WO2004057044A2 - Method and plant for the heat treatment of solids containing iron oxide - Google Patents
Method and plant for the heat treatment of solids containing iron oxide Download PDFInfo
- Publication number
- WO2004057044A2 WO2004057044A2 PCT/EP2003/014106 EP0314106W WO2004057044A2 WO 2004057044 A2 WO2004057044 A2 WO 2004057044A2 EP 0314106 W EP0314106 W EP 0314106W WO 2004057044 A2 WO2004057044 A2 WO 2004057044A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- reactor
- solids
- fluidized bed
- gas supply
- Prior art date
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
-
- 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
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
- C22B5/14—Dry methods smelting of sulfides or formation of mattes by gases fluidised material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00004—Scale aspects
- B01J2219/00006—Large-scale industrial plants
-
- 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
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
Definitions
- the present invention relates to a method for the in particular reductive heat treatment of solids containing iron oxide, in which fine-grained solids are heated to a temperature of about 630°C in a fluidized-bed reactor, and to a corresponding plant.
- Such method and a plant are known for instance from DE 44 10 093 C1 , in order to reduce iron-oxide-containing solids such as iron ores, iron ore concentrates or the like.
- iron-oxide-containing ore is introduced into the fluidized-bed reactor and fluidized with heated reduction gas.
- the solids are entrained by the gas stream and separated from the exhaust gas in a downstream separator, in order to be recirculated to the reactor.
- solids are withdrawn from the lower region of the reactor.
- this object is solved by a method as mentioned above, in which a first gas or gas mixture is introduced from below through at least one preferably centrally arranged gas supply tube (central tube) into a mixing chamber region of the reactor, the central tube being at least partly surrounded by a stationary annular fluidized bed which is fluidized by supplying fluidizing gas, and in which the gas velocities of the first gas or gas mixture as well as of the fluidizing gas for the annular fluidized bed are adjusted such that the Particle-Froude-Numbers in the central tube are between 1 and 100, in the annular fluidized bed between 0.02 and 2 and in the mixing chamber between 0.3 and 30.
- the advantages of a stationary fluidized bed, such as a sufficiently long solids retention time, and the advantages of a circulating fluidized bed, such as a good mass and heat transfer, can surprisingly be combined with each other during the heat treatment, while the disadvantages of both systems are avoided.
- the first gas or gas mixture entrains solids from the annular stationary fluidized bed, which is referred to as annular fluidized bed, into the mixing chamber, so that due to the high slip velocities between the solids and the first gas an intensively mixed suspension is formed and an optimum mass and heat transfer between the two phases is achieved.
- the solids loading of the suspension above the orifice region of the central tube can be varied within wide ranges, so that the pressure loss of the first gas between the orifice region of the central tube and the upper outlet of the mixing chamber can be between 1 mbar and 100 mbar.
- the pressure loss of the first gas between the orifice region of the central tube and the upper outlet of the mixing chamber can be between 1 mbar and 100 mbar.
- a large part of the solids will separate out of the suspension and fall back into the annular fluidized bed.
- This recirculation is called internal solids recirculation, the stream of solids circulating in this internal circulation normally being significantly larger than the amount of solids supplied to the reactor from outside.
- the (smaller) amount of not precipitated solids is discharged from the mixing chamber together with the first gas or gas mixture.
- the retention time of the solids in the reactor can be varied within a wide range by the selection of height and cross-sectional area of the annular fluidized bed and be adapted to the desired heat treatment. Due to the high solids loading on the one hand and the good mass and heat transfer on the other hand, the formation of local temperature peaks in the mixing chamber can be avoided.
- the amount of solids entrained from the reactor with the gas stream is completely or at least partly recirculated to the reactor, with the recirculation expediently being fed into the stationary fluidized bed.
- the stream of solid matter thus recirculated to the annular fluidized bed normally lies in the same order of magnitude as the stream of solid matter supplied to the reactor from outside.
- another advantage of the method in accordance with the invention consists in the possibility of quickly, easily and reliably adjusting the utilization of the reduction gas and the mass transfer to the requirements by changing the flow velocities of the first gas or gas mixture and of the fluidizing gas.
- the construction of the reactor can be simplified such that the same for instance has a cylindrical shape.
- the gas velocities of the first gas mixture and of the fluidizing gas are preferably adjusted for the fluidized bed such that the dimensionless Particle-Froude-Numbers (Fr P ) in the central tube are 1.15 to 20, in particular about 10.6, in the annular fluidized bed 0.115 to 1.15, in particular about 0.28, and/or in the mixing chamber 0.37 to 3.7, in particular about 1.1.
- the Particle-Froude-Numbers are each defined by the following equation:
- d p does not indicate the mean diameter (d 50 ) of the material used, but the mean diameter of the reactor inventory formed during the operation of the reactor, which can differ significantly from the mean diameter of the material used (primary particles).
- particles (secondary particles) with a mean diameter of 20 to 30 ⁇ m can be formed for instance during the heat treatment.
- some materials, e.g. ores, are decrepitated during the heat treatment.
- the generation of the amount of heat necessary for the operation of the reactor can be effected in any way known to the expert for this purpose.
- preheated reduction gas to the reactor for fluidization, which reduces the possibly likewise preheated solids.
- the reactor temperature for instance lies below the temperature of the mass flows entering the reactor.
- reduction gas gas with a hydrogen content of at least 80 %, preferably above 90 %, is particularly useful.
- the consumption of fresh reduction gas can be decreased considerably when the reduction gas is cleaned in a reprocessing stage downstream of the reactor and subsequently recirculated to the reactor.
- the gas is first separated from solids, possibly passed through a scrubber and cooled below the dew point of steam, so that the steam content can be reduced, then compressed and enriched with fresh hydrogen.
- the exhaust gas is supplied to the reactor via the central tube, while processed reduction gas is expediently introduced as fluidizing gas into the annular fluidized bed through a conduit.
- a plant in accordance with the invention which is in particular suited for per orming the method described above, has a reactor constituting a fluidized-bed reactor for the in particular reductive heat treatment of solids containing iron oxide, the reactor having a gas supply system which is formed such that gas flowing through the gas supply system entrains solids from a stationary annular fluidized bed, which at least partly surrounds the gas supply system, into the mixing chamber.
- this gas supply system extends into the mixing chamber. It is, however, also possible to let the gas supply system end below the surface of the annular fluidized bed. The gas is then introduced into the annular fluidized bed e.g. via lateral apertures, entraining solids from the annular fluidized bed into the mixing chamber due to its flow velocity.
- the gas supply system has a central tube extending upwards substantially vertically from the lower region of the reactor into the mixing chamber of the reactor, which central tube is at least partly surrounded by a chamber in which the stationary annular fluidized bed is formed.
- the an- nular fluidized bed need not be circular, but rather other shapes of the annular fluidized bed are also possible in dependence on the geometry of the central tube and of the reactor, as long as the central tube is at least partly surrounded by the annular fluidized bed.
- two or more central tubes with different or the same dimensions can also be provided in the reactor.
- at least one of the central tubes is arranged approximately centrally, based on the cross-sectional area of the reactor.
- the central tube has apertures, for instance in the form of slots, at its shell surface, so that during the opera- tion of the reactor solids constantly get into the central tube through the apertures and are entrained by the first gas or gas mixture from the central tube into the mixing chamber.
- a separator for instance a cyclone for separating solids is provided downstream of the reactor, the separator having a solids conduit which leads to the annular fluidized bed of the first reactor.
- a gas distributor is provided in the annular chamber of the reactor, which di- vides the chamber into an upper fluidized bed region and a lower gas distributor chamber.
- the gas distributor chamber is connected with a supply conduit for fluidizing gas.
- a gas distributor composed of tubes.
- the energy demand of the plant can be reduced in that the reactor has a supply conduit for hydrogen-containing reduction gas, which leads to the central tube and is connected for instance with the exhaust gas outlet of a separator of another reactor provided downstream of the reactor.
- a supply conduit for preheated hydrogen-containing reduction gas which extends in or leads to the annular chamber, may be provided in the plant in accordance with the invention.
- the energy required for the heat treatment should preferably not exclusively be introduced into the reactor via the gases.
- a preheating stage for the solids may be provided upstream of the reactor, so that already preheated solids are introduced into the reactor.
- the temperature of the solids charged into the reactor lies above the reactor temperature.
- means for deflecting the solid and/or fluid flows may be provided in accordance with the invention. It is for instance possible to position an annular weir, whose diameter lies between that of the central tube and that of the reactor wall, in the annular fluidized bed such that the upper edge of the weir protrudes beyond the solids level obtained during operation, whereas the lower edge of the weir is arranged at a distance from the gas distributor or the like.
- solids separated out of the mixing chamber in the vicinity of the reactor wall must first pass by the weir at the lower edge thereof, before they can be entrained by the gas flow of the central tube back into the mixing chamber. In this way, an ex- change of solids is enforced in the annular fluidized bed, so that a more uniform retention time of the solids in the annular fluidized bed is obtained.
- Fig. 1 shows a process diagram of a method and a plant in accordance with an embodiment of the present invention
- Fig. 2 shows an enlarged detail of Fig. 1.
- FIG. 1 which is in particular suited for the heat treatment of solids containing iron oxide, solids are introduced into a reactor 1 via a supply conduit 2, as can be seen in the enlarged representation of Figure 2.
- the for instance cylindrical reactor 1 has a central tube 3 arranged approximately coaxially with the longitudinal axis of the reactor, which central tube extends substantially vertically upwards from the bottom of the reactor 1.
- annular gas distributor chamber 4 In the vicinity of the bottom of the reactor 1 , an annular gas distributor chamber 4 is provided, which at its upper end is terminated by a gas distributor 5 having through openings. A supply conduit 6 opens into the gas distributor chamber 4.
- a discharge conduit 8 is arranged, which opens into a separator 9 constituting a cyclone.
- annular fluidized bed 10 When solids are now introduced into the reactor 1 via the supply conduit 2, a layer an- nularly surrounding the central tube 3 is formed on the gas distributor 5, which layer is referred to as annular fluidized bed 10. Fluidizing gas introduced into the gas distributor chamber 4 through the supply conduit 6 flows through the gas distributor 5 and fluidizes the annular fluidized bed 10, so that a stationary fluidized bed is formed. The velocity of the gases supplied to the reactor 1 via the gas distributor chamber 4 is adjusted such that the Particle-Froude-Number in the annular fluidized bed 10 is about 0.28.
- the solids level 11 in the reactor 1 rises to such an extent that solids get into the orifice of the central tube 3.
- a gas or gas mixture is at the same time introduced into the reactor 1.
- the velocity of the gas supplied to the reactor 1 preferably is adjusted such that the Particle-Froude-Number in the central tube 3 is about 10.6 and in the mixing chamber 7 about 1.1. Due to these high gas velocities, the gas flowing through the central tube 3 entrains solids from the stationary annular fluidized bed 10 into the mixing chamber 7 when passing through the upper orifice region.
- the upper edge of the central tube 3 can be straight, wavy or serrated, or the shell surface can have lateral inlet openings.
- the fine-grained solids such as iron ore are first charged into a preheating stage with a Venturi preheater 12. Downstream of the same a cyclone 13 is provided, in which the solids are separated from exhaust gas. From the cyclone 13, the solids are supplied to another Venturi preheater 14. Downstream of the same, a cyclone 15 is in turn provided, in which the solids are separated from exhaust gas and via a bunker 16 and a screw conveyor 17 are supplied to the reactor 1 via conduit 2.
- Hot combustion gases from a combustion chamber 18 are supplied to the Venturi preheater 14 for heating the solids, to which combustion chamber fuel is supplied via con- duit 10 and combustion air is supplied via conduit 20. It turned out to be advantageous to operate the combustion at a pressure of 0.8 to 10 bar and preferably at atmospheric pressure.
- the still hot exhaust gases which were separated from the solids in the cyclone 15 are supplied to the first Venturi preheater 12 for preheating the solids. After the separation of the solids in the cyclone 13, the exhaust gas is cleaned in a filter 21.
- the solids are subjected to a heat treatment, with heated reducing fluidizing gas being introduced through conduit 6 into the annular fluidized bed 10 formed.
- exhaust gas from another reduction stage downstream of the reactor 1 is supplied through the central tube 3, so that the solids for one part circulate in the reactor 1 in the manner described above and for the other part are discharged from the reactor 1 via conduit 8 and upon separation of the exhaust gas in the cyclone 9 are recirculated to the annular fluidized bed via conduit 22.
- a stream of solids is in addition withdrawn from the reactor 1 and supplied to a downstream fluidized bed reactor 23.
- the fluidized-bed reactor 23 has a classical fluidized bed, into which heated fluidizing gas is introduced via conduit 24. Via conduit 25, solids are withdrawn from the fluidized-bed reactor 23 and supplied for instance to a briquetting plant 26.
- a cyclone 27 the exhaust gases of the fluidized-bed reactor 23 are separated from solids, which are recirculated to the fluidized-bed reactor 23 via conduit 28.
- the exhaust gases are supplied from the cyclone 27 via conduit 29 to the central tube 3 of the reactor 1.
- the exhaust gases of the reactor 1 which were separated from the solids in the cyclone 9, are supplied to a reprocessing via conduit 30.
- the exhaust gases are cooled in a heat exchanger 31 and introduced into a scrubber 32, where the cooled gas is further cooled below the dew point of steam, so that the steam content of the exhaust gas can largely be removed.
- a partial stream of the exhaust gas can be removed from the circuit, to prevent for instance an accumulation of nitrogen in the circulating gas.
- fresh reducing gas can be admixed via conduit 34 for fortification.
- the cleaned gas is now preheated in the heat exchanger 31 and supplied to a heater 35.
- the cleaned hot reduction gas is then supplied to the fluidized-bed reactor 23 via conduit 24 and as fluidizing gas via conduit 6 to the reactor 1.
- the reduction temperature in the reactor 1 which had a diameter of 3 m, was about 630°C.
- the pressure at the outlet of the reactor 1 was 4 bar.
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EA200501030A EA010275B1 (en) | 2002-12-23 | 2003-12-12 | Method and plant for the heat treatment of solids containing iron oxide |
US10/540,434 US7632334B2 (en) | 2002-12-23 | 2003-12-12 | Method and plant for the heat treatment of solids containing iron oxide |
BRPI0317664-9B1A BR0317664B1 (en) | 2002-12-23 | 2003-12-12 | Method and plant for the thermal treatment of solids containing iron oxide |
CA2510930A CA2510930C (en) | 2002-12-23 | 2003-12-12 | Method and plant for the heat treatment of solids containing iron oxide |
UAA200507302A UA81792C2 (en) | 2002-12-23 | 2003-12-12 | Method and plant for heat treatment of solids containing iron oxide |
AU2003292233A AU2003292233B2 (en) | 2002-12-23 | 2003-12-12 | Method and plant for the heat treatment of solids containing iron oxide |
US12/610,821 US8025836B2 (en) | 2002-12-23 | 2009-11-02 | Method and plant for the heat treatment of solids containing iron oxide |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10260731A DE10260731B4 (en) | 2002-12-23 | 2002-12-23 | Process and plant for the heat treatment of iron oxide-containing solids |
DE10260731.1 | 2002-12-23 |
Related Child Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/540,434 A-371-Of-International US7632334B2 (en) | 2002-12-23 | 2003-12-12 | Method and plant for the heat treatment of solids containing iron oxide |
US12/610,821 Division US8025836B2 (en) | 2002-12-23 | 2009-11-02 | Method and plant for the heat treatment of solids containing iron oxide |
Publications (2)
Publication Number | Publication Date |
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WO2004057044A2 true WO2004057044A2 (en) | 2004-07-08 |
WO2004057044A3 WO2004057044A3 (en) | 2005-02-24 |
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ID=32477937
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PCT/EP2003/014106 WO2004057044A2 (en) | 2002-12-23 | 2003-12-12 | Method and plant for the heat treatment of solids containing iron oxide |
Country Status (11)
Country | Link |
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US (2) | US7632334B2 (en) |
CN (1) | CN100529125C (en) |
AU (1) | AU2003292233B2 (en) |
BR (1) | BR0317664B1 (en) |
CA (1) | CA2510930C (en) |
DE (1) | DE10260731B4 (en) |
EA (1) | EA010275B1 (en) |
MY (1) | MY134382A (en) |
UA (1) | UA81792C2 (en) |
WO (1) | WO2004057044A2 (en) |
ZA (1) | ZA200505916B (en) |
Cited By (1)
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EP3080314B1 (en) * | 2013-12-11 | 2019-12-04 | Outotec (Finland) Oy | Arsenic removal from minerals |
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DE10260734B4 (en) * | 2002-12-23 | 2005-05-04 | Outokumpu Oyj | Process and plant for the production of carbon coke |
DE10260737B4 (en) | 2002-12-23 | 2005-06-30 | Outokumpu Oyj | Process and plant for the heat treatment of titanium-containing solids |
DE10260738A1 (en) | 2002-12-23 | 2004-07-15 | Outokumpu Oyj | Process and plant for conveying fine-grained solids |
DE10260735B4 (en) * | 2002-12-23 | 2005-07-14 | Outokumpu Oyj | Process and plant for heat treatment of sulfide ores |
DE10260733B4 (en) * | 2002-12-23 | 2010-08-12 | Outokumpu Oyj | Process and plant for the heat treatment of iron oxide-containing solids |
DE10260739B3 (en) | 2002-12-23 | 2004-09-16 | Outokumpu Oy | Process and plant for producing metal oxide from metal compounds |
DE10260741A1 (en) | 2002-12-23 | 2004-07-08 | Outokumpu Oyj | Process and plant for the heat treatment of fine-grained solids |
DE10260731B4 (en) | 2002-12-23 | 2005-04-14 | Outokumpu Oyj | Process and plant for the heat treatment of iron oxide-containing solids |
DE102004042430A1 (en) * | 2004-08-31 | 2006-03-16 | Outokumpu Oyj | Fluidized bed reactor for the thermal treatment of vortex substances in a microwave-heated fluidized bed |
CN101386908B (en) * | 2007-09-11 | 2010-12-08 | 中国科学院过程工程研究所 | Magnetization roasting technique system for refractory iron ore powder and roasting technology |
US8282887B2 (en) * | 2010-03-30 | 2012-10-09 | Uop Llc | Multi-stage fluidized bed reactor for dehydrogenation of hydrocarbons |
CN103316618B (en) * | 2012-03-21 | 2015-10-28 | 中国石油化工集团公司 | A kind of gas distributor with distributor chamber |
CN102728844A (en) * | 2012-06-29 | 2012-10-17 | 武汉钢铁(集团)公司 | Method for preparing superfine iron powder at low cost |
US10661340B2 (en) * | 2016-08-03 | 2020-05-26 | Reid Reactors Llc | Method and apparatus for producing metallic iron from iron oxide fines |
US10434576B2 (en) * | 2016-08-03 | 2019-10-08 | Reid Reactors Llc | Method and apparatus for producing metallic iron from iron oxide fines |
EP3708684B1 (en) | 2019-03-15 | 2022-03-02 | Primetals Technologies Austria GmbH | Method for direct reduction in a fluidised bed |
EP4340981A1 (en) * | 2021-05-20 | 2024-03-27 | Teknologian Tutkimuskeskus VTT OY | Method and apparatus for heating fluidizing agent and use |
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- 2003-12-12 US US10/540,434 patent/US7632334B2/en not_active Expired - Fee Related
- 2003-12-12 CN CNB2003801073122A patent/CN100529125C/en not_active Expired - Lifetime
- 2003-12-12 UA UAA200507302A patent/UA81792C2/en unknown
- 2003-12-12 WO PCT/EP2003/014106 patent/WO2004057044A2/en not_active Application Discontinuation
- 2003-12-12 ZA ZA200505916A patent/ZA200505916B/en unknown
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- 2003-12-12 EA EA200501030A patent/EA010275B1/en not_active IP Right Cessation
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Also Published As
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US20100044933A1 (en) | 2010-02-25 |
BR0317664B1 (en) | 2013-09-10 |
AU2003292233B2 (en) | 2009-07-09 |
CA2510930A1 (en) | 2004-07-08 |
AU2003292233A1 (en) | 2004-07-14 |
DE10260731B4 (en) | 2005-04-14 |
UA81792C2 (en) | 2008-02-11 |
CA2510930C (en) | 2012-11-27 |
EA200501030A1 (en) | 2006-02-24 |
US7632334B2 (en) | 2009-12-15 |
CN1738918A (en) | 2006-02-22 |
US20060230880A1 (en) | 2006-10-19 |
EA010275B1 (en) | 2008-08-29 |
WO2004057044A3 (en) | 2005-02-24 |
ZA200505916B (en) | 2006-11-29 |
US8025836B2 (en) | 2011-09-27 |
CN100529125C (en) | 2009-08-19 |
BR0317664A (en) | 2005-11-29 |
MY134382A (en) | 2007-12-31 |
DE10260731A1 (en) | 2004-07-08 |
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