JPH09100108A - Production of carbon monoxide gas - Google Patents
Production of carbon monoxide gasInfo
- Publication number
- JPH09100108A JPH09100108A JP7258347A JP25834795A JPH09100108A JP H09100108 A JPH09100108 A JP H09100108A JP 7258347 A JP7258347 A JP 7258347A JP 25834795 A JP25834795 A JP 25834795A JP H09100108 A JPH09100108 A JP H09100108A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- carbon monoxide
- raw material
- reverse shift
- monoxide gas
- 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
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 229910002091 carbon monoxide Inorganic materials 0.000 title claims abstract description 52
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 99
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 27
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims description 10
- 238000000034 method Methods 0.000 abstract description 8
- 238000010276 construction Methods 0.000 abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 5
- 239000000203 mixture Substances 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 239000000446 fuel Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000002407 reforming Methods 0.000 description 3
- 238000000629 steam reforming Methods 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 description 1
- 235000011054 acetic acid Nutrition 0.000 description 1
- 125000005396 acrylic acid ester group Chemical group 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
Landscapes
- Carbon And Carbon Compounds (AREA)
- Industrial Gases (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、一酸化炭素ガスの
製造方法に関し、詳しくは、水素ガスと炭酸ガスから一
酸化炭素ガスを製造する方法に関する。TECHNICAL FIELD The present invention relates to a method for producing carbon monoxide gas, and more particularly to a method for producing carbon monoxide gas from hydrogen gas and carbon dioxide gas.
【０００２】[0002]
【従来の技術】従来、脂肪酸、酢酸、蟻酸、アクリル
酸、アクリル酸エステル、ホスゲン、メタノール等のＣ
1化学の原料である一酸化炭素ガスは、天然ガス、製油
所オフガス（メタン、プロパン、ブタン等）、サフナ等
を原料とした水蒸気改質法、重質油を原料とした部分酸
化法、石炭から合成ガスを製造する石炭ガス化法、製鉄
所から発生する副生ガスから一酸化炭素ガスを分離・精
製する方法、およびメタノールから蟻酸メチル合成法を
利用したメタノール法等によって製造されることが知ら
れている。2. Description of the Related Art Conventionally, C such as fatty acid, acetic acid, formic acid, acrylic acid, acrylic acid ester, phosgene and methanol is used.
1 Chemistry of carbon monoxide gas as a raw material, natural gas, refinery off-gas (methane, propane, butane, etc.), steam reforming method using a raw material such Safuna, partial oxidation of heavy oil as a raw material, coal It can be produced by the coal gasification method of producing synthetic gas from coal, the method of separating and purifying carbon monoxide gas from the by-product gas generated from an iron mill, and the methanol method using the methyl formate synthesis method from methanol. Are known.
【０００３】特に、水蒸気改質法にあっては、改質炉、
水蒸気発生炉、シフト反応器、炭酸ガス分離装置、水蒸
気分離装置等からなる製造装置によって製造されるよう
になっている。Particularly in the steam reforming method, a reforming furnace,
It is manufactured by a manufacturing apparatus including a steam generation furnace, a shift reactor, a carbon dioxide gas separation device, a steam separation device, and the like.
【０００４】[0004]
【発明が解決しようとする課題】しかしながら、このよ
うな従来の一酸化炭素ガスの製造方法として、水蒸気改
質法にあっては、改質炉、水蒸気発生炉、シフト反応
器、炭酸ガス分離装置、水蒸気分離装置等が必要であっ
たため、製造装置の構造が複雑になってしまい、装置の
建設費が増大してしまう上にユーティリティの使用量も
多いため（改質炉や水蒸気発生炉の熱回収のための設備
が必要になるため）、一酸化炭素ガスの製造コストが増
大してしまうという問題があった。However, in the steam reforming method as such a conventional method for producing carbon monoxide gas, there are a reforming furnace, a steam generating furnace, a shift reactor, and a carbon dioxide gas separation device. Since a steam separator was required, the structure of the manufacturing equipment became complicated, the construction cost of the equipment increased, and the amount of utilities used was large (heat of the reforming furnace and steam generator). There is a problem that the production cost of carbon monoxide gas increases because the facility for recovery is required).
【０００５】そこで請求項１記載の発明は、簡易な装置
構成によって一酸化炭素ガスを製造するようにして、装
置の建設費およびユーティリティコストを低減すること
ができ、安価に一酸化炭素ガスを製造することができる
一酸化炭素ガスの製造方法を提供することを目的として
いる。Therefore, in the invention described in claim 1, the carbon monoxide gas can be produced with a simple device configuration, whereby the construction cost and utility cost of the device can be reduced, and the carbon monoxide gas can be produced inexpensively. It is an object of the present invention to provide a method for producing carbon monoxide gas that can be used.
【０００６】[0006]
【課題を解決するための手段】請求項１記載の発明は、
上記課題を解決するために、水素ガスと炭酸ガスを原料
とし、炭酸ガスと水素ガスの逆シフト反応によって一酸
化炭素ガスと未反応の水素ガスおよび炭酸ガスの混合ガ
スを生成する逆シフト反応工程と、該逆シフト反応工程
によって生成された一酸化炭素ガスと未反応の水素ガス
および炭酸ガスの混合ガスから一酸化炭素ガスのみを分
離する分離工程と、を含んでなることを特徴とするもの
である。According to the first aspect of the present invention,
In order to solve the above problems, a reverse shift reaction step in which hydrogen gas and carbon dioxide are used as raw materials and a mixed gas of carbon monoxide gas and unreacted hydrogen gas and carbon dioxide is generated by a reverse shift reaction of carbon dioxide and hydrogen gas. And a separation step of separating only carbon monoxide gas from a mixed gas of carbon monoxide gas generated by the reverse shift reaction step and unreacted hydrogen gas and carbon dioxide gas. Is.
【０００７】その場合、逆シフト反応工程において、逆
シフト反応触媒を充填した逆シフト反応炉でＨ2＋ＣＯ2
→ＣＯ＋Ｈ2Ｏの反応を行なうと、一酸化炭素ガスと水
が生成される。そして、生成ガスから水を分離した後
に、分離工程において一酸化炭素ガスと未反応の水素ガ
スおよび炭酸ガスの混合ガスから例えば、ＣＯＰＳＡ
（ＣＯ−Rressure Swing Adsorption）等の一酸化炭素
ガス分離装置によって一酸化炭素ガスを分離し、未反応
の水素ガスと炭酸ガスをリサイクルガスとして利用し、
余剰分を燃料として使用する。In that case, in the reverse shift reaction step, H 2 + CO 2 is stored in the reverse shift reaction furnace filled with the reverse shift reaction catalyst.
→ When the reaction of CO + H 2 O is performed, carbon monoxide gas and water are produced. Then, after separating the water from the generated gas, in the separation step, for example, COPSA is selected from the mixed gas of the carbon monoxide gas and the unreacted hydrogen gas and carbon dioxide gas.
Carbon monoxide gas is separated by a carbon monoxide gas separator such as (CO-Rressure Swing Adsorption), and unreacted hydrogen gas and carbon dioxide gas are used as recycle gas,
Use the surplus as fuel.
【０００８】このようにすれば、水素ガスと炭酸ガスが
比較的安価に入手できれば、製造装置を簡易な構成にし
て、製造装置の建設費およびユーティリティコストを低
減することができ、一酸化炭素ガスを安価に製造するこ
とができる。さらに、炭酸ガスを原料として有益な一酸
化炭素ガスを製造することができるので、地球の温暖化
の大きな原因となっている炭酸ガスの有効利用にも寄与
することができる。[0008] In this way, if hydrogen gas and carbon dioxide gas can be obtained at a relatively low cost, the manufacturing apparatus can be made to have a simple structure and the construction cost and utility cost of the manufacturing apparatus can be reduced. Can be manufactured at low cost. Furthermore, since carbon monoxide gas can be used as a raw material to produce useful carbon monoxide gas, it can contribute to effective use of carbon dioxide gas, which is a major cause of global warming.
【０００９】[0009]
【発明の実施の形態】以下、本発明の実施例を図面に基
づいて説明する。図１〜３は本発明に係る一酸化炭素ガ
スの製造方法を達成するための一酸化炭素ガスの製造装
置の一実施例を示す図である。図１に示す如く、原料の
水素ガスと炭酸ガスは、ＣＯＰＳＡ（ＣＯ−RressureSw
ing Adsorption）等の一酸化炭素分離装置に１からのオ
フガスと共に原料供給ライン２を通って逆シフト工程を
実施する逆シフト反応炉３内に入り、この逆シフト反応
炉３で一酸化炭素ガスと水蒸気とに改質される。なお、
この逆シフト反応炉３での反応条件は、温度が約420℃
に設定され、圧力が0.9Kg/cm2Gに設定される。また、こ
のときの反応は、吸熱反応であるため、外部から燃料を
焚き加熱する。Embodiments of the present invention will be described below with reference to the drawings. 1 to 3 are views showing an embodiment of a carbon monoxide gas production apparatus for achieving the carbon monoxide gas production method according to the present invention. As shown in Fig. 1, the hydrogen gas and carbon dioxide gas as the raw materials are COPSA (CO-RressureSw
ing Adsorption) and the like with the off gas from 1 through the raw material supply line 2 into the reverse shift reaction furnace 3 for performing the reverse shift process. It is reformed to steam. In addition,
The reaction condition in this reverse shift reactor 3 is that the temperature is about 420 ° C.
And the pressure is set to 0.9 Kg / cm 2 G. Further, since the reaction at this time is an endothermic reaction, the fuel is heated by heating the fuel from the outside.
【００１０】次いで、逆シフト反応炉３から出た生成ガ
スおよび未反応原料ガスの混合ガス（温度570℃、圧力
0.5Kg/cm2G）は、原料ガスを予熱した後、ドライヤヒー
タ４およびアフタークーラー５を経た後、ドレンセパレ
ータ６に入り、水分が除去された後、圧縮機７によって
温度40℃、圧力7.0Kg/cm2Gに昇圧された後、分離工程を
実施する一酸化炭素ガス分離装置１に送られる。Then, a mixed gas of the product gas and the unreacted raw material gas discharged from the reverse shift reactor 3 (temperature: 570 ° C., pressure:
0.5 Kg / cm 2 G), after preheating the raw material gas, after passing through the dryer heater 4 and the after-cooler 5, enters the drain separator 6 to remove water, and then the compressor 7 sets the temperature to 40 ° C. and the pressure to 7.0. After the pressure is increased to Kg / cm 2 G, it is sent to the carbon monoxide gas separation device 1 which carries out the separation step.
【００１１】この分離装置１では、一酸化炭素ガスとそ
の他のガスに分離され、一酸化炭素ガスはＣＯ圧縮機８
によって昇圧された後、脱湿ユニット９を経て製品とな
る。一方、一酸化炭素ガス分離装置１からのオフガスは
オフガスホルダー10を経た後、オフガスブロアー11によ
って逆シフト反応炉３にリサイクルされる。また、余剰
分の燃料は逆シフト反応炉３の上述した加熱用の燃料と
して利用される。In this separator 1, the carbon monoxide gas is separated into other gas, and the carbon monoxide gas is separated by the CO compressor 8
After the pressure is increased by, the product passes through the dehumidifying unit 9 and becomes a product. On the other hand, the off gas from the carbon monoxide gas separation device 1 passes through the off gas holder 10 and is then recycled to the reverse shift reactor 3 by the off gas blower 11. The surplus fuel is used as the heating fuel for the above-described reverse shift reactor 3.
【００１２】本実施例では、上述したような装置によっ
て、200Nm3/Hrの一酸化炭素ガスを製造した場合に、図
２、３に示す製造プロセスの物質収支（マテリアルバラ
ンス）から明らかなように、一酸化炭素ガス分離装置１
から分離された一酸化炭素ガスはかなりのレベルで製造
されることが分かった。このように本実施例では、水素
ガスと炭酸ガスを原料とし、逆シフト反応炉３を用い、
炭酸ガスと水素ガスの逆シフト反応によって一酸化炭素
ガスと未反応の水素ガスおよび炭酸ガスの混合ガスを生
成した後、一酸化炭素ガス分離装置１を用いて一酸化炭
素ガスと未反応の水素ガスおよび炭酸ガスの混合ガスか
ら一酸化炭素ガスのみを分離するようにしたため、水素
ガスと炭酸ガスが比較的安価に入手できれば、製造装置
を簡易な構成にして、製造装置の建設費およびユーティ
リティコストを低減することができ、一酸化炭素ガスを
安価に製造することができる。さらに、炭酸ガスを原料
として有益な一酸化炭素ガスを製造することができるの
で、地球の温暖化の大きな原因となっている炭酸ガスの
有効利用にも寄与することができる。In this example, when 200 Nm 3 / Hr carbon monoxide gas was produced by the above-mentioned apparatus, as is clear from the material balance of the production process shown in FIGS. , Carbon monoxide gas separator 1
It has been found that the carbon monoxide gas separated from is produced at significant levels. As described above, in the present embodiment, hydrogen gas and carbon dioxide gas are used as raw materials, the reverse shift reactor 3 is used,
After a mixed gas of carbon monoxide gas, unreacted hydrogen gas and carbon dioxide gas is generated by a reverse shift reaction of carbon dioxide gas and hydrogen gas, carbon monoxide gas and unreacted hydrogen are separated using the carbon monoxide gas separation device 1. Since only carbon monoxide gas is separated from the mixed gas of carbon dioxide and carbon dioxide, if hydrogen gas and carbon dioxide can be obtained at a relatively low cost, the production equipment will have a simple structure, and the construction cost and utility cost of the production equipment will be reduced. Can be reduced, and carbon monoxide gas can be produced at low cost. Furthermore, since carbon monoxide gas can be used as a raw material to produce useful carbon monoxide gas, it can contribute to effective use of carbon dioxide gas, which is a major cause of global warming.
【００１３】[0013]
【発明の効果】請求項１記載の発明によれば、水素ガス
と炭酸ガスが比較的安価に入手できれば、製造装置を簡
易な構成にして、製造装置の建設費およびユーティリテ
ィコストを低減することができ、一酸化炭素ガスを安価
に製造することができる。さらに、炭酸ガスを原料とし
て有益な一酸化炭素ガスを製造することができるので、
地球の温暖化の大きな原因となっている炭酸ガスの有効
利用にも寄与することができる。According to the first aspect of the present invention, if hydrogen gas and carbon dioxide gas can be obtained at a relatively low cost, the manufacturing apparatus can have a simple structure and the construction cost and utility cost of the manufacturing apparatus can be reduced. Therefore, the carbon monoxide gas can be produced at a low cost. Furthermore, since carbon monoxide gas can be produced as a useful carbon monoxide gas,
It can also contribute to effective use of carbon dioxide, which is a major cause of global warming.
【図１】本発明に係る一酸化炭素ガスの製造方法の一実
施例を示す図であり、その製造方法を達成するための製
造装置の一実施例を示す図である。FIG. 1 is a diagram showing an embodiment of a method for producing carbon monoxide gas according to the present invention, and is a diagram showing an embodiment of a production apparatus for achieving the production method.
【図２】一実施例の一酸化炭素ガスの物質収支を示す図
である。FIG. 2 is a diagram showing a mass balance of carbon monoxide gas in one example.
【図３】一実施例の一酸化炭素ガスの物質収支を示す図
である。FIG. 3 is a diagram showing a mass balance of carbon monoxide gas in one example.
１ 一酸化炭素ガス分離装置 ２ 原料供給ライン ３ 逆シフト反応炉 ４ ドライヤーヒータ ５ アフタークーラー ６ ドレンセパレータ ７ 圧縮機 ８ ＣＯ圧縮機 ９ 脱湿ユニット 10 オフガスホルダー 11 オフガスブロアー 1 Carbon Monoxide Gas Separator 2 Raw Material Supply Line 3 Reverse Shift Reactor 4 Dryer Heater 5 After Cooler 6 Drain Separator 7 Compressor 8 CO Compressor 9 Dehumidifying Unit 10 Off Gas Holder 11 Off Gas Blower
Claims (1)
と水素ガスの逆シフト反応によって一酸化炭素ガスと未
反応の水素ガスおよび炭酸ガスの混合ガスを生成する逆
シフト反応工程と、 該逆シフト反応工程によって生成された一酸化炭素ガス
と未反応の水素ガスおよび炭酸ガスの混合ガスから一酸
化炭素ガスのみを分離する分離工程と、を含んでなるこ
とを特徴とする一酸化炭素ガスの製造方法。1. A reverse shift reaction step in which hydrogen gas and carbon dioxide gas are used as raw materials and a mixed gas of carbon monoxide gas and unreacted hydrogen gas and carbon dioxide gas is generated by a reverse shift reaction of carbon dioxide gas and hydrogen gas, And a separation step of separating only carbon monoxide gas from a mixed gas of carbon monoxide gas produced by the reverse shift reaction step and unreacted hydrogen gas and carbon dioxide gas. Manufacturing method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7258347A JPH09100108A (en) | 1995-10-05 | 1995-10-05 | Production of carbon monoxide gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7258347A JPH09100108A (en) | 1995-10-05 | 1995-10-05 | Production of carbon monoxide gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09100108A true JPH09100108A (en) | 1997-04-15 |
Family
ID=17318986
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7258347A Pending JPH09100108A (en) | 1995-10-05 | 1995-10-05 | Production of carbon monoxide gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09100108A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000068146A1 (en) * | 1999-05-06 | 2000-11-16 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | On site carbon monoxide generator |
| US8946308B2 (en) | 2008-12-17 | 2015-02-03 | Saudi Basic Industries Corporation | Process for increasing the carbon monoxide content of a syngas mixture |
| JP2023180568A (en) * | 2022-06-09 | 2023-12-21 | 株式会社神戸製鋼所 | Synthesis gas production system and synthesis gas production method |
| WO2024048423A1 (en) * | 2022-08-30 | 2024-03-07 | Ｊｆｅミネラル株式会社 | Circulating reduction system, iron ore reduction method, and blast furnace operation method |
| JP2024516224A (en) * | 2021-04-30 | 2024-04-12 | コベストロ、ドイチュラント、アクチエンゲゼルシャフト | Improved Sustainability in Polycarbonate Manufacturing |
| CN118110561A (en) * | 2024-04-30 | 2024-05-31 | 泰兴市华诚机电制造有限公司 | Tunnel construction safety guarantee cabin oxygen generation device and method |
| WO2025215458A1 (en) * | 2024-04-11 | 2025-10-16 | Arcelormittal | Ironmaking method and associated plant |
-
1995
- 1995-10-05 JP JP7258347A patent/JPH09100108A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000068146A1 (en) * | 1999-05-06 | 2000-11-16 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | On site carbon monoxide generator |
| US8946308B2 (en) | 2008-12-17 | 2015-02-03 | Saudi Basic Industries Corporation | Process for increasing the carbon monoxide content of a syngas mixture |
| US9249079B2 (en) | 2008-12-17 | 2016-02-02 | Saudi Basic Industries Corporation | Process for increasing the carbon monoxide content of a syngas mixture |
| JP2024516224A (en) * | 2021-04-30 | 2024-04-12 | コベストロ、ドイチュラント、アクチエンゲゼルシャフト | Improved Sustainability in Polycarbonate Manufacturing |
| JP2023180568A (en) * | 2022-06-09 | 2023-12-21 | 株式会社神戸製鋼所 | Synthesis gas production system and synthesis gas production method |
| WO2024048423A1 (en) * | 2022-08-30 | 2024-03-07 | Ｊｆｅミネラル株式会社 | Circulating reduction system, iron ore reduction method, and blast furnace operation method |
| JPWO2024048423A1 (en) * | 2022-08-30 | 2024-03-07 | ||
| WO2025215458A1 (en) * | 2024-04-11 | 2025-10-16 | Arcelormittal | Ironmaking method and associated plant |
| WO2025215401A1 (en) * | 2024-04-11 | 2025-10-16 | Arcelormittal | Ironmaking method and associated plant |
| CN118110561A (en) * | 2024-04-30 | 2024-05-31 | 泰兴市华诚机电制造有限公司 | Tunnel construction safety guarantee cabin oxygen generation device and method |
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