JP2003261301A - Method of producing hydrogen by steel making co- production - Google Patents
Method of producing hydrogen by steel making co- productionInfo
- Publication number
- JP2003261301A JP2003261301A JP2002062857A JP2002062857A JP2003261301A JP 2003261301 A JP2003261301 A JP 2003261301A JP 2002062857 A JP2002062857 A JP 2002062857A JP 2002062857 A JP2002062857 A JP 2002062857A JP 2003261301 A JP2003261301 A JP 2003261301A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- hydrogen
- blast furnace
- fuel
- coke oven
- 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
- 239000001257 hydrogen Substances 0.000 title claims abstract description 38
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 38
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 12
- 238000009628 steelmaking Methods 0.000 title abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 64
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000000571 coke Substances 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000001301 oxygen Substances 0.000 claims abstract description 8
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 8
- 238000007664 blowing Methods 0.000 claims abstract description 7
- 238000005338 heat storage Methods 0.000 claims description 7
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 239000003245 coal Substances 0.000 abstract description 19
- 239000002737 fuel gas Substances 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 230000001172 regenerating effect Effects 0.000 abstract description 2
- 239000000446 fuel Substances 0.000 description 34
- 238000002309 gasification Methods 0.000 description 21
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 13
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 10
- 229910052742 iron Inorganic materials 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910000805 Pig iron Inorganic materials 0.000 description 4
- 239000003345 natural gas Substances 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Landscapes
- Hydrogen, Water And Hydrids (AREA)
- Industrial Gases (AREA)
Abstract
Description
【０００１】[0001]
【発明が属する技術分野】本発明は、石炭、メタン等の
燃料をガス化して、水素を製造する方法に関する。水素
は、一酸化炭素ＣＯとの化学合成にて、ジメチルエーテ
ル（ＣＨ3ＯＣＨ3）等の合成燃料を製造するための原料
として重要である。
３ＣＯ＋３Ｈ2→ＣＨ3ＯＣＨ3＋ＣＯ2
また水素は燃料電池用燃料としても、重要で価値の高い
エネルギーである。TECHNICAL FIELD The present invention relates to a method for producing hydrogen by gasifying a fuel such as coal or methane. Hydrogen is important as a raw material for producing synthetic fuel such as dimethyl ether (CH3OCH3) in the chemical synthesis with carbon monoxide CO. 3CO + 3H2 → CH3OCH3 + CO2 Hydrogen is an important and valuable energy as a fuel for fuel cells.
【０００２】[0002]
【従来の技術】従来のメタン等の燃料をガス化して、水
素を製造する方法では、専用のガス化炉設備が必要であ
る。 ガス化用燃料として、通常は天然ガスが利用され
ることが多いが、天然ガスが高価な燃料であり、水素製
造費用は安く出来ない。安い燃料として、天然ガスの替
わりにコークス炉発生ガスを使う方法もあるが、コーク
ス炉発生ガス中の硫化物等の不純物を除去しておく前処
理をしなければならない。そうでないと、ガス化触媒を
劣化させたり、利用先の燃料電池の寿命に問題が出てく
る。またコークス炉発生ガス中には、炭化水素ガスが３
６％程度しか含まれず、残りは殆ど水素である。 従っ
てガス化生産効率が低下してしまい、設備費用がかかる
という問題がある。ガス化用燃料として、安価な石炭を
使用する石炭ガス化方式においては、ガス化の設備費用
が高いことで、あまりこの方法は利用されていない。石
炭ガス化するためには、高温雰囲気にする必要があり、
冷ガス効率が７８％程度と低くなる欠点がある。冷ガス
効率とは、（生成ガスの発熱量）／（原料の総発熱量）
の比率である。冷ガス効率が低い要因は、ガス化炉から
排出される発生ガス温度が高く、その大部分が、蒸気回
収の方法でしか熱回収出来ないからである。その他に、
炉を維持するために、炉壁を冷却するときの熱損失も大
きい。ガス化反応率が高くなく、未反応のチャーが発生
し、それをまたガス化炉に循環する過程で、無視出来な
い熱損失がある。石炭ガス化生成ガスでは、Ｈ2／ＣＯ
の比率が０．６と低く、一酸化炭素ＣＯを次の反応式に
て水素に転換する必要が出てくる。
水素転換反応式：Ｈ2Ｏ＋ＣＯ→Ｈ2＋ＣＯ2＋１０kcal
／mol
これは発熱反応であり、その分のエネルギーロスと、二
酸化炭素ＣＯ2排出増があって、好ましくはない。また
ジメチルエーテルの合成に、この石炭ガス化生成ガスを
利用する場合にも、問題は多い。ジメチルエーテルの合
成には、Ｈ2／ＣＯの比率が１の原料ガスが適している
が、石炭ガス化生成ガスでは、水素が不足している。メ
タノール合成では、Ｈ2／ＣＯの比率が２の原料ガスが
適しているので、さらに水素が不足する。従って石炭ガ
ス化にて合成燃料を製造する場合には、エネルギーロス
とＣＯ2排出増の問題がある。 海外の石炭山元で石炭
ガス化にて、安い合成燃料を製造して、それを輸入する
ことで自国のＣＯ2排出増は免れても、山元でのＣＯ2排
出増の問題がより大きい。地球規模で見て、豊富な石炭
資源から石油代替燃料を製造することは、重要な課題で
はあるが、この環境問題も無視出来ない。2. Description of the Related Art The conventional method for producing hydrogen by gasifying a fuel such as methane requires a dedicated gasification furnace facility. Natural gas is often used as a gasification fuel, but natural gas is an expensive fuel and the hydrogen production cost cannot be reduced. As a cheap fuel, there is a method of using coke oven generated gas instead of natural gas, but it is necessary to perform a pretreatment to remove impurities such as sulfides in the coke oven generated gas. Otherwise, the gasification catalyst will be deteriorated and the life of the fuel cell at the destination will be problematic. In addition, the hydrocarbon gas generated in the coke oven gas is 3
It contains only about 6%, and the rest is mostly hydrogen. Therefore, there is a problem that the gasification production efficiency is reduced and the equipment cost is increased. In a coal gasification system that uses cheap coal as a gasification fuel, this method is not often used because of high gasification equipment costs. In order to gasify coal, it is necessary to create a high temperature atmosphere,
There is a drawback that the cold gas efficiency is as low as about 78%. Cold gas efficiency is (calorific value of generated gas) / (total calorific value of raw materials)
Is the ratio of. The reason for the low cold gas efficiency is that the temperature of the generated gas discharged from the gasification furnace is high and most of the heat can be recovered only by the steam recovery method. Other,
Heat loss is also large when cooling the furnace wall to maintain the furnace. The gasification reaction rate is not high, unreacted char is generated, and there is a considerable heat loss in the process of circulating it to the gasifier. In the case of coal gasification product gas, H2 / CO
The ratio is as low as 0.6, and it becomes necessary to convert carbon monoxide CO into hydrogen by the following reaction formula. Hydrogen conversion reaction formula: H2O + CO → H2 + CO2 + 10kcal
/ Mol This is an exothermic reaction, and there is energy loss and an increase in carbon dioxide CO2 emission, which is not preferable. Also, there are many problems when using this coal gasification product gas for the synthesis of dimethyl ether. A raw material gas having an H2 / CO ratio of 1 is suitable for the synthesis of dimethyl ether, but the coal gasification product gas lacks hydrogen. In the methanol synthesis, a raw material gas having an H2 / CO ratio of 2 is suitable, so that hydrogen is further insufficient. Therefore, when a synthetic fuel is produced by coal gasification, there are problems of energy loss and increased CO2 emission. Coal gasification at overseas coal hills produces cheap synthetic fuels and then imports them to avoid CO2 emission increase in their own country, but the problem of CO2 emission increase at the mountain is larger. On a global scale, producing oil alternative fuels from abundant coal resources is an important issue, but this environmental issue cannot be ignored.
【０００３】[0003]
【発明が解決しようとする課題】本発明の目的とすると
ころは、豊富な石炭資源から、合成燃料用原料ガスある
いは燃料電池用水素を製造することにおいて、その製造
工程のエネルギーロスを最小にする方法を提供すること
である。その課題のポイントは、ガス化生成ガス中の水
素組成を高くすることである。SUMMARY OF THE INVENTION An object of the present invention is to minimize energy loss in the production process in producing raw material gas for synthetic fuel or hydrogen for fuel cell from abundant coal resources. Is to provide a method. The point of the problem is to increase the hydrogen composition in the gasification product gas.
【０００４】[0004]
【課題を解決するための手段】１．エネルギーロスの少
ないガス化方法として、製鉄高炉に酸素送風を行い、水
素の豊富なメタンを含有する燃料ガスを高炉羽口（３）
に吹き込むことを特徴とする水素製造方法である。
２．さらにコークス炉発生ガスは、製鉄コンビナートに
て、安価に入手出来るので、これを高炉羽口（３）に吹
き込むことを特徴とする水素製造方法である。
３．さらにコークス炉発生ガスを高炉羽口（３）に吹き
込む前に、蓄熱式熱交換器（２）にて、加熱しておくこ
とを特徴とする水素製造方法である。[Means for Solving the Problems] 1. As a gasification method with less energy loss, oxygen is blown into the steelmaking blast furnace to supply the fuel gas containing hydrogen-rich methane to the blast furnace tuyeres (3).
The method for producing hydrogen is characterized in that 2. Further, the coke oven gas can be obtained at a low cost in an iron-making complex, so that the gas is blown into the blast furnace tuyere (3), which is a hydrogen production method. 3. Furthermore, the hydrogen production method is characterized in that the coke oven-generated gas is heated in the heat storage heat exchanger (2) before being blown into the blast furnace tuyere (3).
【０００５】[0005]
【実施例】図１は、本発明の一実施例を示すものであ
る。現在の製鉄高炉（１）は、本来石炭およびコークス
のガス化炉としての機能を持っている。コークスの他
に、羽口（３）から微粉炭、タール等の燃料も炉内に吹
き込まれている。製鉄高炉（１）での、ガス化としての
特徴は、２３００℃という高温雰囲気にてガス化を行う
ので、ガス化反応能率が高いことである。従って未反応
チャーの発生が少ないという特徴がある。もっと大きい
特徴は、炉内の高温生成ガスは、炉内充填物と熱交換す
ることで、エネルギーロスが小さいことである。製鉄の
みに、必要最低限の燃料以上に高炉に投入する燃料を過
剰投入燃料と称する。 この過剰投入燃料に対する冷ガ
ス効率は、１００％近い。過剰投入燃料に対し、炉内温
度が過大にならないように、水蒸気等の冷却材を吹き込
む。 これは下記の吸熱反応にて、エネルギーロスな
く、高炉副生ガスの発熱量を向上で出来る。
Ｃ＋Ｈ2Ｏ→Ｈ2＋ＣＯ−２８．２kcal/mol
高炉にも下部炉壁、及び炉底部の冷却損失があるが、そ
の冷却損失量は、製鉄コプロダクションしても増加する
ことはなく、従来並である。この熱損失は、製鉄用に必
要最小限の燃料に含まれており、過剰投入燃料に対する
熱損失は、非常に小さい。酸素濃度９５％以上高くし
て、多量燃料と水蒸気を高炉羽口（３）に吹き込めば過
剰投入燃料量を大きく出来る。 これによってＮ2成分
も微量となり、ＣＯ、Ｈ2を主成分とする発熱量の高い
発生ガスが得られる。FIG. 1 shows an embodiment of the present invention. The current steelmaking blast furnace (1) originally has a function as a gasifier for coal and coke. In addition to coke, fuel such as pulverized coal and tar is also blown into the furnace from the tuyere (3). A feature of gasification in the steelmaking blast furnace (1) is that the gasification reaction efficiency is high because the gasification is performed in a high temperature atmosphere of 2300 ° C. Therefore, there is a characteristic that the generation of unreacted char is small. A more significant feature is that the high-temperature product gas in the furnace exchanges heat with the filling in the furnace, resulting in a small energy loss. The fuel that is added to the blast furnace in excess of the minimum required fuel for only steelmaking is called excess input fuel. The cold gas efficiency for this excess input fuel is close to 100%. A coolant such as steam is blown into the excess fuel so that the temperature inside the furnace does not become excessive. This is due to the following endothermic reaction, which can improve the calorific value of the blast furnace byproduct gas without energy loss. C + H2O → H2 + CO-28.2kcal / mol The blast furnace also has a cooling loss in the lower furnace wall and the bottom of the furnace, but the cooling loss amount does not increase even in iron production co-production, and is the same level as before. This heat loss is contained in the minimum necessary fuel for iron making, and the heat loss for the excess input fuel is very small. If the oxygen concentration is increased to 95% or more and a large amount of fuel and water vapor are blown into the tuyere (3) of the blast furnace, the amount of excess input fuel can be increased. As a result, the amount of N2 component also becomes small, and a generated gas containing CO and H2 as the main components and having a high calorific value is obtained.
【０００６】ここで高炉羽口に吹き込む燃料を微粉炭だ
けにすると、Ｈ2／ＣＯの比率が０．６と低くなるの
で、コークス炉発生ガス３６０Ｎｍ3／ｔ−銑鉄と水蒸
気（ｃ）３００Ｎｍ3／ｔ−銑鉄とを高炉羽口（３）か
ら吹き込む。微粉炭吹き込み量（ｂ）は１５０kg／ｔ−
銑鉄におさえる。コークス炉発生ガス中には、メタンを
主とする炭化水素ガスが約３６％程度含んでいる。 ま
たこのコークス炉発生ガスの事前処理には、精密な脱硫
処理は不要であり、現状の清浄化設備で十分である。吹
き込まれたメタンＣＨ4は、炉内の高御雰囲気におい
て、下記の反応によってＨ2を多量に発生するが、Ｈ2の
発生には（A）の吸熱反応が望ましい。
（A） ＣＨ4＋Ｈ2Ｏ→３Ｈ2＋ＣＯ−４９．３kcal／mol
（B） ＣＨ4＋１／２Ｏ2→２Ｈ2＋ＣＯ＋８．３kcal／m
ol
しかし、吸熱反応は熱を供給しないことには、反応が進
まない。そこでコークス炉発生ガスと水蒸気の混合ガス
６６０Ｎｍ3／ｔ−銑鉄を蓄熱式熱交換器（２）にて、
高温に加熱しておいてから、高炉羽口（３）に吹き込
む。この蓄熱式熱交換器（２）は、熱風炉と称されてお
り、一般的には送風空気を高温加熱するものであるが、
これを利用する。一方酸素ガスは、空気分離装置（４）
から供給され、酸素圧縮機（５）にて加圧して、予熱熱
交換器（６）にて、予熱されてから高炉羽口（３）に吹
き込まれる。以上の蓄熱式熱交換器（２）の熱源には、
隣接する高炉（１０）の同じく炉頂部発生ガス（ａ）
と、同炉頂部発生ガス（ａ）を燃料とするガスタービン
（１１）の排気ガスを利用することで、エネルギーが有
効利用出来る。ガスタービン（１１）の排気ガスの一部
は、追い焚きバーナー（１２）に燃料ガスと共に挿入さ
れて、高温燃焼し蓄熱式熱交換器（２）の熱源となる。
追い焚き燃料は、隣接高炉（１０）の発生ガス（ａ）が
利用される。If only pulverized coal is used as the fuel blown into the tuyere of the blast furnace, the H2 / CO ratio will be as low as 0.6, and therefore the coke oven generated gas will be 360 Nm3 / t-pig iron and steam (c) 300 Nm3 / t-. Blowing pig iron and blast furnace tuyere (3). Pulverized coal injection rate (b) is 150 kg / t-
Holds in pig iron. The coke oven generated gas contains about 36% of hydrocarbon gas mainly containing methane. Pretreatment of the gas generated from the coke oven does not require precise desulfurization treatment, and the current cleaning equipment is sufficient. The blown methane CH4 generates a large amount of H2 by the following reaction in a high-temperature atmosphere in the furnace, and the endothermic reaction (A) is desirable for the generation of H2. (A) CH4 + H2O → 3H2 + CO-49.3kcal / mol (B) CH4 + 1 / 2O2 → 2H2 + CO + 8.3kcal / m
However, the endothermic reaction does not proceed because it does not supply heat. Therefore, a mixed gas of coke oven generated gas and steam of 660 Nm3 / t-pig iron is stored in the heat storage heat exchanger (2),
It is heated to a high temperature and then blown into the blast furnace tuyere (3). This heat storage type heat exchanger (2) is called a hot stove and generally heats blast air at a high temperature.
Use this. On the other hand, oxygen gas is used in the air separation device (4).
It is supplied from the above, pressurized by the oxygen compressor (5), preheated by the preheat heat exchanger (6), and then blown into the blast furnace tuyere (3). The heat source of the above heat storage type heat exchanger (2) is
Gas generated at the same furnace top (a) of the adjacent blast furnace (10)
By using the exhaust gas of the gas turbine (11) that uses the gas (a) generated at the furnace top as a fuel, energy can be effectively used. A part of the exhaust gas of the gas turbine (11) is inserted into the reburning burner (12) together with the fuel gas, burns at high temperature, and becomes a heat source of the regenerative heat exchanger (2).
The gas (a) generated in the adjacent blast furnace (10) is used as the refueling fuel.
【０００７】なお隣接する高炉では、羽口吹き込み燃料
は微粉炭に限定しており、貴重なコークス炉生成ガスは
使用しない。以上によって、Ｎ2成分が微少で、Ｈ2／Ｃ
Ｏ比が１．５を越える発生ガスが得られる。 これを加
圧し、ガス清浄化する。 この清浄化されたガスを原料
として合成反応設備（１５）にて、ジメチルエーテル等
の合成燃料が得られる。この合成反応において、Ｎ2成
分が多いと反応生産性が低下する。またコークス炉発生
ガスには数量的に限界があり、不足する場合には、天然
ガスを補填するようにしておくことが望ましい。In the adjacent blast furnace, the tuyere-blown fuel is limited to pulverized coal, and precious coke oven generated gas is not used. Due to the above, the amount of N2 component is very small and H2 / C
A generated gas having an O ratio of more than 1.5 can be obtained. This is pressurized to clean the gas. A synthetic fuel such as dimethyl ether is obtained in the synthetic reaction facility (15) using this purified gas as a raw material. In this synthetic reaction, if the amount of N2 component is large, the reaction productivity decreases. In addition, there is a limit in the amount of gas generated from the coke oven, and if there is a shortage, it is desirable to supplement natural gas.
【０００８】図示はしていないが、同様にこの水素リッ
チな原料ガスから水素を製造出来る。この場合もＮ2成
分が微少でなければならない。Ｎ2成分を経済的に除去
することが出来ないからである。従って純度の高い酸素
を送風すべきである。なを製鉄の面では、Ｎ2成分が微
少であることは、還元能力の高い発生ガスを炉内に存在
することで、効率よく鉄鉱石を還元出来る。従って製鉄
生産性は現状以上に上げられるので、製鉄生産と蒸気の
エネルギー生産が両立することが出来る。Although not shown, hydrogen can be similarly produced from this hydrogen-rich source gas. Also in this case, the N2 component must be minute. This is because the N2 component cannot be removed economically. Therefore, high-purity oxygen should be blown. In terms of iron making, the small amount of N2 component means that the iron ore can be efficiently reduced by the presence of the generated gas with high reducing ability in the furnace. Therefore, since the productivity of steelmaking can be increased more than the current level, the production of iron and the energy production of steam can be compatible.
【０００９】[0009]
【発明の効果】製鉄コプロダクション方式により、過剰
投入燃料の冷ガス効率は、１００％に近い。このことに
より、非常に効率のよいガス化プロセスが得られる。９
０％以上の高濃度酸素を高炉羽口（３）に送風すること
で、Ｎ2成分の微少な原料ガスが製造できる。さらに、
メタンを含有する水素成分の高い燃料ガスを高炉羽口
（３）に吹き込むことによって、水素リッチな原料ガス
が製造出来る。このメタンを含有する水素リッチな燃料
ガスに、コークス炉発生ガスを使用することで安く水素
リッチな原料ガスが製造出来る。さらに、蓄熱式熱交換
器（２）にて、このメタンを含有する水素成分の高い燃
料ガスと水蒸気を高温に加熱しておくことで、高炉
（１）炉内に熱を与えて、水素が多く発生する吸熱反応
が進むようにすることで、水素リッチな原料ガスが製造
出来る。この水素リッチな原料ガスから、ジメチルエー
テル等の合成燃料が、経済的に大量製造出来る。また燃
料電池用の水素燃料も同様に経済的に大量製造出来る。According to the iron production co-production method, the cold gas efficiency of the excess input fuel is close to 100%. This results in a very efficient gasification process. 9
By blowing 0% or more of high-concentration oxygen to the blast furnace tuyere (3), a raw material gas containing a small amount of N2 component can be produced. further,
By blowing a fuel gas containing methane and having a high hydrogen component into the blast furnace tuyere (3), a hydrogen-rich source gas can be produced. By using the coke oven generated gas as the hydrogen-rich fuel gas containing methane, a cheap hydrogen-rich source gas can be produced. Further, by heating the fuel gas containing methane and having a high hydrogen component and steam in a heat storage type heat exchanger (2) to a high temperature, heat is applied to the blast furnace (1) and the hydrogen is By allowing the endothermic reactions that occur frequently to proceed, a hydrogen-rich source gas can be produced. From this hydrogen-rich source gas, synthetic fuel such as dimethyl ether can be economically mass-produced. Similarly, hydrogen fuel for fuel cells can be mass-produced economically.
【図１】図１は、本発明の実施例を示すもので、高炉製
鉄設備をガス化炉として利用する、製鉄コプロダクショ
ンによる水素製造方法を示す。FIG. 1 shows an embodiment of the present invention and shows a method for producing hydrogen by iron production co-production using a blast furnace iron making facility as a gasification furnace.
１ 高炉 ２ 蓄熱式熱交換器 ３ 高炉羽口 ４ 空気分離装置 ５ 酸素圧縮機 ６ 予熱熱交換器 ７ コークス炉 ８ コークス炉発生ガス圧縮機 ９ スクラバー除塵器 １０ 隣接高炉 １１ ガスタービン発電設備 １２ 追い焚きバーナー １３ 高炉炉頂発生ガス圧縮機 １４ ガス清浄化装置 １５ 合成反応設備 ａ 隣接高炉炉頂発生ガス ｂ 微粉炭吹き込み ｃ 水蒸気 1 blast furnace 2 heat storage type heat exchanger 3 blast furnace tuyeres 4 Air separation device 5 oxygen compressor 6 Preheating heat exchanger 7 coke oven 8 Coke oven generated gas compressor 9 Scrubber dust remover 10 adjacent blast furnace 11 Gas turbine power generation equipment 12 Reheating Burner 13 Blast furnace top gas compressor 14 Gas purifier 15 Synthetic reaction equipment a Adjacent blast furnace top gas b Pulverized coal injection c water vapor
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｃ１０Ｋ 3/06 Ｃ１０Ｋ 3/06 ─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. 7 Identification code FI theme code (reference) C10K 3/06 C10K 3/06
Claims (3)
濃度酸素を送風すること、高炉羽口（３）にメタンを含
有するガスを吹込むことを特徴とする水素製造方法1. A method for producing hydrogen, which comprises blowing high-concentration oxygen of 90% or more in the blast furnace iron-making method, and blowing a gas containing methane into the tuyere (3) of the blast furnace.
クス炉発生ガスを使用することを特徴とする水素製造方
法2. A method for producing hydrogen, wherein a coke oven-generated gas is used as the methane-containing gas according to claim 1.
るガスに水蒸気を加えて、蓄熱式熱交換設備（２）にて
加熱してから、高炉羽口（３）に吹込むことを特徴とす
る水素製造方法3. The method according to claim 1, wherein steam is added to the gas containing methane, the steam is heated in the heat storage heat exchange facility (2), and then the gas is blown into the tuyere (3) of the blast furnace. Hydrogen production method
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002062857A JP2003261301A (en) | 2002-03-08 | 2002-03-08 | Method of producing hydrogen by steel making co- production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002062857A JP2003261301A (en) | 2002-03-08 | 2002-03-08 | Method of producing hydrogen by steel making co- production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2003261301A true JP2003261301A (en) | 2003-09-16 |
Family
ID=28670687
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2002062857A Pending JP2003261301A (en) | 2002-03-08 | 2002-03-08 | Method of producing hydrogen by steel making co- production |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2003261301A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101351317B1 (en) | 2011-12-12 | 2014-01-15 | 재단법인 포항산업과학연구원 | A method for preparing reducing gas by using cokes oven gas and by-product gas from steel works |
| EP2719777A1 (en) * | 2012-10-12 | 2014-04-16 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Blast-furnace process with coke-oven gas injection and production plant for same |
| RU196737U1 (en) * | 2019-12-18 | 2020-03-13 | Федеральное государственное бюджетное учреждение науки Институт проблем химической физики Российской Академии наук (ФГБУН ИПХФ РАН) | DEVICE FOR PRODUCING HYDROGEN, CARBON MONOXIDE AND ETHYLENE |
| CN114829632A (en) * | 2019-12-26 | 2022-07-29 | 杰富意钢铁株式会社 | Method for operating a blast furnace and associated installation |
| CN115449573A (en) * | 2022-09-09 | 2022-12-09 | 云南曲靖钢铁集团呈钢钢铁有限公司 | Energy-saving environment-friendly blast furnace and blast furnace ironmaking process |
| CN117366546A (en) * | 2023-12-07 | 2024-01-09 | 四川铭能科技开发有限公司 | Gas turbine tail gas afterburning system based on hot-blast furnace |
-
2002
- 2002-03-08 JP JP2002062857A patent/JP2003261301A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101351317B1 (en) | 2011-12-12 | 2014-01-15 | 재단법인 포항산업과학연구원 | A method for preparing reducing gas by using cokes oven gas and by-product gas from steel works |
| EP2719777A1 (en) * | 2012-10-12 | 2014-04-16 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Blast-furnace process with coke-oven gas injection and production plant for same |
| RU196737U1 (en) * | 2019-12-18 | 2020-03-13 | Федеральное государственное бюджетное учреждение науки Институт проблем химической физики Российской Академии наук (ФГБУН ИПХФ РАН) | DEVICE FOR PRODUCING HYDROGEN, CARBON MONOXIDE AND ETHYLENE |
| CN114829632A (en) * | 2019-12-26 | 2022-07-29 | 杰富意钢铁株式会社 | Method for operating a blast furnace and associated installation |
| US12365953B2 (en) | 2019-12-26 | 2025-07-22 | Jfe Steel Corporation | Method of operating blast furnace and blast furnace ancillary facility |
| CN115449573A (en) * | 2022-09-09 | 2022-12-09 | 云南曲靖钢铁集团呈钢钢铁有限公司 | Energy-saving environment-friendly blast furnace and blast furnace ironmaking process |
| CN115449573B (en) * | 2022-09-09 | 2023-09-29 | 云南曲靖钢铁集团呈钢钢铁有限公司 | Energy-saving environment-friendly blast furnace and blast furnace ironmaking process |
| CN117366546A (en) * | 2023-12-07 | 2024-01-09 | 四川铭能科技开发有限公司 | Gas turbine tail gas afterburning system based on hot-blast furnace |
| CN117366546B (en) * | 2023-12-07 | 2024-03-19 | 四川铭能科技开发有限公司 | Gas turbine tail gas afterburning system based on hot-blast furnace |
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