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WO2013045257A1 - Procédé et dispositif de production d'hydrogène à partir de gaz provenant de la production de fonte - Google Patents

Procédé et dispositif de production d'hydrogène à partir de gaz provenant de la production de fonte Download PDF

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Publication number
WO2013045257A1
WO2013045257A1 PCT/EP2012/067601 EP2012067601W WO2013045257A1 WO 2013045257 A1 WO2013045257 A1 WO 2013045257A1 EP 2012067601 W EP2012067601 W EP 2012067601W WO 2013045257 A1 WO2013045257 A1 WO 2013045257A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
reduction
iron carriers
hydrogen
oxidic iron
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.)
Ceased
Application number
PCT/EP2012/067601
Other languages
German (de)
English (en)
Inventor
Robert Millner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
SIEMENS VAI METALS TECHNOLOGIES GmbH
Primetals Technologies Austria GmbH
Original Assignee
SIEMENS VAI METALS TECHNOLOGIES GmbH
Siemens VAI Metals Technologies GmbH Austria
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by SIEMENS VAI METALS TECHNOLOGIES GmbH, Siemens VAI Metals Technologies GmbH Austria filed Critical SIEMENS VAI METALS TECHNOLOGIES GmbH
Publication of WO2013045257A1 publication Critical patent/WO2013045257A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B7/00—Blast furnaces
    • C21B7/002—Evacuating and treating of exhaust gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
    • C21B13/002—Reduction of iron ores by passing through a heated column of carbon
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/24—Increasing the gas reduction potential of recycled exhaust gases by shift reactions
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
    • C21B2100/66—Heat exchange
    • Y—GENERAL 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2

Definitions

  • the present application relates to a process for the production of technically pure hydrogen, wherein a gas based on a gas resulting from the reduction of oxidic iron carriers from the group
  • Offgas from a fluidized-bed cascade in which finely particulate oxidic iron carriers are reduced countercurrently by a reducing gas
  • Topgas from a reduction shaft in which lumpy oxidic iron carriers are reduced by a reducing gas
  • the invention relates to a system with devices for carrying out this method.
  • Hydrogen is widely used in steelmaking, for example, as a fuel or as an inert gas - it is due to its high thermal conductivity and its reduction potential about the tempering of high-alloy steels. But even outside of the steelworks H 2 is widely used in the chemical or petrochemical industry. Typically, hydrogen is produced by steam reforming of natural gas or by electrolysis, which is quite expensive due to the high cost of natural gas and electrical energy. In some integrated steel plants, hydrogen is also produced from coke oven gas. However, coke oven gas does not accrue to all pig iron production plants, so that such a production route not always possible. For example, no coke accumulates during pig iron production route via the COREX ® or FINEX ® process.
  • Topgas from a reduction shaft in which lumpy oxidic iron carriers are reduced by a reducing gas
  • Excess gas from a melter gasifier or based on a mixture of two or more of the gases from this group is subjected to gas purification by means of PSA or VPSA, and the resulting product gas is at least partially subjected first to a membrane separation for the separation of hydrogen and then the resulting hydrogen-rich Gas is subjected to another gas purification by means of PSA or VPSA.
  • Offgas from a fluidized-bed cascade in which finely particulate oxidic iron carriers are reduced by a reducing gas
  • Topgas from a reduction shaft in which lumpy oxidic iron carriers are reduced by a reducing gas
  • the resulting product gas contains no water - dew point -100 ° C and therefore no condensation - and no higher hydrocarbons such as tar or PAH, since such substances are previously discharged with the tail gas of PSA or VPSA.
  • This facilitates further processing of this product gas via downstream compressors, diaphragms, pressure swing adsorption systems, as less equipment and less maintenance is required and longer service lives are possible.
  • the product gas obtained in the gas purification by means of PSA or VPSA is - at least in part - first subjected to a membrane separation for the separation of hydrogen.
  • PSA or VPSA This PSA or VPSA is also referred to below as Hydrogen PSA or Hydrogen VPSA.
  • a gas based on a ... gas from the group is meant that this gas consists of a gas from said group, or consists of a gas, which by pretreatment a gas is obtained from said group. Under reduction shaft and melter gasifier is not to understand a blast furnace.
  • the membrane separation takes place on one or more membranes which are suitable for separating hydrogen H 2 from carbon monoxide CO, nitrogen N 2 , argon Ar, carbon dioxide C0 2 and methane CH 4 .
  • membranes are known in the art and consist for example of hollow polymer fibers.
  • hydrogen H 2 penetrates from a gas mixture under a pressure, the membrane faster than the other components of the gas mixture.
  • the resulting hydrogen-rich gas is collected standing under a lower pressure.
  • a further gas purification of a hydrogen-rich gas thus obtained - which has a hydrogen content of about 90% by volume - by means of VPSA or PSA.
  • technically pure hydrogen having a hydrogen content greater than 99% by volume is obtained after this further gas purification step.
  • Such technically pure hydrogen obtained contains no impurities such as tar or hydrogen sulfide, and therefore requires no pretreatment before a final use. He is also absolutely dry.
  • the gas fed to the membrane separation and subsequently the PSA or VPSA gas contains no impurities and is absolutely dry - dew point about -100 ° C - needed in contrast to coke oven gas-derived hydrogen no further pretreatment.
  • the gas which is subjected to gas purification by means of PSA or VPSA is a dedusted gas from the abovementioned group of gases resulting from the reduction of oxidic iron carriers or a dedusted mixture of two or more gases from this group. Dedusting makes it easier to carry out PSA or VPSA.
  • the gas supplied to PSA or VPSA is cooled to a temperature in the range of 30-50 ° C, since in this temperature range the adsorption isotherms are most steep for efficient C0 2 removal, thus allowing the highest loading of C0 2 .
  • the gas which is present on a gas resulting from the reduction of oxidic iron carriers is from the group - top gas from an oxygen-blowing blast furnace,
  • Offgas from a fluidized-bed cascade in which finely particulate oxidic iron carriers are reduced countercurrently by a reducing gas
  • Topgas from a reduction shaft in which lumpy oxidic iron carriers are reduced by a reducing gas
  • Dusted gas can also be converted to CO shift.
  • the amount of recoverable hydrogen increases, thus producing carbon monoxide CO hydrogen H 2 . In this way, the amount of hydrogen generated can be increased.
  • vent gas In membrane separation for the separation of hydrogen, a so-called vent gas is applied to the membrane.
  • This vent gas contains, apart from hydrogen, the components of the product gas fed to the membrane separation - CO, N 2 , CO 2 , CH 4 .
  • this vent gas is the reducing gas of a fluidized bed cascade or a reduction shaft - preferably the fluidized-bed cascade or the reduction shaft, from which the gas used according to the invention for the production of technically pure hydrogen originates - supplied.
  • its reduction potential can be used;
  • detrimental components such as H 2 0 or C0 2 are due to the passage of the gas cleaning by PSA or VPSA not or only in low concentrations available.
  • Hydrogen PSA produces a tail gas.
  • This tail gas contains components such as CO and CH 4 with a usable for thermal utilization energy content.
  • this tail gas is the export gas of a fluidized bed cascade or a reduction shaft for the reduction of oxidic iron carriers - preferably the fluidized bed cascade or the reduction shaft for the reduction of oxidic iron carriers, from which according to the invention used for the production of technically pure hydrogen derived gas - fed.
  • its energy content can be used in a thermal utilization of such an export gas;
  • detrimental components such as H 2 0 or C0 2 are due to the passage of the gas cleaning by PSA or VPSA not or only in low concentrations available.
  • Another object of the invention is a system for carrying out a method according to the invention. Such a system includes
  • Reduction shaft for the reduction of lumpy oxidic iron carriers by a reducing gas
  • a first gas cleaning device for carrying out VPSA or PSA
  • a product gas supply line for supplying product gas from the first gas purification device for passing VPSA or PSA into the membrane separation device for separating hydrogen
  • a second gas cleaning device for carrying out PSA or VPSA
  • system is to be understood in this context that it is a plurality of devices cooperating in the sense of the invention.
  • the system contains, for example, the devices gas purification device, membrane separation device, raw gas line et cetera.
  • Offgas from a fluidized-bed cascade in which finely particulate oxidic iron carriers are reduced by a reducing gas
  • Topgas from a reduction shaft in which lumpy oxidic iron carriers are reduced by a reducing gas
  • the gas supply line comprises a device for carrying out a CO shift Con vertization
  • Offgas from a fluidized-bed cascade in which finely particulate oxidic iron carriers are reduced by a reducing gas
  • Topgas from a reduction shaft in which lumpy oxidic iron carriers are reduced by a reducing gas
  • a heat exchanger and / or a cooler is present in the gas supply line. After the CO shift conversion, aftercooling and, if appropriate, steam removal may take place before the gas purification is carried out by means of VPSA or PSA.
  • a Ventgas emanating from the membrane separation device opens into an opening into the fluidized bed cascade or the reduction shaft reducing gas supply line or into a line from which the reducing gas supply line.
  • the reduction potential of the vent gas can be used.
  • a tail gas line emanating from the hydrogen PSA or hydrogen VPSA discharges into an export gas discharge emanating from the fluidized-bed cascade or the reduction shaft.
  • the energy content of the tail gas can be used in a thermal utilization of such export gas.
  • FIG. 1 shows a system with FINEX ® CO shift reactor system for the production of technically pure hydrogen.
  • FIG. 2 shows a similar structure FINEX ® plant for the production of technically pure hydrogen, in which no CO shift reactor system is available.
  • FIG. 1 shows a FINEX ® plant can be reduced in the fine-particulate in a fluidized bed cascade 1 oxidic support iron in counterflow through a produced in a melter 2 reducing gas.
  • Offgas from the fluidized bed cascade 1 is via the gas supply line 3 of the first Gas cleaning device 4 for performing PSA for the purpose of removing C0 2 / H 2 0 supplied.
  • Reduction gas produced in the melter gasifier 2 is conducted via the reducing gas supply line 5 into the fluidized bed cascade.
  • the first gas cleaning device 4 for carrying out PSA is also supplied with excess gas from the melter gasifier 2 via the gas supply line 3.
  • the mixture of offgas and excess gas supplied via the gas supply line 3 is subjected to a gas purification in the gas purification device 4 for carrying out PSA, in which C0 2 and H 2 0 are separated off.
  • the resulting product gas is supplied via the product gas supply line 6 for supplying product gas from the gas purification device 4 for performing PSA under compression in the compressor 7 in the membrane separation device 8 for the separation of hydrogen.
  • this product gas is subjected to a membrane separation for the separation of hydrogen.
  • this hydrogen-rich gas in the second gas cleaning device 10 for performing PSA - also called hydrogen PSA - fed via crude gas line 9 (for conducting in the membrane separation device 8 for the separation of hydrogen resulting hydrogen-rich gas).
  • crude gas line 9 starts from the membrane separation device 8 for the separation of hydrogen and flows into the second gas purification device 10 for the implementation of PSA.
  • the off-gas leading branch of the gas supply line 3a is based on a dedusting device 1 1 for dedusting of the offgas - is shown a wet scrubber - from.
  • the surplus gas leading branch of the gas supply line 3b is based on a dedusting device 12 for dedusting excess gas - is shown a wet scrubber - from.
  • the gas supply line 3 contains a device for carrying out a CO shift conversion 13 and, viewed in the direction of hydrogen PSA, behind it a heat exchanger 14 and a cooler 15. After the CO shift conversion has taken place, aftercooling and, if appropriate, steam removal can take place before gas purification is performed by VPSA.
  • a steam supply line 16 opens into the gas supply line 3.
  • a Ventgastechnisch 17 emanating from the membrane separation device 8 opens into the pipe reduction gas from the melter carburetor derived pipe reduction gas line 22. This allows the reduction potential of the vent gas can be used.
  • a tail gas line 18 emanating from the hydrogen PSA 10 discharges into a dedusted off-gas from the fluidized-bed cascade 1, leading off export gas discharge 19.
  • the energy content of the tail gas can thus be utilized in a thermal utilization of such an export gas.
  • a compressor 20 is present between membrane separation device 8 and hydrogen PSA.
  • a compressor 21 is provided, so that the PSA of the first gas cleaning device 4 compressed gas is supplied.
  • the two compressors 20 and 7 are optionally available; they are selected depending on the prevailing at the membrane separation device 8 pressure.
  • Product gas from the PSA of the first gas purification device 4 can be fed into the vent gas line 17 as required and thus added to the reduction gas system.
  • Figure 2 shows an analog system, in which, however, no device for performing a CO shift conversion 13 and corresponding no heat exchanger 14, no cooler 15, no steam supply line 16 are present in the gas supply line.
  • no device for performing a CO shift conversion 13 and corresponding no heat exchanger 14, no cooler 15, no steam supply line 16 are present in the gas supply line.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de production d'hydrogène techniquement pur, selon lequel on soumet à une purification par adsorption PSA ou VPSA un gaz à base d'un gaz provenant de la réduction de matériaux ferrifères oxydés et appartenant au groupe comprenant : le gaz brûlé provenant d'un haut fourneau à soufflage d'oxygène ; le gaz de dégagement provenant d'une cascade de lit fluidisé dans laquelle des matériaux ferrifères oxydés sous forme de particules fines sont réduits à contre-courant par un gaz de réduction ; le gaz de gueulard provenant d'une cuve de réduction dans laquelle des matériaux ferrifères oxydés en morceaux sont réduits par un gaz de réduction ; le gaz excédentaire provenant d'un gazéificateur à fusion ; ou à base d'un mélange de deux ou plusieurs gaz appartenant à ce groupe. Le produit gazeux ainsi obtenu est tout d'abord au moins en partie soumis à une séparation par membrane pour séparer l'hydrogène, après quoi le gaz ainsi produit enrichi en hydrogène est soumis à une nouvelle purification par adsorption PSA ou VPSA. L'invention concerne par ailleurs un système comprenant des dispositifs permettant la mise en œuvre dudit procédé.
PCT/EP2012/067601 2011-09-29 2012-09-10 Procédé et dispositif de production d'hydrogène à partir de gaz provenant de la production de fonte Ceased WO2013045257A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA1415/2011A AT511992B1 (de) 2011-09-29 2011-09-29 Verfahren und vorrichtung zur herstellung von wasserstoff aus bei der roheisenerzeugung anfallenden gasen
ATA1415/2011 2011-09-29

Publications (1)

Publication Number Publication Date
WO2013045257A1 true WO2013045257A1 (fr) 2013-04-04

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PCT/EP2012/067601 Ceased WO2013045257A1 (fr) 2011-09-29 2012-09-10 Procédé et dispositif de production d'hydrogène à partir de gaz provenant de la production de fonte

Country Status (2)

Country Link
AT (1) AT511992B1 (fr)
WO (1) WO2013045257A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107337179A (zh) * 2017-08-09 2017-11-10 北京京诚泽宇能源环保工程技术有限公司 一种气基竖炉还原气的制备系统及方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102014114343B4 (de) 2013-10-07 2024-04-18 Thyssenkrupp Industrial Solutions Ag Verfahren zur kombinierten Herstellung von Roheisen und eines auf Synthesegas basierenden organischen Chemieprodukts

Citations (7)

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Publication number Priority date Publication date Assignee Title
WO1999042624A1 (fr) * 1998-02-20 1999-08-26 Hylsa, S.A. De C.V. Procede et appareil pour produire du fer de reduction directe grace a une utilisation optimale d'un gaz reducteur
EP0997693A2 (fr) * 1998-10-28 2000-05-03 Praxair Technology, Inc. Procédé intégrant par rectfication cryogénique, un haut-fourneau et un réacteur à réduction directe
US20030047037A1 (en) * 2001-07-27 2003-03-13 Sethna Rustam H. Process for removal of carbon dioxide for use in producing direct reduced iron
WO2009146982A1 (fr) * 2008-06-06 2009-12-10 Siemens Vai Metals Technologies Gmbh & Co Procédé et équipement de fabrication de fonte brute ou d'ébauches liquides en acier
WO2010042023A1 (fr) * 2008-10-06 2010-04-15 Luossavaara-Kiirunavaara Ab Procédé de production de fer directement réduit
WO2010057767A1 (fr) * 2008-11-21 2010-05-27 Siemens Vai Metals Technologies Gmbh & Co Procédé et dispositif de production d'un gaz brut de synthèse
WO2011012964A2 (fr) * 2009-07-31 2011-02-03 Hyl Technologies, S.A. De C.V. Procédé de production de fer préréduit aux émissions limitées de co2

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GB9123369D0 (en) * 1991-11-04 1991-12-18 Boc Group Plc Separation of hydrogen
WO2010020655A1 (fr) * 2008-08-21 2010-02-25 Shell Internationale Research Maatschappij B.V. Procédé amélioré de production de fer élémentaire

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999042624A1 (fr) * 1998-02-20 1999-08-26 Hylsa, S.A. De C.V. Procede et appareil pour produire du fer de reduction directe grace a une utilisation optimale d'un gaz reducteur
EP0997693A2 (fr) * 1998-10-28 2000-05-03 Praxair Technology, Inc. Procédé intégrant par rectfication cryogénique, un haut-fourneau et un réacteur à réduction directe
US20030047037A1 (en) * 2001-07-27 2003-03-13 Sethna Rustam H. Process for removal of carbon dioxide for use in producing direct reduced iron
WO2009146982A1 (fr) * 2008-06-06 2009-12-10 Siemens Vai Metals Technologies Gmbh & Co Procédé et équipement de fabrication de fonte brute ou d'ébauches liquides en acier
WO2010042023A1 (fr) * 2008-10-06 2010-04-15 Luossavaara-Kiirunavaara Ab Procédé de production de fer directement réduit
WO2010057767A1 (fr) * 2008-11-21 2010-05-27 Siemens Vai Metals Technologies Gmbh & Co Procédé et dispositif de production d'un gaz brut de synthèse
WO2011012964A2 (fr) * 2009-07-31 2011-02-03 Hyl Technologies, S.A. De C.V. Procédé de production de fer préréduit aux émissions limitées de co2

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107337179A (zh) * 2017-08-09 2017-11-10 北京京诚泽宇能源环保工程技术有限公司 一种气基竖炉还原气的制备系统及方法

Also Published As

Publication number Publication date
AT511992B1 (de) 2013-12-15
AT511992A1 (de) 2013-04-15

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