CN101473050B - Pressure control in direct smelting process - Google Patents
Pressure control in direct smelting process Download PDFInfo
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- CN101473050B CN101473050B CN2007800226472A CN200780022647A CN101473050B CN 101473050 B CN101473050 B CN 101473050B CN 2007800226472 A CN2007800226472 A CN 2007800226472A CN 200780022647 A CN200780022647 A CN 200780022647A CN 101473050 B CN101473050 B CN 101473050B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
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- 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
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
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- 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
- C21B13/143—Injection of partially reduced ore into a molten bath
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
- C21C5/56—Manufacture of steel by other methods
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B3/00—Hearth-type furnaces, e.g. of reverberatory type; Tank furnaces
- F27B3/10—Details, accessories, or equipment peculiar to hearth-type furnaces
- F27B3/22—Arrangements of air or gas supply devices
- F27B3/225—Oxygen blowing
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B3/00—Hearth-type furnaces, e.g. of reverberatory type; Tank furnaces
- F27B3/10—Details, accessories, or equipment peculiar to hearth-type furnaces
- F27B3/26—Arrangements of heat-exchange apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D19/00—Arrangements of controlling devices
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- 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
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
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- 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
-
- 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
- C21B2100/64—Controlling the physical properties of the gas, e.g. pressure or temperature
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- 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
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C2100/00—Exhaust gas
- C21C2100/02—Treatment of the exhaust gas
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C2100/00—Exhaust gas
- C21C2100/06—Energy from waste gas used in other processes
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- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
A process for direct smelting metalliferous feed material in a direct smelting vessel and producing process outputs of molten metal, molten slag, and an off-gas from the vessel is disclosed. The process includes controlling pressure in the direct smelting vessel by controlling off-gas pressure in an off-gas stream supplied to a fluidised bed pretreatment apparatus while the process is operating in the 'hold' and 'idle' process states.
Description
Technical field
The present invention relates to a kind of direct melting technology and equipment based on molten metal bath, be used for producing molten metal at direct melting container.
Particularly, the present invention relates to control the interior pressure of direct melting container.
The present invention especially but and not exclusively relate to direct melting technology based on molten metal bath, be used for supplying with material from the metal of iron content, for example iron ore, partial reduction iron ore and (as from steelworks) iron content waste streams produce molten pig.
Background technology
Known direct melting technology based on molten metal bath is commonly referred to HIsmelt technology.Under the situation of producing molten pig, this HIsmelt technology may further comprise the steps:
(a) molten bath of formation molten pig and slag in direct melting container;
(b) inject in the molten bath: (i) metal-containing supplying material is generally the iron ore that is fine powder form; (ii) solid carbon-containing material is generally coal, as reductive agent and the energy source of metal-containing supplying material; And
(c) with the metal-containing supplying material melting be iron in the molten bath.
At this, term " melting " is interpreted as referring to thermal treatment, wherein, carries out the chemical reaction of reducing metal oxide, to produce molten metal.
In HIsmelt technology, metal-containing supplying material and solid carbon-containing material are injected into molten metal bath by a plurality of spray gun/blast orifices, described spray gun/blast orifice tilts with respect to vertical direction, inwardly passing the sidewall of direct melting container and to enter this container lower region, thereby at least part of solid matter is transported to metal level in the container bottom downwards.Spray gun by downward extension is injected into the upper area of container with oxygen-containing gas (being generally air or the oxygen-rich air) air blast of heat, thereby the reactant gases that molten metal bath is discharged carries out afterfire in the upper area of container.Usually, under the situation of producing molten pig, the temperature of warm air or hot oxygen-rich air is approximately 1200 ℃, and produces in hot blast stove.Take away the tail gas of the afterfire generation of container reaction gases from the upper area of container by exhaust pipe.Container is included in the sidewall of container and the water-cooled refractory slab in the furnace roof liner, and water circulates by described plate continuously in the mode of successive loops.
This HIsmelt technology makes and can produce a large amount of molten pigs by direct melting in an independent compact container, is at least 0.5Mt/a usually.
Yet, in order in HIsmelt technology, to obtain high molten pig productivity, need (a) to produce a large amount of warm airs or hot oxygen-rich air and carrier gases (being used for solid injects), and these gases are transported to direct melting container, (b) with a large amount of metal-containing supplying material, such as containing the iron supply materials conveyance to container, comprise and produce a large amount of carrier gases, and this carrier gases is transported to container, (c) from a large amount of hot exhaust gas of container transport, (d) be transported away a large amount of molten pigs and the slag that produces from container this technology, and (e) a large amount of water circulated by cooled plate, all these carries out in the zone of relative closure.
In view of this, high molten pig productivity need have a kind of like this HIsmelt equipment, it comprises direct melting container and the supplementary unit of (a) pressurization, such as the lock hopper that is used for supplying with to container supply solid material, and be positioned at pressure control device on the exhaust pipe of container, (b) produce the stove of high flow capacity warm air or hot oxygen-rich air for container, and (c) exhaust gas processing device, it can be handled a large amount of tail gas that are discharged from the container.
A kind of HIsmelt technical process of current proposition is designed in multiple " state " operation down, and these " states " have different running condition during the melting operating period, and described " state " for example comprises following state of the art:
(a) start;
(b) thermometal production, that is, supply is through pretreated metal-containing supplying material such as hot ore, such as solid carbon-containing material and the hot-blast air of coal;
(c) keep, that is, do not supply through pretreated metal-containing supplying material, supply solid carbon-containing material and hot-blast air;
(d) idle running namely, is not supplied through pretreated metal-containing supplying material and is not supplied solid carbon-containing material, supply hot-blast air; And
(e) calm, that is, do not supply through pretreated metal-containing supplying material, do not supply solid carbon-containing material, do not supply the hot-blast air yet.
Usually, in above-mentioned state of the art, the volumetric flow rate of the tail gas that produces in direct melting container is different.For example, usually, the flow of the tail gas during the thermometal production status is higher, and the flow of the tail gas during idling conditions is lower.In further example, usually, during windless condition, do not have tail gas, do not have caloric value in the tail gas during idling conditions.
Concerning above-mentioned HIsmelt technology, during above-mentioned " maintenance " and " idle running " state of the art, directly the pressure-controlling in the melting container is important problem.
Summary of the invention
On wide in range meaning, the invention provides a kind of technology, this technology is used for direct melting metal-containing supplying material in direct melting container, and produce the process products of molten metal, slag and tail gas from container, this technology comprises, when this technology operates in the state of the art of aforesaid " maintenance " and " idle running ", by the tail gas pressure of control in the tail gas stream that supplies to the fluidized-bed pretreatment unit, control the pressure in the direct melting container.
More specifically, the invention provides a kind of technology, this technology is used for " thermometal production " state direct melting metal-containing supplying material in direct melting container in technology, and the process products of generation molten metal, slag and tail gas, described direct melting container forms the part of direct melting equipment, and this technology comprises:
(a) according to required given processing condition, in a plurality of state of the art, optionally move described technology, this state of the art comprises " thermometal production " state and " maintenance " and " idle running " state, in " thermometal production " state, melting metal-containing supplying material in container is to produce molten metal, in " maintenance " and " idle running " state, directly keep the molten bath of melting material with molten state in the melting container, and do not producing extra molten metal;
(b) when technology operates in " thermometal production " state, to be divided at least two bursts of tail gas stream from the tail gas that direct melting container discharges, and one tail gas stream supplied to the fluidized-bed pretreatment unit, be fed into the metal-containing supplying material of direct melting container subsequently with pre-treatment, and another burst tail gas stream is supplied to described equipment, to be used as fuel gas;
(c) when technology operates in " maintenance " and " idle running " state of the art, will supply to the fluidized-bed pretreatment unit from the tail gas stream that direct melting container discharges, be fed into the metal-containing supplying material of direct melting container subsequently with fluidisation at least; And
(d) when technology operates in " maintenance " and " idle running " state of the art, by the tail gas pressure of control in the tail gas stream that supplies to the fluidized-bed pretreatment unit, control the pressure in the direct melting container.
Preferably, this technology comprises, in the time of in operating in " thermometal production " state, supplying to described equipment with as the exhaust flow in another burst tail gas stream of fuel gas, controls the pressure in the direct melting container by control.
The present invention is based on this understanding: by the tail gas pressure of control in the tail gas stream that supplies to the fluidized-bed pretreatment unit, be best implemented in the pressure-controlling in " maintenance " and " idle running " state of the art.
The present invention is also based on this understanding: by another the alternative tail gas stream with respect to the tail gas stream that supplies to the fluidized-bed pretreatment unit, realize the pressure-controlling during " thermometal production " state best.
Preferably, described technology comprises: will be at least one tail gas stream act as a fuel gas supply to (i) waste heat recovery unit and (ii) in the stove at least one, described waste heat recovery unit is for generation of the steam that uses in this technology, and described stove is for generation of the warm air air blast of using in this technology.
Preferably, " maintenance " state comprises: warm air air blast or hot oxygen-rich air air blast, solid carbon-containing material and flux are supplied to direct melting container, and do not supply with metal-containing material.
Preferably, " idle running " state comprises: warm air air blast or hot oxygen-rich air air blast are supplied to direct melting container, and do not supply with metal-containing material and solid carbon-containing material.
Preferably, described technology comprises: in the water scrubber in the downstream of pretreatment unit, and cooling and remove microparticle material and soluble gas kind and metallic vapor from the tail gas stream that supplies to the fluidized-bed pretreatment unit.
Preferably, step (d) comprising: when technology operates in " maintenance " and " idle running " state of the art, by opening or closing the tail gas control valve in the washer, the exhaust flow of the washer that controlling flows through describes in aforementioned section, thereby control the pressure in the direct melting container, this washer is called " pressure-controlling washer " hereinafter.
Preferably, step (c) comprising: when technology operates in " maintenance " and " idle running " state of the art, the whole tail gas stream basically that discharge to the major general from direct melting container supply to the fluidized-bed pretreatment unit as tail gas stream, and therefore minimize any tail gas shunting.
In this case, in the stove of the warm air air blast of using for generation of described technology or hot oxygen-rich air air blast, has only insufficient tail gas usually as fuel gas.
Therefore, in this case, described technology comprises: when described technology operates in " maintenance " and " idle running " state of the art, with another fuel gas, supply to the warm air air blast used for generation of described technology or the stove of hot oxygen-rich air air blast such as Sweet natural gas.
Preferably, described technology comprises: when described technology operates in " thermometal production " state, in the water scrubber of the upstream of stove and waste heat recovery unit, cooling and remove microparticle material and soluble gas kind and metallic vapor from another burst tail gas stream.
Preferably, the washer of describing in aforementioned section comprises the exhaust flow control valve.
Preferably, described technology comprises: when the beginning of " maintenance " and " idle running " state of the art, be closed in the valve in the pneumatic scrubber of describing in preceding two sections at least basically.
Preferably, described technology comprises: will supply to waste heat recovery unit from the tail gas of pretreatment unit, as fuel gas, to produce the steam that described technology is used.
Preferably, described technology comprises: during " maintenance " and " idle running " state of the art, a part of tail gas stream that supplies to the fluidized-bed pretreatment unit in the pretreatment unit is carried out recycling.
Preferably, described technology comprises: when described technology operates in " thermometal production " state, with first volumetric flow rate warm air air blast or hot oxygen-rich air air blast are supplied to direct melting container, and when described technology operates in " maintenance " and " idle running " state of the art, with the second lower volumetric flow rate warm air or oxygen-rich air air blast are supplied to direct melting container.
Preferably, described technology comprises: when described technology operates in " thermometal production " state, with the pressure-controlling in the direct melting container to the first pressure set-point, and when described technology operates in " maintenance " and " idle running " state of the art, the pressure-controlling in the direct melting container is arrived lower pressure set-point.
Preferably, described technology comprises: the molten metal temperature of monitoring in the direct melting container during " idle running " state of the art, and as required with fuel gas supply to container and in container combustion fuel gas, to keep the molten metal temperature in the container.
Preferably, described technology comprises: when described technology operates in " idle running " state and described technology is during combustion fuel gas, to reduce the level of the slag in the direct melting container in container.
The present invention also provides a kind of technology for the direct melting equipment of operation, this direct melting equipment has direct melting container and fluidized-bed pretreatment unit, described direct melting container moves under pressure, described fluidized-bed pretreatment unit is used for the metal-containing material that pre-treatment supplies to direct melting container subsequently, described equipment produces the product of molten metal, slag and tail gas, wherein, described technology comprises:
(a) according to required given processing condition, operational outfit optionally in a plurality of state of the art, described state of the art comprises " thermometal production " state and " maintenance " and " idle running " state, in " thermometal production " state, melting metal-containing supplying material in container, with the production molten metal, and in " maintenance " and " idle running " state, in direct melting container with molten state keep melting material the molten bath, and do not produce extra molten metal;
(b) when described equipment operates in " thermometal production " state, to be divided at least two bursts of tail gas stream from the tail gas that direct melting container discharges, and one tail gas stream supplied to the fluidized-bed pretreatment unit, be fed into the metal-containing supplying material of direct melting container subsequently with pre-treatment, and another tail gas stream is supplied to described equipment, to be used as fuel gas;
(c) when described equipment operates in " maintenance " and " idle running " state of the art, will supply to the fluidized-bed pretreatment unit from the tail gas stream that direct melting container discharges, be fed into the metal-containing supplying material of direct melting container subsequently with fluidisation at least; And
(d) when described technology operates in " maintenance " and " idle running " state of the art, by the tail gas pressure of control in the tail gas stream that supplies to the fluidized-bed pretreatment unit, control the pressure in the direct melting container.
In general sense, it is a kind of for direct melting metal-containing supplying material and produce the direct melting equipment of molten metal that the present invention also provides, and this equipment comprises:
(a) fluidized-bed pretreatment unit is used for the pre-treatment metal-containing supplying material;
(b) direct melting container, be used for by producing molten metal in the direct melting of this container through the technology of the metal-containing supplying material of preheating, described technology comprises a plurality of state of the art, and these a plurality of state of the art comprise as " startup " described here, " thermometal production ", " maintenance ", " idle running " and " calm ";
(c) exhaust pipe is used for the tail gas that direct melting container produces is taken away, and the tail gas in the tail gas stream is supplied to pretreatment unit; And
(d) process controller is used for when described technology operates in as " maintenance " described here and " idle running " state of the art, supplies to the tail gas pressure in the tail gas stream of pretreatment unit by control, controls the interior pressure of direct melting container.
More specifically, the invention provides a kind ofly for direct melting metal-containing supplying material and produce the direct melting equipment of molten metal, this equipment comprises:
(a) fluidized-bed pretreatment unit is used for the pre-treatment metal-containing supplying material;
(b) direct melting container, be used for producing molten metal by direct melting in container through the technology of the metal-containing supplying material of preheating, this technology comprises a plurality of state of the art, and these a plurality of state of the art comprise aforesaid " startup ", " thermometal production ", " maintenance ", " idle running " and " calm ";
(c) stove, warm air air blast or the hot oxygen-rich air air blast used for generation of technology;
(d) waste heat recovery unit, the steam of using for generation of this equipment;
(e) exhaust pipe is used for the tail gas that produces in the direct melting container being taken away and tail gas being divided into two bursts of tail gas stream, and wherein one tail gas stream is supplied to pretreatment unit by first pipe section, and another burst tail gas stream is fed into second pipe section; And
(f) process controller is used for when technology operates in aforesaid " maintenance " and " idle running " state of the art, by the tail gas pressure of control in supplying to the tail gas stream of pretreatment unit, controls the pressure in the direct melting container.
Preferably, when process controller can also be worked as technology and operated in as mentioned above in " thermometal production " state, by the tail gas pressure of control in the tail gas stream that supplies to second pipe section, control the pressure in the direct melting container.
Description of drawings
Hereinafter with reference to accompanying drawing the present invention is described in further detail, in the accompanying drawing:
Fig. 1 is the synoptic diagram according to an embodiment of direct melting equipment of the present invention; And
Fig. 2 is the wet type taper washing tower in the tail gas stream that tail gas is fed to waste heat recovery unit shown in Figure 1 and stove and the enlarged view of exhaust gas cooler.
Embodiment
Below to the description of the equipment shown in the accompanying drawing based on this situation: according to the HIsmelt technology described in International Application Serial No. PCT/AU96/00197 of the applicant, adopt this equipment to come melting to contain the iron supply material, thereby produce molten pig.Disclosure in the patent specification that this international application comprises is attached to herein by cross reference.
This technology is based on the use of direct melting container 3.
In use, container 3 contains the molten pig molten bath.To contain iron supply material (such as powdered iron ore, the steel mill's waste material that contains iron or DRI powder), coal and flux (lime and rhombspar) via solid spray gun 5 and directly inject the molten bath.
Particularly, one group of spray gun 5 is used for injecting supply material and the flux of iron content, and another group spray gun 5 is used for injecting coal and flux.
Spray gun 5 is protected their not influences of receptor 3 interior high temperature by water-cooled.Spray gun 5 is lined with the material of high abrasion usually, is subjected to the wearing and tearing of the gas/solid mixture of high-velocity jet to prevent them.
Contain the iron supply material and carry out pre-treatment by being preheating to 600 to 700 ℃ of temperature in the scope, and before injecting the molten bath in 17 prereduction of fluidized-bed preheater.
Inject at ambient temperature before the molten bath, coal and flux are stored in a series of lock hoppers 25.Via coal drying and grinding equipment 71 coal is fed to lock hopper 25.
The coal that injects liquefies in the molten bath, thereby discharges H
2And CO.These gases are as reductive agent and energy source.Carbon in the coal is dissolved in the molten bath fast.Dissolved carbon and solid carbon produce the CO as reduzate also as reductive agent.The iron content supply material melts of injecting is the molten pig in molten bath, and discharges continuously via forehearth 67.The slag that produces in this process is regularly discharged via the slag notch (not shown).
The iron supply material melts that contains that to inject that takes place in the molten bath is that the related typical reduction reaction of molten pig is thermo-negative reaction.Keeping this process, more specifically keeping the required energy of these thermo-negative reaction is CO and the H that discharges by from the molten bath
2With react and provide being generally the oxygen-rich air that injects under 1200 ℃ the high temperature via HAB spray gun 7.
The energy that discharges from the above-mentioned afterfire reaction in the container top space is transferred to the molten pig molten bath via " zone of transition ", should " zone of transition " be the form in the high turbulence zone of the drop that contains slag and iron above the molten bath.The heat heating that these drops are produced by the afterfire reaction in this zone of transition, and turn back to slag/iron bath, thus energy is transferred to the molten bath.
The hot oxygen-rich air that is injected in the container 3 via HAB spray gun 7 produces in hot blast stove 11 by this way, namely, make oxygen-rich air (nominally the oxygen volume content is 30 to 35%) by stove 11, and to air heating, be responsible for 41 via hot-blast afterwards hot oxygen-rich air is transported to HAB spray gun 7.
The operation of regulating stove 11 is to guarantee having continuous, unbroken hot oxygen-rich air to flow to HAB spray gun 7 in 41 being responsible under constant straight line temperature.
Each stove 11 is according to the repeated sequence operation in a plurality of stages, and these stages comprise heating phase, perfusion phase and heat exchange stage, and the heat exchange stage is than the time segment length of heating phase.
During the heating phase of stove 11, heat stove 11 in the following manner, i.e. burning (a) is from the tail gas through cooling and purification of container 3, and/or (b) optional another fuel gas, such as Sweet natural gas, and (c) combustion gases in the burner assembly (not shown) of stove 11, make products of combustion pass through stove 11 afterwards.
During the heat exchange stage of stove 11, in the charge air flow that will produce to gas blower 31 from the oxygen mix of breathing equipment 29.These oxygen-rich air streams pass through stove 11, and at stove 11 internal heating, thereby be that container 3 produces hot oxygen enrichment charge air flow.These hot oxygen-rich air streams are called as " hot-blast " or " warm air air blast " usually.
The perfusion phase of stove 11 is such stages, that is, one of them stove cuts out substantially, and neither burned tail gas (with other fuel gas, such as Sweet natural gas) heats also not by cooling off with the airflow heat exchange.
The time length of the perfusion phase of given stove 11 is at least and opens and closes the required time quantum of valve, the opening and closing of these valves are that conversion tail gas and hot blast are required, thereby (a) given stove are switched to the heat exchange stage and (b) another stove switched to the heating phase from the heat exchange stage from the heating phase.
In flue gas desulfurization (FGD) system 13, purify the products of combustion that stove 11 discharges in its heat-processed.This FGD removes from products of combustion usually with hydrogen sulfide (H
2S) and sulfurous gas (SO
2) sulphur that exists of form.The tail gas that produces in the container 3 contains sulphur, and is such as will be described below, before tail gas arrives stove 11, can not remove sulphur fully in the tail gas clean-up that carry out in container 3 downstreams.
Before the products of combustion that stove 11 discharged in its heating phase passes through the FGD system, described products of combustion can pass through the heat exchanger (not shown), and, as supplying with before material is fed to the burner of stove 11 in the heating phase tail gas and the combustion gases from the container 3 that cool off and purify are preheated at tail gas that will heating and combustion air.The tail gas of container and combustion air can preheat about 180 ℃ temperature.
Tail gas discharges from container 3 via the exhaust pipe 9 that is positioned at container 3 tops, and tail gas is at first by radiant coolers 15, and this radiant coolers is hereinafter referred to as " tail gas cover ".Usually, tail gas leaves container and enters this tail gas cover under about 1450 ℃ temperature.
Tail gas is cooled in by tail gas cover 15, thereby causes producing in steam drum 35 steam that gathers.This tail gas cover can be United States Patent (USP) 6,585, the tail gas cover of the sort of type of the cooling described in 929 and part cleaning of off-gas.
The tail gas stream of leaving tail gas cover 15 is under about 1000 ℃ temperature, and is divided into two strands of air-flows.
Specifically with reference to Fig. 2, one tail gas stream of leaving tail gas cover 15 includes 55-65% the tail gas from container 3, and this burst tail gas stream is at first by wet type taper washing tower 21.
77 pairs of flows by the tail gas of washing tower 21 of control valve are controlled.This is to first changeable flow constraint from the tail gas of container 3.Therefore, the pressure in 77 pairs of direct melting containers 3 of control valve is controlled, and in the process of producing molten pig, preferably it is controlled to the gauge pressure of 0.8 bar.
Tail gas from washing tower 21 leaves washing tower 21 via the outlet 81 in the lower chambers 73, and by exhaust gas cooler 23, below this exhaust gas cooler 23 further cooled exhaust gas to 50 ℃, usually between 30 ℃ to 45 ℃, with the moisture from tail gas removal capacity, thereby tail gas can be used as fuel gas.Usually, the tail gas that leaves water cooler has 5% or H still less
2O and be lower than 10mg/Nm
3, be generally 5.0mg/Nm
3The mist amount that contains.
Under the situation of common Metal Production, the tail gas that produces is suitable for use as (a) stove 11 (as mentioned above) and (b) fuel gas in the WHR system 25.In addition, the tail gas through washing and cooling is suitable in dry and grinding equipment 71 coal being carried out drying.
For above purpose, will be divided into three strands of air-flows from the tail gas of gas cooler 23, wherein one air-flow leads to stove 11, and another strand air-flow leads to 25, the three strands of air-flows of WHR system and leads to dry and grinding equipment 71.
Tail gas stream from exhaust gas cooler 23 is the tail gas of relative high-content.The air-flow that leads to WHR system 25 mixes with the tail gas of the cooling by preheater 17 as described below and purification, and the tail gas of this cooling and purification is the tail gas of relative low levels, and this is because in this preheater, by the CO in the tail gas and H
2Carried out prereduction to containing the iron supply material.
As above describe in detail, under common Metal Production situation, the caloric value that the tail gas stream of associating has makes it be suitable for the gaseous combustion that acts as a fuel.
The tail gas stream of associating, additional fuel gas source and the air of (Reference numeral 83 indications among Fig. 1) Sweet natural gas form are fed to WHR system 25, and burning within it.
The tail gas stream of associating is burning by this way in WHR system 25, that is, and and maximized destruction CO, minimized formation NO simultaneously
x
Unite with the tail gas from stove 11 from the tail gas that WHR system 25 discharges, lead to FGD system 13 then.In FGD system 13, remove SO
2, and discharge the exhaust to atmosphere by chimney 45.
Approximately contain another strand air-flow of tail gas of 35-45% volume ratio by being used for containing the fluidized-bed preheater 17 of iron supply material.This preheater 17 is removed moisture from containing the iron supply material, and carries out preheating and prereduction to containing the iron supply material.Tail gas is fluidizing agent in the preheater 17 and the source of energy.
When technology is when producing molten metal, the process controller of equipment is controlled the tail gas stream that flows to preheater 17, thereby (a) tail gas stream is controlled to be greater than minimum flow rate, keeping the fluidized state in the preheater 17, and the temperature that (b) will contain the constant of iron supply material preheater to 600 to 700 ℃ the scope.
The tail gas that discharges from preheater 17 passes through swirler 61, and isolates the dust of carrying secretly from tail gas.
Then, tail gas is by wet type taper washing tower 63, and this washing tower 63 is got rid of microparticle material and soluble gaseous species and metallic vapor from tail gas, and the temperature of tail gas is cooled to below 100 ℃ from 500 ℃ to 200 ℃, usually between 65 ℃ to 90 ℃.
Then, by exhaust gas cooler 65, this exhaust gas cooler 65 further is cooled to tail gas below 50 ℃ from the tail gas of washing tower 63, and usually between 30 ℃ to 45 ℃, removing the moisture of capacity from tail gas, thereby tail gas can be used as fuel gas.Usually, the tail gas that leaves water cooler has 5% or H still less
2O, and be lower than 10mg/Nm
3, be generally 5.0mg/Nm
3The mist amount that contains.
As mentioned above, unite with the tail gas stream from water cooler 23 then through the tail gas of cooling and purification, and in waste heat recovery (WHR) system 25, be used as fuel gas.
This WHR system 25 comprises:
Steam drum; And
Heat exchanger unit is such as overheated spiral tube and softening water water economizer.
The steam generation device of WHR system 25 comprises:
Radiation shielding for the protection of the downstream spiral tube;
Overheated of two-stage (wherein, controlling heat by injecting softening water as required, superheated vapour is maintained 420 ℃ temperature) with desuperheater control piece;
Main evaporator portion comprises three convection current spiral tube modules;
Water economizer portion; And
Sweating room has three modular softening water control pieces.
The steam that produces in WHR system 25 and tail gas cover 15 is used for driving the main air compressor (not shown) of HAB gas blower 31 and breathing equipment 29, remaining steam is by the turbine type alternator, and this turbine type alternator produces the required electric energy of operational outfit.
The turbogenerator system comprises the condensing turbine that is designed to receive superheated vapour.The surface condenser of the ejecta of turbine by under vacuum, moving, and by condensate pump institute is formed condensate pump and deliver to degasifier.
Use tail gas to offset a certain amount of electric energy as the fuel gas in the equipment, the equipment that so just makes substantially can be self-sufficient at concerned power, otherwise this a part of power supply will obtain from external electrical network.
Usually, the burner assembly 37 of WHR system 25 is the tubular carbon steel shell, and its inside is fire-resistant and insulation.
In use, because following a plurality of factors, comprise: (a) produce at the technology run duration and thereby the variation of the tail gas of discharging from container 3, (b) equipment is to the variation of steam demand, (c) can be used for the variation of tail gas of the burner assembly 37 of WHR system 25, this variation is because the competitive demand of 11 pairs of tail gas of stove is caused, (d) variation of 11 pairs of tail gas demands of stove, therefore, the burner assembly 37 of WHR system 25 moves under the situation that the associating exhaust flow from above-mentioned tail gas separated flow changes.
Described process quilt is designed in multiple " state " operation down, and these " states " have different operation conditions during the melting operating period, and these " states " for example comprise following state of the art:
(a) start;
(b) production of thermometal namely, is supplied hot ore, coal, flux and hot-blast;
(c) keep, that is, do not supply hot ore, supply coal and hot-blast;
(d) idle running namely, is not supplied ore and coal, and the fuel gas such as Sweet natural gas is supplied in the supply hot-blast in some cases; And
(e) calm, that is, do not supply ore and coal, do not supply hot-blast yet.
During maintaining condition, the caloric value of tail gas can change between low levels and the relative high-content relatively.Caloric value depends on the speed of supplying with coal in the molten bath and supplies with the speed of warm air air blast in the container 3.These parameter influences carbon content and the CO in the tail gas and the CO in the tail gas
2Content.
During idling conditions, the exhaust gas heat value is relatively low.Usually, have only container 3 (together with the purging nitrogen by 5 supplies of solid spray gun) is arrived in the warm air blast supply, the composition of tail gas just is similar to air.
During idling conditions, the thermometal temperature is monitored, and when needed, will be fed to such as the fuel gas of Sweet natural gas in the headspace of molten metal bath top.This fuel gas burns in the warm air air blast.This helps heating container 3 and molten metal bath.
The burning that fuel gas carries out by this way normally completely, thereby with wherein only provide the idling conditions of warm air air blast to compare to container 3, the caloric value of tail gas can not improve.
When technology was in the idling conditions, before container 3 combust fuel gases, the operator of container can be diverted to minimum level with slag, or even had arranged slag.The slag shunting makes the slag that leaves a certain minimum level in container 3, slag arrange then basically with all slag amount discharge containers.Reduce the level of the slag in the container 3, make metal can be directly heat by burning.Under these situations, slag has played the effect of shackle, and has reduced the heat that metal is subjected to.
In above-mentioned state of the art, the volumetric flow rate of the tail gas that produces in the container 3 is different with caloric value.For example, the flow of tail gas is relative higher during the thermometal production status with caloric value, and relatively low during idling conditions.
In addition, during given state of the art process, the volumetric flow rate of the tail gas that produces in the container 3 and caloric value are also different owing to the variation of operational conditions.For example, during the thermometal production status, operational conditions is understood some and is changed, and these variations will cause the tail gas that produces different on amount and caloric value.
In addition, the volumetric flow rate of the fuel gas that can use of WHR system 25 changed along with the stage of stove 11.Particularly, when stove 11 moved in its perfusion phase, the tail gas separated flow that leads to WHR system 25 had quite high flow.As mentioned above, compare in required tail gas amount of heating phase with stove 11, stove 11 is much lower in the required tail gas amount of its perfusion phase.
In addition, in the different states of technology, the steam of equipment (with electric power) demand is different, thereby the volumetric flow rate of the required fuel gas of WHR system 25 is also different with caloric value.For example, during the thermometal production status, the steam of equipment (and electric power) demand exceeds about 40-60% during than starting state.
In addition, in the different states of technology, the fuel gas demand of stove 11 is different.For example, during the thermometal production status, the amount of required fuel gas will be higher than idling conditions.
In view of this, during at least some state of the art, need and to be fed to the burner assembly 37 of WHR system 25 such as the optional fuel gas of Sweet natural gas (or other fuel gas outside the tail gas), thereby satisfy the steam demand of equipment during the melting operating period.
In addition, in view of this, need to change the flow such as the optional fuel gas of Sweet natural gas (or other fuel gas outside the tail gas) of the burner assembly 37 that is fed to WHR system 25, thereby compensation is from variable flow and the caloric value of the tail gas of container 3, to satisfy the steam demand of equipment during the given state of melting operating period.
In addition, in view of this, under at least some state of the art, need to be fed to the burner assembly of stove 11 such as the optional fuel gas of Sweet natural gas (or other fuel gas), with the compensation flow of tail gas and the variation of caloric value, thereby keep target flow and the target caloric value of the fuel gas that burner assembly uses.
When technology operates in calm, maintenance and the idling conditions, need the optional fuel gas of supply such as Sweet natural gas especially.During these states, the tail gas that flows to stove 11 is completely severed, or has the minimizing of certain degree at least, thereby during these state of the art, need have another fuel gas such as Sweet natural gas to keep stove 11 operations with desired level.
Therefore, the process controller of equipment provides the required flow of fuel gas and caloric value by changing the burner assembly 37 that moves WHR system 25 as the flow of the Sweet natural gas of additional fuel gas with the point of any time in technology.
Therefore, the process controller of equipment also moves the burner assembly 37 of WHR system 25 by the flow that changes air, with the variable flow of counteracting tail gas and Sweet natural gas, thereby guarantee best combustion.
Therefore, the process controller of equipment also by changing the burner assembly that moves stove 11 as the flow of the Sweet natural gas of additional fuel gas, provides the required flow of fuel gas and caloric value with the point of any time in technology.
Therefore, the process controller of equipment also moves the burner assembly of stove 11 by the flow that changes air, with the variable flow of counteracting tail gas and Sweet natural gas, thereby guarantee best combustion.
In addition, reduce in the demand owing to stove 11 inner exhaust gas, thereby before the tail gas that leads to burner assembly 37 increased, the process controller of equipment beginning oblique line formula ground in being generally 30 seconds predetermined amount of time increased the air flow quantity of the burner assembly 37 that leads to WHR system 25.
Similarly, in the increase in demand owing to stove 11 inner exhaust gas, thereby before the tail gas that leads to burner assembly 37 reduced, the process controller of equipment beginning oblique line formula ground in being generally 30 seconds predetermined amount of time reduced the air flow quantity of the burner assembly 37 that leads to WHR system 25.
For point at any time, determine the burner assembly 37 of WHR system 25 and the required gas discharge of burner assembly of stove 11, equipment is important parameters at the exhaust gas heat value of different time points.
Equipment comprises mass spectrograph CV1, CV2 and CV3, and these mass spectrographs are positioned at the selected position of equipment, in order to determine the exhaust gas heat value of these positions.Measured caloric value is handled by the process controller of described equipment, and this is that a part of determining tail gas and the required flow of Sweet natural gas is handled.
Selected position is positioned at the downstream of tail gas cover 15 (CV1), exhaust gas cooler 23 and leads to stove 11 and the upstream (CV2) of the tail gas of WHR system 25 shunting and the downstream (CV3) of preheater 61.
Move above-mentioned technology with the scope of different states and also the pressure-controlling in the container during the different states 3 is had influence.
In addition, maintain fluidized state in order to contain the iron supply material, preheater 17 has a certain minimum gas flow requirement.Control gas flow by preheater 17 by the control valve of the wet type taper washing tower 63 that is positioned at preheater 17 downstreams.
Foregoing description shows, when described explained hereafter molten pig, namely when described technology operates in the thermometal production status, controls container pressure by the control valve 77 of wet type taper washing tower 21.
More specifically, equipment comprises the pressure transmitter P1 that is positioned at tail gas cover 15, and this pressure transmitter is monitored the tail gas pressure that flows through the tail gas cover with continuous form.When technology operated in the thermometal production status, the process controller of equipment was in response to the pressure of monitoring, and the control valve 77 of operation wet type taper washing tower 21, thereby regulates pressure as required, preferably keeps constant container pressure.The time constant of the pilot circuit of control valve 77 is significantly less than the time constant of the pilot circuit of the control valve in the washing tower 63 in preheater 17 downstreams.Therefore, the pressure in control container 3 and control during Metal Production, mainly are that container pressure is controlled with regard to the control between the gas flow of preheater 17.
During other states of technology, especially during maintenance and idling conditions, still be necessary to keep the control to the pressure in the container 3.During these states, such pressure-controlling is to realize by the above-mentioned control valve in the wet type taper washing tower 63 in preheater 17 downstreams rather than by the control valve 77 of wet type taper washing tower 21.
More specifically, when technology operates in these states, the control valve 77 of wet type taper washing tower 21 is closed at least basically, thereby does not have tail gas stream or minimum tail gas stream is only arranged at the most by washing tower 21, enters stove 11 and WHR system 25 then from this source.Therefore, during maintenance and idling conditions, the control valve in the wet type taper washing tower 63 becomes main pressure controller.This has also guaranteed the gas flow by preheater, so that metal-containing material is maintained in the fluidized state.
In addition, when technology became in maintenance and the idling conditions, process controller moved to reduce the flow set point that is fed to the warm air air blast of container 3 from stove 11.The pressure set-point of container also is lowered.Usually, the set-point is reduced to gauge pressure 0.4 bar from gauge pressure 0.8 bar.
During maintenance and idling conditions, a part of tail gas by preheater 17 is recycled, and unites with the tail gas from container 3, thereby helps to keep the fluidization conditions in the preheater 17.
Under windless condition, not to the air blast of container supply warm air.Close the washing tower 63 in preheater 17 downstreams, and all tail gas in the preheater 17 are carried out recycle, thereby move as fluidizing agent.
During maintenance and idling conditions, the warm air blast volume that stove 11 produces reduces.Be no more than top temperature in order to ensure stove 11, and during the thermometal production status, compare to the total energy of stove supplied fuel gas, reduce the total energy to stove 11 supplied fuel gases.Like this, during maintenance and idling conditions, the energy that is input to stove 11 reduces, thereby is complementary with the reduction of the warm air air blast stream that reduces to energy requirement.
Under situation without departing from the spirit and scope of the present invention, can make multiple change to the embodiment of the invention described above.
Claims (17)
1. direct melting technology, described direct melting technology is used for the state of the art direct melting metal-containing supplying material in direct melting container in " thermometal production ", and produce the process products of molten metal, slag and tail gas from described direct melting container, described direct melting container forms the part of direct melting equipment, and described direct melting technology comprises:
(a) according to required given processing condition, in a plurality of state of the art, optionally move described technology, described state of the art comprises described " thermometal production " state and " maintenance " state and " idle running " state, in described " thermometal production " state, melting metal-containing supplying material in described container, to produce molten metal, in described " maintenance " state and " idle running " state, the molten bath of melting material maintains in the described direct melting container with molten state, and does not produce extra molten metal;
(b) when described technology operates in described " thermometal production " state, to be divided at least two bursts of tail gas stream from the tail gas that described direct melting container discharges, and one tail gas stream supplied to the fluidized-bed pretreatment unit, be fed into the metal-containing supplying material of described direct melting container subsequently with pre-treatment, and another burst tail gas stream is supplied to (i) waste heat recovery unit and (ii) at least one in the stove, wherein said waste heat recovery unit is for generation of the steam that uses in described technology, and described stove is for generation of the warm air air blast of using in described technology;
(c) when described technology operates in described " maintenance " state and " idle running " state, to supply to described fluidized-bed pretreatment unit from the tail gas stream that described direct melting container discharges, be fed into the metal-containing supplying material of described direct melting container with fluidisation at least subsequently; And
(d) when described technology operates in described " maintenance " state and " idle running " state, by the tail gas pressure of control in the tail gas stream that supplies to described fluidized-bed pretreatment unit, control the pressure in the described direct melting container.
2. technology according to claim 1, comprise: in the time of in described when operating in " thermometal production " state, supplying to described equipment with as the exhaust flow in described another burst tail gas stream of fuel gas, control the pressure in the described direct melting container by control.
3. technology according to claim 1 and 2, wherein, described " maintenance " state comprises: warm air air blast or hot oxygen-rich air air blast, solid carbon-containing material and flux are supplied to described direct melting container, and do not supply with metal-containing material.
4. technology according to claim 1 and 2, wherein, described " idle running " state comprises: warm air air blast or hot oxygen-rich air air blast are supplied to described direct melting container, and do not supply with metal-containing material and solid carbon-containing material.
5. technology according to claim 1 and 2 comprises: in the water scrubber in the downstream of described pretreatment unit, and cooling and remove microparticle material and soluble gas kind and metallic vapor from the tail gas stream that supplies to described fluidized-bed pretreatment unit.
6. technology according to claim 5, wherein step (d) comprising: when described technology operates in described " maintenance " state and " idle running " state, by opening or closing the tail gas control valve in the described washer, control the flow of the tail gas of the described washer of flowing through, thereby control the pressure in the described direct melting container.
7. technology according to claim 1 and 2, wherein step (c) comprising: when described technology operates in described " maintenance " state and " idle running " state, to supply to described fluidized-bed pretreatment unit as tail gas stream from whole tail gas stream that described direct melting container discharges, and therefore minimize any tail gas shunting.
8. technology according to claim 1 and 2, comprise: when described technology operates in described " maintenance " state and " idle running " state, with another fuel gas supply to stove, warm air air blast or hot oxygen-rich air air blast that described stove is used for generation of described technology.
9. technology according to claim 1 and 2, comprise: when described technology operates in described " maintenance " state and " idle running " state, Sweet natural gas is supplied to stove, warm air air blast or hot oxygen-rich air air blast that described stove is used for generation of described technology.
10. technology according to claim 1 and 2, comprise: when described technology operates in described " thermometal production " state, in the water scrubber of the upstream of described stove and described waste heat recovery unit, cooling and remove microparticle material and soluble gas kind and metallic vapor from described another burst tail gas stream.
11. technology according to claim 10 comprises: when the beginning of described " maintenance " state and " idle running " state, be closed in the tail gas control valve in the described water scrubber.
12. technology according to claim 1 and 2 comprises: will supply to described waste heat recovery unit from the tail gas of described pretreatment unit, as fuel gas, with the steam of using for generation of described technology.
13. technology according to claim 1 and 2 comprises: during described " maintenance " state and " idle running " state, a part that supplies to the described tail gas stream of the described fluidized-bed pretreatment unit in the described pretreatment unit is carried out recycling.
14. technology according to claim 1 and 2, comprise: when described technology operates in described " thermometal production " state, with first volumetric flow rate warm air air blast or hot oxygen-rich air air blast are supplied to described direct melting container, and when described technology operates in described " maintenance " state and " idle running " state, with the second lower volumetric flow rate warm air air blast or hot oxygen-rich air air blast are supplied to described direct melting container.
15. technology according to claim 1 and 2, comprise: when described technology operates in described " thermometal production " state, with the pressure-controlling in the described direct melting container to the first pressure set-point, and when described technology operates in described " maintenance " state and " idle running " state, the pressure-controlling in the described direct melting container is arrived lower pressure set-point.
16. technology according to claim 1 and 2, be included in the molten metal temperature in the described direct melting container of monitoring during described " idle running " state, and the described fuel gas that as required fuel gas supply burnt to described container and in described container is to keep the described molten metal temperature in the described container.
17. technology according to claim 2 comprises: be in described container, during the described fuel gas of burning, to reduce the level of the slag in the described direct melting container when described technology operates in described " idle running " state and described technology.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2006902130 | 2006-04-24 | ||
| AU2006902130A AU2006902130A0 (en) | 2006-04-24 | Off-gas processing in direct smelting process | |
| PCT/AU2007/000542 WO2007121536A1 (en) | 2006-04-24 | 2007-04-24 | Pressure control in direct smelting process |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012105261352A Division CN103060503A (en) | 2006-04-24 | 2007-04-24 | Pressure control in direct smelting process |
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| Publication Number | Publication Date |
|---|---|
| CN101473050A CN101473050A (en) | 2009-07-01 |
| CN101473050B true CN101473050B (en) | 2013-07-03 |
Family
ID=38624477
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007800226472A Active CN101473050B (en) | 2006-04-24 | 2007-04-24 | Pressure control in direct smelting process |
| CN2012105261352A Pending CN103060503A (en) | 2006-04-24 | 2007-04-24 | Pressure control in direct smelting process |
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| CN2012105261352A Pending CN103060503A (en) | 2006-04-24 | 2007-04-24 | Pressure control in direct smelting process |
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| Country | Link |
|---|---|
| US (1) | US20100011908A1 (en) |
| CN (2) | CN101473050B (en) |
| WO (1) | WO2007121536A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| NZ608909A (en) * | 2010-09-15 | 2015-02-27 | Tech Resources Pty Ltd | Direct smelting process |
| UA113295C2 (en) * | 2011-12-06 | 2017-01-10 | Текнолоджікал Рісорсес Пті. Лімітед | Starting a smelting process |
| UA113296C2 (en) * | 2011-12-06 | 2017-01-10 | Текнолоджікал Рісорсес Пті. Лімітед | Starting a smelting process |
| JP5818704B2 (en) * | 2012-01-25 | 2015-11-18 | 三菱日立パワーシステムズ株式会社 | Gasification furnace, gasification power plant |
| WO2014071464A1 (en) * | 2012-11-12 | 2014-05-15 | Technological Resources Pty. Limited | A two-stage smelting process and apparatus |
| CN103409576B (en) * | 2013-08-14 | 2015-10-14 | 北京首钢国际工程技术有限公司 | A kind of direct smelting furnace gas energy reclaims and dry dedusting technology |
| CN103468847B (en) * | 2013-08-14 | 2015-04-15 | 北京首钢国际工程技术有限公司 | Iron bath method high temperature gas waste heat and waste energy utilization and dry method dedusting technology |
| CN107532223A (en) * | 2015-02-03 | 2018-01-02 | 技术资源有限公司 | The processing of low calorific value waste gas |
| WO2017014699A1 (en) * | 2015-07-23 | 2017-01-26 | Limastian Narong | Method of utilizing furnace off-gas for reduction of iron oxide pellets |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2576607A1 (en) * | 1985-01-25 | 1986-08-01 | Montereau Acieries | Process for preheating scrap iron and iron or steel scrap |
| US6519942B2 (en) * | 2001-01-23 | 2003-02-18 | Reginald Wintrell | Systems and methods for harvesting energy from direct iron-making off gases |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2715536C2 (en) * | 1977-04-07 | 1982-07-15 | Bergwerksverband Gmbh | Method and device for recovering waste heat from coke ovens |
| SU1013490A1 (en) * | 1981-09-07 | 1983-04-23 | Украинский Государственный Институт По Проектированию Металлургических Заводов | Method for making steel in oxygen converter |
| US5258054A (en) * | 1991-11-06 | 1993-11-02 | Ebenfelt Li W | Method for continuously producing steel or semi-steel |
| JPH0743081A (en) * | 1993-07-30 | 1995-02-10 | Sumitomo Metal Mining Co Ltd | Control method of internal pressure of self-fluxing furnace |
| AUPP483898A0 (en) * | 1998-07-24 | 1998-08-13 | Technological Resources Pty Limited | A direct smelting process & apparatus |
| AUPQ083599A0 (en) * | 1999-06-08 | 1999-07-01 | Technological Resources Pty Limited | Direct smelting vessel |
| AUPQ152299A0 (en) * | 1999-07-09 | 1999-08-05 | Technological Resources Pty Limited | Start-up procedure for direct smelting process |
| AUPQ205799A0 (en) * | 1999-08-05 | 1999-08-26 | Technological Resources Pty Limited | A direct smelting process |
| AUPQ213099A0 (en) * | 1999-08-10 | 1999-09-02 | Technological Resources Pty Limited | Pressure control |
| AUPQ346399A0 (en) * | 1999-10-15 | 1999-11-11 | Technological Resources Pty Limited | Stable idle procedure |
| US6602321B2 (en) * | 2000-09-26 | 2003-08-05 | Technological Resources Pty. Ltd. | Direct smelting process |
| WO2005083130A1 (en) * | 2004-02-27 | 2005-09-09 | Technological Resources Pty. Limited | Direct smelting plant and process |
-
2007
- 2007-04-24 CN CN2007800226472A patent/CN101473050B/en active Active
- 2007-04-24 US US12/298,349 patent/US20100011908A1/en not_active Abandoned
- 2007-04-24 CN CN2012105261352A patent/CN103060503A/en active Pending
- 2007-04-24 WO PCT/AU2007/000542 patent/WO2007121536A1/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2576607A1 (en) * | 1985-01-25 | 1986-08-01 | Montereau Acieries | Process for preheating scrap iron and iron or steel scrap |
| US6519942B2 (en) * | 2001-01-23 | 2003-02-18 | Reginald Wintrell | Systems and methods for harvesting energy from direct iron-making off gases |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2007121536A1 (en) | 2007-11-01 |
| CN103060503A (en) | 2013-04-24 |
| CN101473050A (en) | 2009-07-01 |
| US20100011908A1 (en) | 2010-01-21 |
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Effective date of registration: 20180928 Address after: No. 999 Wensheng street, Shouguang, Shandong Patentee after: SHANDONG MOLONG PETROLEUM MACHINERY Co.,Ltd. Address before: Australia Melbourne Patentee before: TECHNOLOGICAL RESOURCES Pty Ltd. |
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| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20090701 Assignee: Hebei Xinggang Technology Co.,Ltd. Assignor: SHANDONG MOLONG PETROLEUM MACHINERY Co.,Ltd. Contract record no.: X2023980034949 Denomination of invention: Pressure Control in Direct Melting Process Granted publication date: 20130703 License type: Common License Record date: 20230423 |