous resources such as coal and efficiently producing reduced iron, hydrogen, and electric power using the reducing gas.
[0002]
[Prior art]
CO gas and H in the solid reduction furnace2A method of making reduced iron using a reducing gas containing gas as a main component is known. A shaft furnace or a fluidized bed is used as the solid reduction furnace. FIG. 2 shows an example of a reduction method using a shaft furnace. Natural gas is reformed with steam in the reducing gas generator 1 to produce H.2A reducing gas of 700 to 900 ° C. containing gas and CO gas as main components is produced, and the iron ore 2 and the reducing gas are in direct contact with each other in the solid reduction furnace 4 to produce CO, H2Is CO2, H2Change to O to remove oxygen in iron ore and reduce. The gas that reduced iron ore is still hot, contains iron dust, CO, H2Therefore, the heat recovery device 5 recovers the heat, the dust collector 6 removes the dust, the gas cooling device 7 cools, the decarbonator 9 decarboxylates, and the gas heating furnace 10 reheats and reduces. Reused as sex gas.
[0003]
It is preferable that coal can be used as a raw material for producing the reducing gas instead of natural gas. This is because coal can be used stably over a long period of time due to its rich reserves, stable supply, and low price. FIG. 3 shows an example of a method for producing reduced iron using coal as a raw material. A coal gasifier 12 is used for the production of the reducing gas. The pulverized coal obtained by pulverizing the coal 15 is gasified from the gasification burner by blowing it into the gasification furnace 12 together with oxygen gas 16 (adding steam 17 as necessary). The gasification temperature is generally performed at a high temperature of 1400 to 1700 ° C. in order to melt and separate the ash content in the coal. The gasified gas enters the cooling furnace 13 through the upper part of the gasification furnace. Most of the ash in the coal melts and falls from the lower part of the gasification furnace to become solidified slag. In the cooling furnace 13, a radiation boiler is disposed inside to cool the gas by radiant heat transfer, or the gas discharged from the cooling furnace is recovered, collected and cooled, and then blown into the cooling furnace to cool the gas.
[0004]
Patent Document 1 describes an invention that efficiently combines the production of a reducing gas by coal gasification and the reduction of iron ore using the gas. When a reducing gas produced from natural gas is used, the gas used for the reduction is heat recovered, dedusted, cooled, decarboxylated, then reheated and reused as the reducing gas. On the other hand, when reducing gas from coal gasification is used, a part of the reducing gas discharged from the reduction furnace 4 is recovered and collected by the heat recovery device 5 as shown in FIG. After dust is removed by the dust device 6, cooled by the gas cooling device 7, and decarboxylated by the decarboxylation device 9, it is blown into the cooling furnace without being reheated. The high-temperature gas gasified in the gasification furnace and the recycled low-temperature reducing gas are mixed in the cooling furnace, and can be adjusted to a temperature of 700 to 900 ° C. suitable for iron ore reduction.
[0005]
In the invention described in Patent Document 1, after decarboxylation of the gas used for the reduction, a part of the gas is taken out of the system. When producing reducing gas by gasifying coal, hydrogen sulfide gas in which sulfur in coal is converted is contained. Therefore, regarding the treatment of the gas extracted outside the system, it is preferable to install a desulfurization device or the like that removes sulfur in the gas, if necessary.
[0006]
In Patent Document 2, as shown in FIG. 4, coal gas is produced by gasifying coal to produce a synthesis gas containing a reducing gas, and reducing iron ore using the reducing gas to produce reduced iron. A direct reduction iron manufacturing process is described. H contained in coal gasifier gas2Considering the influence of sulfur compounds such as S on the quality of reduced iron, it is desirable to desulfurize the coal gasifier gas, and the coal gasifier gas desirably performs hot desulfurization. Therefore, a desulfurization device 20 is provided in front of the reduction furnace. Moreover, the 400-500 degreeC gas which reduced the iron ore is utilized for drying of the gasification raw material coal.
[0007]
Non-Patent Document 1 describes a coal gasification combined power generation using a gas produced by a coal gasifier gas as a fuel. An example is shown in FIG. After the coal gasification reducing gas is coarsely collected by the cyclone, heat is recovered by the heat recovery device 5, dedusted by the dust collector 6, cooled by the gas cooling device 7, and further purified by desulfurization by the desulfurization device 21. After being converted, it is provided to a combined power generation device 22 for a gas turbine and a steam turbine.
[0008]
[Patent Document 1]
JP 2000-212620 A
[Patent Document 2]
JP 2002-146420 A
[Patent Document 3]
JP-A-8-253801
[Non-Patent Document 1]
"Gasification combined cycle power generation" Thermal and nuclear power generation Vol.52, No.10 (2001), pp1244-1252
[0009]
[Problems to be solved by the invention]
Coal gasification furnaces and their peripheral equipment are expensive to construct, which is an obstacle to commercializing coal gasification direct reduction iron making or coal gasification combined power generation. The first object of the present invention is to improve the capital investment efficiency and enable commercialization of coal gasification direct reduction steelmaking and coal gasification combined power generation.
[0010]
The gas obtained by gasifying coal contains sulfur. On the other hand, reduced iron produced by reduced iron making is generally used as an electric furnace raw material and is required to have a low sulfur content as an impurity. Therefore, in coal gasification direct reduction iron making, as described in Patent Document 2, it is necessary to provide a gas desulfurization device 20 in front of the reduction furnace. Therefore, it has been forced to cool to a temperature of 400 to 500 ° C. where desulfurization is possible, desulfurize it, reheat it to about 900 ° C., and then put it into the reduction furnace. In coal gasification combined power generation, as described in Non-Patent Document 1, gas is desulfurized by the desulfurization device 21 before being used for combined power generation. When extracting and reusing the reducing gas used in coal gasification direct reduction iron production outside the system, it is preferable to install a desulfurization device for removing sulfur in the gas as described in Patent Document 1. . As described above, when using coal gasification gas, it is indispensable to install a desulfurization apparatus, which has been a factor in increasing the construction cost of equipment around the coal gasification furnace. The second object of the present invention is to eliminate the need for installation of a desulfurization facility in coal gasification direct reduction iron making or coal gasification combined power generation. At the same time, it aims to simplify the incidental facilities other than desulfurization facilities.
[0011]
Responses to global warming issues include the development and commercialization of new energy, a shift to low carbon dioxide generation energy, an increase in the nuclear power ratio, the efficient and rational use of existing primary energy, the utilization of unused energy and waste energy. It is promoted by use. Biomass in particular is carbon neutral and can be said to be a resource that should be actively used to replace oil, coal, and the like. Waste plastic is also a resource that should be actively used to replace oil and coal. The third object of the present invention is to use biomass or waste plastic as an alternative to coal and reduce carbon dioxide emissions.
[0012]
[Means for Solving the Problems]
  That is, the gist of the present invention is as follows.
(1) After producing the reducing gas 11 by partially burning the carbonaceous raw material 15 containing one or both of biomass and waste plastic in addition to coal, or coal with oxygen 16, and cooling the reducing gas 11 The reducing gas at 700 to 900 ° C. after cooling is sent to the shaft furnace 4 filled with the iron ore 2, and in the process in which the reducing gas 11 rises in the shaft furnace 4, The iron ore 2 is brought into contact with the shaft furnace 4 to reduce the iron ore, and the sulfur content is reduced.In the range of 0.14-1.4% by massAnd producing solid reduced iron 3 containing metallic iron, desulfurizing the reducing gas 11 and discharging a reducing gas at 400 to 500 ° C. from the shaft furnace, and desulfurizing reducing gas 11. A process for producing reduced iron and reducing gas for blast furnace charging raw material, characterized in that
(2) The method for producing reduced iron and reducing gas for blast furnace charging as described in (1) above, wherein the metallization rate of the solid reduced iron containing sulfur is 40 to 80%.
(3) The reducing gas 11 discharged from the shaft furnace 4 is separated from the iron ore discharged with the reducing gas 11 and the fine powder containing the sulfur content of the reduced iron, and further desulfurized reducing property. The method for producing reduced iron for reducing blast furnace charge and reducing gas as described in (1) or (2) above, wherein the gas is a gas.
(4) The blast furnace according to any one of (1) to (3) above, wherein the desulfurized reducing gas 11 is obtained by moving the sulfur content contained in the reducing gas 11 to the reduced iron 3. A method for producing reduced iron for reducing raw materials and reducing gas.
(5) It has a cooling furnace 13 subsequent to the gasification furnace 12 for producing the reducing gas 11, and is characterized in that a carbonaceous raw material containing one or both of biomass and waste plastic is introduced into the cooling furnace 13. The method for producing reduced iron and reducing gas for a blast furnace charging raw material according to any one of (1) to (4) above.
(6) A method for using reduced iron, characterized in that solid reduced iron 3 containing sulfur as described in any one of (1) to (5) is charged into a blast furnace.
(7) A method for using a reducing gas, wherein the desulfurized reducing gas 11 according to any one of (1) to (6) is used for hydrogen gas production and / or combined power generation.
(8) Water and / or water vapor is added to the desulfurized reducing gas 11 and sensible heat of the reducing gas is used as a heat source to convert CO gas in the reducing gas to H.2Gas and CO2Reformed into gas and the CO2The method for using a reducing gas as described in (7) above, wherein hydrogen gas is produced by absorbing and separating the gas.
[0013]
  In the present invention, sulfur in a reducing gas produced using carbonaceous raw materials containing sulfur, particularly coal,shaftMoved from reducing gas to reducing iron in furnace 4 to produce solid reduced iron containing sulfur, as a resultshaftThe reducing gas discharged from the furnace 4 is desulfurized. for that reason,shaftEven when the reducing gas discharged from the furnace 4 is used as a hydrogen gas production raw material or a combined power generation fuel, it is not necessary to install a desulfurization facility for removing sulfur from the reducing gas. Also, since the sulfur content in the reducing gas moves into the reduced iron,shaftThere is no need to install a desulfurization facility to remove sulfur from the reducing gas before charging the furnace.
[0014]
Preferably in the present invention, the produced solid reduced iron is charged into the blast furnace as a blast furnace charging raw material. Since the blast furnace itself has a desulfurization function, even if sulfur is contained in the charged reduced iron, the sulfur content of pig iron produced in the blast furnace is extremely small. Therefore, even if it is the reduced iron containing the sulfur content manufactured by this invention, it can be used as an iron-making raw material without any problem.
[0015]
The reducing agent that reduces iron ore in the blast furnace is coke, and cheap steam coal can hardly be used as coal for producing coke. On the other hand, cheap coal can be used for coal gasification direct reduction iron making. Therefore, it becomes possible to reduce the cost of the coal used for iron making as a whole by charging the reduced iron produced by the coal gasification reduction steel making of the present invention into the blast furnace.
[0016]
  In the present invention, a reducing gas produced by gasifying a carbonaceous raw materialshaftUsed to reduce iron ore in the furnace, and then used for hydrogen gas production and combined power generation. Therefore, it is possible to share a reducing gas heat recovery device, a dust collector, and the like. Therefore, it is possible to efficiently use the incidental facilities as compared to facilities that separately implement reduced iron production and combined power generation.
[0017]
DETAILED DESCRIPTION OF THE INVENTION
The present invention will be described with reference to FIG.
[0018]
First, a gasification furnace for producing a reducing gas by partially burning a carbonaceous raw material containing a sulfur content with oxygen will be described. Since the case where a carbonaceous raw material is especially coal is demonstrated, it may be called the coal gasifier 12.
[0019]
The pulverized coal obtained by pulverizing the coal 15 is blown into the gasification furnace 12 together with a gas obtained by adding steam 17 to the oxygen gas 16 as needed. The gasification temperature is set to a temperature of 1400 to 1700 ° C. in order to melt and separate the ash content in the coal. As a result, CO, H in the gasifier2Is produced as a main component. The generated reducing gas 11 includes H caused by sulfur brought in from coal.2S (partial COS) is contained in an amount of 500 to 5000 ppm. The gasified gas enters the cooling furnace 13 through the upper part of the gasification furnace. Most of the ash in the coal melts and falls from the lower part of the gasification furnace, and becomes solidified slag in the water tank.
[0020]
In the cooling furnace 13, a radiant boiler is disposed to cool the gas by radiant heat transfer, or a part of the gas generated in the cooling furnace or the reducing gas discharged from the reducing furnace is recovered, collected, and gas A part of the cooled gas is blown into a cooling furnace to cool the gas. The present invention in which the carbonaceous raw material including biomass and waste plastic is blown into the cooling furnace will be described in detail later.
[0021]
  Since some solid content remains in the gas, the solid content is removed by the cyclone 14 as necessary. Solids are used as gasification raw materialsThe
[0022]
  Next, the reducing gas 11 produced in the gasification furnace 12 and the iron ore 2 are brought into contact with each other to reduce the iron ore.shaftI will explain the furnace 4The
[0023]
The shaft furnace 4 is filled with pellet-shaped iron ore or a lump of iron ore, and is reduced by the reducing gas 11 in the course of descending the shaft furnace 4 and discharged as reduced iron 3 from the lower end of the shaft furnace. The iron ore 2 is introduced from the upper end of the shaft furnace 4 to replenish the iron ore in the shaft furnace. On the other hand, the reducing gas 11 of about 900 ° C. is fed from the lower end of the shaft furnace 4, and the iron ore and the reducing gas are in direct contact with each other during the ascending process in the shaft furnace, so that CO, H2Is CO2, H2Change to O to remove oxygen in iron ore and reduce. The reducing gas rises in the shaft furnace while a reduction reaction proceeds, and is discharged from the upper end of the shaft furnace.
[0024]
The temperature of the reducing gas fed from the lower end of the shaft furnace is 700 to 900 ° C., and the temperature of the solid (reduced iron, iron ore) at the lower end of the shaft furnace is also kept slightly lower than the gas temperature. The temperature is selected in order to efficiently carry out the reduction reaction in the shaft furnace. As for the temperature distribution in the vertical direction in the shaft furnace, the temperature decreases for the reducing gas and the solid (reduced iron, iron ore) as it goes upward. The temperature of the gas and solid at the upper end of the shaft furnace is the product Ws of the solid flow rate (kg / h) and the specific heat of the solid (kcal / kg / deg), the flow rate of the gas (kg / h) and the specific heat of the gas (kcal / kg). / Deg) can be adjusted by adjusting the ratio (Ws / Wg) to the product Wg and the temperature of the reducing gas fed from the lower end of the shaft furnace.
[0025]
Conventionally, reduced iron produced by direct gasification of coal gasification has been mainly used as an electric furnace steelmaking raw material. Since steel produced in an electric furnace is required to have a low sulfur content, naturally reduced iron as a raw material is also required to have a low sulfur content.
[0026]
Therefore, conventionally, it has been necessary to provide a desulfurization facility before entering the reduction furnace to remove the sulfur content in the reducing gas.
[0027]
On the other hand, the reaction of the sulfur content in the furnace when no desulfurization facility is provided before the reduction furnace will be described. H in the reducing gas in the reducing furnace2The reaction in which S reacts with iron ore to become FeS proceeds in a temperature range of 400 to 600 ° C. Conventionally, in order to prevent the progress of this reaction as much as possible, a temperature distribution that avoids a region in the temperature range of 400 to 600 ° C. in the shaft furnace as much as possible has been adopted. Specifically, the reducing gas temperature at the upper end of the shaft furnace was set to about 550 to 700 ° C. As a result, about 50% of the sulfur content in the reducing gas fed into the shaft furnace moved into the reduced iron, and the remaining 50% was discharged from the reducing furnace while remaining in the reducing gas.
[0028]
In the present invention, as much sulfur as possible in the reducing gas fed into the shaft furnace 4 is moved into the reduced iron. Therefore, in this invention, the temperature of the reducing gas in a shaft furnace upper end shall be 400-600 degreeC. More preferably, the temperature is 400 to 500 ° C. Thereby, the area | region used as the temperature range of 400-600 degreeC in which desulfurization from which a sulfur content moves from reducing gas in reduced iron can be expanded. As a result, about 90% of the sulfur content in the reducing gas fed into the shaft furnace moves into the reduced iron, and the sulfur content discharged from the reducing furnace is kept below 10% while remaining in the reducing gas. Is possible.
[0029]
  shaftThe reducing gas 11 discharged from the furnace 4 is accompanied by iron ore and fine powder of reduced iron. The reducing gas 11 is guided to the dust collector 6, and the fine powder in the reducing gas is collected by the dust collector 6. by the way,shaftBetween the upper end of the furnace 4 and the dust collector 6, the temperature of the reducing gas 11 is kept at a high temperature of 400 ° C. or more, and the fine powder temperature of iron ore and reduced iron contained in the reducing gas is also kept at the same temperature. It is. Since this temperature is a temperature range in which desulfurization of the reducing gas further proceeds, H remaining in the reducing gas2S moves to the iron ore and reduced iron fine powder in the reducing gas before reaching the dust collector 6, and the fine powder is collected by the dust collector 6, so that it passes through the dust collector 6. The sulfur content of the subsequent reducing gas can be further reduced.
[0030]
  As described above, the present invention is characterized in that a desulfurized reducing gas is obtained by transferring sulfur contained in the reducing gas to reduced iron.shaftNo desulfurization equipment is required to desulfurize the reducing gas discharged from the furnace.
[0031]
In the present invention, the carbonaceous raw material containing sulfur is a carbonaceous raw material containing 0.1% or more of sulfur. A typical example of the carbonaceous raw material containing sulfur is coal. This can contain one or both of biomass and waste plastic, as described below. Coal char can also be used. These carbonaceous resources are used in the form of fine powder or granules. CO, H2The type of carbonaceous resource is not limited as long as gas is generated. Therefore, various carbonaceous resources can be used.
[0032]
In the present invention, solid reduced iron containing a sulfur content refers to solid reduced iron containing a sulfur content of 0.03% or more.
[0033]
Further, the desulfurized reducing gas refers to one having a sulfur content of 70 ppm or less in the reducing gas. As a result, it can be used as it is as a fuel for a combustion furnace. More preferably, the sulfur content is 50 ppm or less. As a result, it can be used as a combined power generation fuel. However, when using high-sulfur coal containing several percent of sulfur, a desulfurization unit may be necessary, but the capacity can be significantly reduced.
[0034]
In the present invention, as a carbonaceous raw material, in addition to coal, one or both of biomass and waste plastic can be included. In the present invention, among biomass, woody and agricultural biomass that are easy to carry by airflow are targeted. The definition of biomass follows the definition of FAO (United Nations Food and Agriculture Organization). In other words, woody biomass refers to forestry biomass in the FAO definition and part of waste biomass, such as papermaking waste, sawn timber, thinned thinned wood, firewood charcoal forest, garden wood, construction waste such as wood, etc. Applicable. Agricultural biomass includes agricultural waste such as straw and rice husk and agricultural energy crops such as rapeseed and soybean. This is used because it contains a small amount of water (~ 50% by mass), has a high calorific value based on moisture, and can be easily processed into particles capable of airflow conveyance. The waste plastic is a substance containing a paraffinic polymer compound such as polyethylene (PE), polypropylene (PP), polystyrene (PS) or polyvinyl chloride (PVC). However, PVC needs to be reduced as much as possible to avoid equipment corrosion, and is preferably suppressed to 10% or less of the carbonaceous raw material excluding coal. By using biomass or waste plastic as a carbonaceous raw material, it is possible to reduce carbon dioxide emissions as an alternative to coal, and to cope with global warming.
[0035]
When biomass or waste plastic is added to coal and fed into a gasifier, it is necessary to process or granulate the particle size to 5 mm or less.
[0036]
  As described above, after coal gasification is performed at a temperature of 1400 to 1700 ° C. in the coal gasification furnace 12 to generate a reducing gas, the generated reducing gas is sent to the cooling furnace 13 and reduced in the cooling furnace 13. The sex gas is cooled to about 1000 ° C. In the normal cooling furnace 13, as described above, a radiation boiler is arranged to cool the gas by radiant heat transfer, or the gas generated in the cooling furnace 13shaftA part of the reducing gas discharged from the furnace is heat-recovered, collected, and part of the gas cooled is blown into the cooling furnace 13 to cool the gas.
[0037]
In the present invention, cooling is preferably performed by blowing a carbonaceous raw material containing biomass and waste plastic into the cooling furnace 13. Even in the temperature range in the cooling furnace, the gasification of the carbonaceous raw material can proceed, and heat can be taken from the gas when the reaction proceeds, so that the cooling can be performed. On the other hand, since ash solidifies at the temperature in the cooling furnace, a carbonaceous raw material having a high ash content, such as coal, is not preferable as a carbonaceous raw material blown into the cooling furnace. On the other hand, biomass and waste plastics are most preferable as carbonaceous raw materials to be blown into the cooling furnace because the content of ash is small and problems caused by the ash do not occur even if blown into the cooling furnace. That is, by introducing a carbonaceous raw material containing one or both of biomass and waste plastic into a cooling furnace, the reducing gas can be cooled and the production of reducing gas can be increased without causing the problem of ash.
[0039]
The solid reduced iron 3 containing a sulfur content produced in the present invention is particularly preferably put into a blast furnace. As mentioned above, since the blast furnace itself has a desulfurization function, even if sulfur is contained in the charged reduced iron, the sulfur content of pig iron produced in the blast furnace is very small. . Therefore, even if it is the reduced iron containing the sulfur content manufactured by this invention, it can be used as an iron-making raw material without any problem. Moreover, since it is set as the raw material charged in the blast furnace, as described in Patent Document 3, the metallization rate in the reduction furnace (amount of metal iron / total amount of iron in iron ore × 100 (%)) is 90% or more. There is no need. In the present invention, the metallization rate is preferably 40 to 80%.
[0040]
Moreover, the reducing agent which reduces iron ore in a blast furnace is coke, and expensive caking coal is used as coal for coke production, and the usage rate of cheap steam coal is limited. On the other hand, it is possible to use only cheap coal for coal gasification direct reduction iron making. Therefore, it becomes possible to reduce the cost of the coal used for iron making as a whole by charging the reduced iron produced by the coal gasification reduction steel making of the present invention into the blast furnace.
[0041]
It is particularly preferable that the desulfurized reducing gas produced in the present invention is used for hydrogen gas production and / or combined power generation. Since the sulfur content in the reducing gas is low, it can be used for hydrogen gas production or combined power generation as it is without passing through the desulfurization facility. Also, most of the water vapor is removed during the cooling process, and the CO in the reducing gas is passed through the decarbonator.2Removed, CO and H2It can be set as the reducing gas which has as a main component. The reducing gas having such a component is suitable as a gas used for hydrogen gas production and / or combined power generation.
[0042]
In the present invention, water and / or water vapor is added to the desulfurized reducing gas, and the sensible heat of the reducing gas is used as a heat source to convert the CO gas in the reducing gas to H.2Gas and CO2Reformed into gas and the CO2It is preferable to produce hydrogen gas by absorbing and separating the gas.
[0043]
  The desulfurized reducing gas isshaftWhen it is at a high temperature of about 400 ° C. or higher when discharged from the furnace 4 and dust is collected by the dust collector 6, if water or steam is added in the shift reactor 24, the sensible heat of the reducing gas is used as a heat source. Utilizing it, a shift reaction is caused by catalytic reaction, and CO gas in the reducing gas is converted to H.2Gas and CO2It can be reformed to gas. Next, the reducing gas is cooled by the heat recovery device 5, and further passed through the decarboxylation device 9 to obtain CO2If the gas is absorbed and separated, hydrogen gas can be produced as a result. CO in reducing gas after iron ore reduction2Concentration is 20% or more, and CO after shift reaction.2Has a high concentration of 50% or more, so CO2 is highly efficient by the amine absorption method.2Separation is possible. As the heat necessary for the regeneration of the absorbing liquid, low-pressure steam generated from heat recovery of the process or low-pressure steam generated by burning municipal waste or the like can be used.
[0044]
The hydrogen gas produced in this manner can be used as it is as a reducing gas for heat treatment of steel products and as a raw material for fuel cells in steelworks. It is also possible to compress hydrogen gas and use it for combined power generation. Even when the shift reaction is not performed, the gas can be compressed and used for combined power generation.
[0045]
  That is,shaftThe reducing gas discharged from the furnace can be used for hydrogen production or combined power generation after shift reaction-decarboxylation of the reducing gas, method for combined power generation after decarboxylation of the reducing gas, reduction Any of the methods using the property gas as it is for combined power generation can be employed. of course,shaftA part or all of the reducing gas discharged from the furnace 4 is returned to the cooling furnace 13 to cool the reducing gas, and againshaftIt may be used as a reducing gas in the furnace 4.
[0046]
  In the present invention, a reducing gas produced by gasifying a carbonaceous raw materialshaftUsed to reduce iron ore in the furnace, and then used for hydrogen gas production and combined power generation. Therefore, it is possible to share a reducing gas heat recovery device, a dust collector, and the like. Therefore, it is possible to efficiently use the incidental facilities as compared to facilities that separately implement reduced iron production and combined power generation. In particular, for a coal gasifier with a high capital investment, the capital investment per reducing gas production volume decreases as the reducing gas production capacity increases. Therefore, compared to the case of separately constructing a coal gasification furnace for reduced iron making and combined power generation, the present invention for performing both reduced iron manufacturing and combined power generation using one larger scale coal gasification furnace, Overall capital investment efficiency can be improved.
[0047]
As described above, in the present invention, reduced iron, hydrogen, and electric power can be efficiently co-produced from a carbonaceous resource mainly composed of coal.
[0048]
【Example】
  As shown in FIG.,Reduced iron (DRI) was produced using a naphtho type furnace. The reducing gas 11 was produced using a two-stage gasification furnace having a gasification furnace 12 and a cooling furnace 13. Pulverized coal 0.67 ton / t-DRI and oxygen 560 Nm obtained by pulverizing Indonesian subbituminous coal to an average particle size of 50 μm in the lower gasifier 12Three/ T-DRI was introduced and gasified by partial combustion at 1500 ° C. and 5 ata. Furthermore, 0.3 ton / t-DRI of biomass (construction waste material chip) crushed to 5 mm or less in high-temperature reducing gas having reached 1500 ° C. in the upper cooling furnace 13 is cooled to 1000 ° C. and thermally decomposed. As a result, the amount of reducing gas produced was increased. It is possible to cover 20-30% of the reducing gas with carbon-neutral biomass or waste plastic. 35 g / Nm in reducing gasThreeOf carbon solids was present, but the cyclone 14 gave 5 g / Nm.ThreeAfter removing the dust belowshaftThe furnace 4 was charged.
[0049]
  shaftIn the furnace 4, conditions such as a reducing gas amount and a reducing gas temperature were set so that a metallization rate (amount of metallic iron / total iron amount in iron ore × 100 (%)) was 80%. The purpose of the reduced iron 3 is to be charged into the blast furnace together with the sintered ore and used as a raw material for the hot metal, so that the reduction rate of 60 to 90% can sufficiently achieve the object.
[0050]
  Amount of reducing gas,shaftTable 1 shows the gas properties and temperatures at the furnace inlet and outlet.
[0051]
[Table 1]
Figure 0004250472
[0052]
  shaftH in the reducing gas at the furnace inlet2S contained 520ppm (COS was 20ppm)shaftH after the dust removal device at the furnace outlet2S was reduced to 30 ppm (COS remained unchanged). On the other hand, the S content that was extremely small in iron ore 2 rose to 0.15 mass% in the reduced iron 3, and it was confirmed that the S content in the reducing gas was transferred to the reduced iron. . Usually, the required level of the market for the S content in the reduced iron is about 0.015% by mass. However, in this example, the reduced iron was used in a blast furnace having a desulfurization function, so there was no problem. It was available. In this example,shaftSince the gas temperature at the furnace outlet was set to a temperature of 420 ° C., H in the reducing gas2S reacts with reduced iron, and sulfur content moves from reducing gas to reduced iron.
[0053]
  still,shaftThe S concentration in the dust obtained from the dust collector 6 after the furnace was 0.3% by mass.shaftSince the temperature of 400 ° C. or higher was maintained even after leaving the furnace 4, the iron powder in the reducing gas and the residual H2It is determined that the reaction with S continued.
[0054]
  shaftThe reducing gas 11 after being discharged from the furnace 4 isshaftAbout 1/3 of the latent heat held in front of the furnaceshaftIt was only consumed in the furnace and kept sufficiently high energy. Here, the reducing gas 11 is converted into a shift reaction (CO + H2O → H2+ CO2The reducing gas 11 is collected by the dust collector 6 and then introduced into the shift reactor 24 without cooling, where hydrogen and carbon dioxide gas are used. The hydrogen was separated and utilized. As a result, hydrogen is 1400 NmThree/ T-DRI, CO2Was able to recover 2.4 ton / t-DRI. The shift reaction causes CO2The concentration is as high as over 50%, and the absorption efficiency by the amine method is CO.2Compared to the boiler exhaust gas with a concentration of about 10%, it was improved by 5 to 10%. Future CO2As the development of immobilization technology progressed, it was found that it could become a promising technology for global warming countermeasures. The separated hydrogen gas 25 was used as a heat treatment gas for an ironworks. Furthermore, it was confirmed that combined power generation is possible by pressurization, and that it can be used as iron ore reducing gas by circulating in this process.
[0055]
  Next, as a comparative example,shaftThe reducing gas temperature at the furnace outlet was set to 550 ° C. Other conditions are the same as in the above embodiment.shaftH in the reducing gas after the dust collector at the furnace outlet2S was reduced only to 200 ppm (COS remained unchanged). On the other hand, the amount of S that was extremely small in iron ore increased to 0.08% by mass in the reduced iron, and it was confirmed that a part of S in the reducing gas was transferred to the reduced iron. .shaftSince the sulfur content in the reducing gas discharged from the furnace is not sufficiently reduced, it cannot be used as hydrogen gas or for combined power generation as it is. On the other hand, since the sulfur content in the reduced iron is high, it can be used as a raw material for charging a blast furnace, but it is difficult to use it as a main raw material for electric furnace iron making.
[0056]
【The invention's effect】
According to the present invention, reduced iron, hydrogen, and electric power can be efficiently co-produced, so that the capital investment efficiency can be improved and the coal gasification direct reduction iron making and the coal gasification combined power generation can be commercialized.
[0057]
The present invention can also eliminate the need for installation of a desulfurization facility in coal gasification direct reduction iron making or coal gasification combined power generation.
[0058]
Furthermore, the present invention can use biomass or waste plastic as an alternative to coal to reduce carbon dioxide emissions.
[Brief description of the drawings]
FIG. 1 is a diagram showing an efficient utilization method of carbonaceous resources according to the present invention.
FIG. 2 is a diagram showing a conventional method for producing reduced iron.
FIG. 3 is a diagram showing a conventional method for producing reduced iron.
FIG. 4 is a diagram showing a conventional method for producing reduced iron.
FIG. 5 is a diagram illustrating a conventional coal gasification combined power generation method.
[Explanation of symbols]
  1 Reducing gas generator
  2 Iron ore
  3 Reduced iron
  4Shaft furnace
  5 Heat recovery device
  6 Dust collector
  7 Gas cooling device
  8 Compressor
  9 Decarbonizer
10 Gas heating furnace
11 Reducing gas
12 Coal gasifier
13 Cooling furnace
14 Cyclone
15 Carbonaceous raw material (coal)
16 Oxygen
17 Water vapor
18 Coal humidity control equipment
19 Gas cleaning and cooling device
20, 21 Desulfurization equipment
22 Power generator
23 Electricity
24 shift reactor
25 Hydrogen gas
26 Carbonaceous material
27 Exhaust gas from outside the system

Claims (8)

石炭に加えてバイオマスと廃プラスチックの一方若しくは両方を含む炭素質原料、又は、石炭を酸素により部分燃焼させて還元性ガスを製造し、該還元性ガスを冷却した後、冷却後の700〜900℃の還元性ガスを鉄鉱石が充填されているシャフト炉に送り込み、該還元性ガスが該シャフト炉内を上昇する過程で、該還元性ガスと該鉄鉱石を該シャフト炉中で接触させて鉄鉱石を還元し、硫黄分を0.14〜1.4質量%の範囲で含有し、金属鉄を含む固体の還元鉄を製造すると共に、該還元性ガスを脱硫して該シャフト炉から400〜500℃の還元性ガスを排出して、脱硫された還元性ガスを製造することを特徴とする高炉装入原料用還元鉄及び還元性ガスの製造方法。A carbonaceous raw material containing one or both of biomass and waste plastic in addition to coal, or a coal is partially burned with oxygen to produce a reducing gas, and after cooling the reducing gas, 700 to 900 after cooling A reducing gas at 0 ° C. is fed into a shaft furnace filled with iron ore, and the reducing gas and the iron ore are brought into contact with each other in the shaft furnace in a process in which the reducing gas rises in the shaft furnace. The iron ore is reduced, and sulfur is contained in the range of 0.14 to 1.4% by mass to produce solid reduced iron containing metallic iron, and the reducing gas is desulfurized to remove 400 from the shaft furnace. A method for producing reduced iron for a blast furnace charge and a reducing gas, wherein a reducing gas at ˜500 ° C. is discharged to produce a desulfurized reducing gas. 前記硫黄分を含有する固体の還元鉄の金属化率を40〜80%とすることを特徴とする請求項1記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。  The method for producing reduced iron and reducing gas for a blast furnace charge according to claim 1, wherein the metallization ratio of the solid reduced iron containing sulfur is 40 to 80%. 前記シャフト炉から排出された還元性ガスと、該還元性ガスに同伴して排出された鉄鉱石および還元鉄の硫黄分を含有する微粉とを分離し、更に脱硫された還元性ガスとすることを特徴とする請求項1又は2に記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。  Separating the reducing gas discharged from the shaft furnace from the iron ore discharged along with the reducing gas and the fine powder containing the sulfur content of the reduced iron, and further desulfurizing reducing gas. The method for producing reduced iron and reducing gas for a blast furnace charging raw material according to claim 1 or 2. 還元性ガスに含まれる硫黄分を還元鉄に移動することによって脱硫された還元性ガスを得ることを特徴とする請求項1乃至3のいずれかに記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。  The reduced iron for reducing the blast furnace charge according to any one of claims 1 to 3, wherein the reducing gas desulfurized by moving sulfur contained in the reducing gas to reduced iron is obtained. Gas production method. 前記還元性ガスを製造するガス化炉に引き続いて冷却炉を有し、バイオマスと廃プラスチックの一方又は両方を含む炭素質原料を冷却炉中に投入することを特徴とする請求項1乃至4のいずれかに記載の高炉装入原料用還元鉄及び還元性ガスの製造方法。  The gasification furnace for producing the reducing gas is followed by a cooling furnace, and a carbonaceous raw material containing one or both of biomass and waste plastic is introduced into the cooling furnace. The manufacturing method of the reduced iron for blast furnace charging raw materials in any one, and reducing gas. 請求項1乃至5のいずれかの方法に記載の前記硫黄分を含有する固体の還元鉄を、高炉に投入することを特徴とする還元鉄の利用方法。  A method for using reduced iron, characterized in that the solid reduced iron containing the sulfur content according to any one of claims 1 to 5 is charged into a blast furnace. 請求項1乃至6のいずれかの方法に記載の前記脱硫された還元性ガスを、水素ガス製造及び/又は複合発電に利用することを特徴とする還元性ガスの利用方法。  A method for using a reducing gas, wherein the desulfurized reducing gas according to any one of claims 1 to 6 is used for hydrogen gas production and / or combined power generation. 前記脱硫された還元性ガスに水及び/又は水蒸気を添加し、該還元性ガスの顕熱を熱源として利用して還元性ガス中のCOガスをH2ガスとCO2ガスに改質し、該CO2ガスを吸収分離することにより水素ガスを製造することを特徴とする請求項7に記載の還元性ガスの利用方法。Water and / or water vapor is added to the desulfurized reducing gas, and the sensible heat of the reducing gas is used as a heat source to reform the CO gas in the reducing gas into H 2 gas and CO 2 gas, The method for using a reducing gas according to claim 7, wherein hydrogen gas is produced by absorbing and separating the CO 2 gas.
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