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CN101473048A - Direct smelting plant with waste heat recovery unit - Google Patents

Direct smelting plant with waste heat recovery unit Download PDF

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Publication number
CN101473048A
CN101473048A CNA2007800226241A CN200780022624A CN101473048A CN 101473048 A CN101473048 A CN 101473048A CN A2007800226241 A CNA2007800226241 A CN A2007800226241A CN 200780022624 A CN200780022624 A CN 200780022624A CN 101473048 A CN101473048 A CN 101473048A
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CN
China
Prior art keywords
gas
fuel gas
tail gas
unit
heat recovery
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Granted
Application number
CNA2007800226241A
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Chinese (zh)
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CN101473048B (en
Inventor
罗德尼·詹姆士·德赖
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Shouguang Maolong New Material Technology Development Co ltd
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Technological Resources Pty Ltd
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Priority claimed from AU2006902129A external-priority patent/AU2006902129A0/en
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Publication of CN101473048A publication Critical patent/CN101473048A/en
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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
    • F27D17/10—Arrangements for using waste heat
    • 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
    • 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
    • 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
    • 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
    • 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; Electric arc furnaces ; Tank furnaces
    • F27B3/10—Details, accessories or equipment, e.g. dust-collectors, specially adapted for hearth-type furnaces
    • F27B3/22—Arrangements of air or gas supply devices
    • F27B3/225—Oxygen blowing
    • 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; Electric arc furnaces ; Tank furnaces
    • F27B3/10—Details, accessories or equipment, e.g. dust-collectors, specially adapted for hearth-type furnaces
    • F27B3/26—Arrangements of heat-exchange apparatus
    • 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
    • F27D13/00—Apparatus for preheating charges; Arrangements for preheating charges
    • 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
    • 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
    • C21B2100/42—Sulphur removal
    • 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
    • C21B2100/62—Energy conversion other than by heat exchange, e.g. by use of exhaust gas in energy production
    • 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
    • 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
    • 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
    • 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
    • Y02P10/25—Process efficiency

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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

公开了一种用于通过直接熔炼工艺从含金属供给材料生产熔融金属的直接熔炼设备。该设备包括工艺控制器，用于调节向运行单元中的至少一个的燃烧器单元供应的燃料气体的体积流量，以至少达到所述设备为了运行该直接熔炼工艺的所选要求。

Figure 200780022624

A direct smelting plant for producing molten metal from metal-containing feed material by a direct smelting process is disclosed. The plant comprises a process controller for regulating the volume flow of fuel gas supplied to the burner unit of at least one of the operating units to at least meet the selected requirements of said plant for operating the direct smelting process.

Figure 200780022624

Description

Direct melting equipment with waste heat recovery unit
Technical field
The present invention relates to a kind of based on molten metal bath direct melting equipment and be used for producing the technology of molten metal at direct melting container.
Particularly, the present invention relates to from the energy recovery of the tail gas of direct melting container discharge.
The present invention especially but and not exclusively relate to the direct melting technology that is used for supplying with the material produce molten pig based on molten metal bath from ferruginous metal, these ferruginous metals are supplied with materials: iron ore, partial reduction iron ore and iron content waste streams (the iron content waste streams that for example, comes from steelworks).
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 of powdered form; And (ii) solid carbon-containing material, be generally coal, as the reductive agent and the energy source of metal-containing supplying material; And
(c) with the supply material melting of metal be iron in the molten bath.
Here, term " melting " is interpreted as being meant a kind of thermal treatment, wherein carries out metal oxide reductive chemical reaction to produce molten metal.
In HIsmelt technology, thereby metal-containing supplying material and solid carbon-containing material are injected into molten metal bath by a plurality of with respect to the downward spray gun/blast orifice that inwardly passes the sidewall of direct melting container and enter in this container lower region of vertical direction inclination, thereby near small part solid matter is transported to the metal level that is positioned at container bottom.Spray gun by downward extension injects the upper area of container with the oxygen-containing gas stream (being generally air or oxygen-rich air) of heat, thereby the reactant gases that molten metal bath is discharged carries out the afterfire reaction in the upper area of container.Usually, under the situation of producing molten pig, the temperature of warm air or 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 of 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 the direct melting in an independent compact container, is generally 0.5Mt/a at least.
Yet, in order in HIsmelt technology, to obtain high molten pig productivity, need (a) to produce a large amount of warm airs or oxygen-rich air and carrier gases (being used for solid injects), and with these gas delivery 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) transport a large amount of hot exhaust gas from container, (d) transport a large amount of molten pigs and the slag that produces from container this technology, and (e) a large amount of water is circulated by cooled plate, all these carries out in the zone of relative closure.
In view of this, high molten pig productive rate needs a kind of like this HIsmelt equipment, it comprises the direct melting container and the supplementary unit of (a) pressurization, supply with the lock hopper of material and be positioned at pressure control device on the exhaust pipe of container to container supply solid such as being used for, (b) produce the stove of high flow capacity warm air or 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.
Propose, use during the melting operating period from least a portion in the tail gas of direct melting container as the fuel gas that comprises in the exhaust gas processing device of waste heat recovery unit, more specifically, as the fuel gas in the burner unit of the waste heat recovery stove of waste heat recovery unit, this waste heat recovery unit produces and is used for (a) generating and (b) steam of operation HIsmelt technology.
Here, term " melting operating period " should be understood to mean the direct melting technology based on molten metal bath, such as the operational process of HIsmelt technology, and not exclusively stops to relate to the technology that finally flows out molten metal and slag from direct melting container.
But also propose, using during the melting operating period from least a portion in the tail gas of direct melting container as the fuel gas in the burner unit of stove, this stove produces air or the oxygen-rich air that is used for HIsmelt technology.
During the melting operating period, from the tail gas of direct melting container may use the above-mentioned operation unit that is not limited to move waste heat recovery unit and stove, but can be with tail gas as at the fuel gas that moves as outside an equipment part and/or the equipment other in unitary burner unit.
A kind of HIsmelt process quilt of current proposition is designed to have multiple " state " operation down of different operation conditions during the melting operating period, these states for example comprise following state of the art:
(a) start;
(b) production of thermometal, that is, supply is through pretreated metal-containing supplying material, such as hot ore, such as the solid carbon-containing material and the warm air air blast of coal;
(c) keep, that is, do not supply through pretreated metal-containing supplying material supply solid carbon-containing material and warm air air blast;
(d) idle running promptly, is not supplied the pretreated metal-containing supplying material of process and is not supplied solid carbon-containing material, the air blast of supply warm 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 warm air air blast yet.
Usually, the volumetric flow rate at the tail gas that produces in direct melting container under the above-mentioned state of the art is different.For example, the flow of tail gas is higher usually during the thermometal production status, and the flow of tail gas is lower usually during idling conditions.In further example, during windless condition, do not have tail gas usually, during idling conditions, do not have caloric value in the tail gas usually.
The volumetric flow rate and the caloric value of the tail gas that produces in direct melting container in the given state of the art process also can be different owing to the variation of the running status during this state of the art.For example, running status can change during the Metal Production state, and the tail gas that these changes will cause producing has different flows and caloric value.
Therefore, the applicant recognizes, during at least some states of HIsmelt technology, need and/or be that the difference of this device external is moved the operating requirement that unitary burner unit (or fuel element of other types) supply Sweet natural gas (or other fuel gas outside the tail gas) reaches this equipment or outside operation parts to a part that forms specific HIsmelt equipment.
For example, under the situation of above-mentioned HIsmelt equipment, need reach the steam requirement of this equipment during the melting operating period to the burner unit supply Sweet natural gas (or other fuel gas outside the tail gas) of waste heat recovery unit.
In addition, under the situation of above-mentioned HIsmelt equipment, the applicant has had recognized the need to the burner unit supply Sweet natural gas (or other fuel gas outside the tail gas) to stove, compensates flow that is changing and caloric value from the tail gas of direct melting container.
In addition, under the situation of above-mentioned HIsmelt equipment, the applicant recognizes, need to change during given supply status flow to the Sweet natural gas (or other fuel gas outside the tail gas) of the burner unit supply of the burner unit of waste heat recovery unit and stove, compensate during this supply status flow that is changing and caloric value, to reach the operating requirement of this equipment from the tail gas of direct melting container.
In addition, the applicant recognizes that therefore the velocity of variation of the caloric value of the tail gas that produces in the HIsmelt technology need be monitored the caloric value of tail gas nearly probably significantly greater than the situation in the blast furnace.
Summary of the invention
On wide in range meaning, the invention provides a kind of direct melting equipment, it is used for producing molten metal by direct melting technology from metal-containing supplying material, and this direct melting equipment comprises:
(a) direct melting container is used for producing molten metal, slag and tail gas by the technology in the direct melting metal-containing supplying material of described container;
(b) the first fuel gas feeding mechanism is used to supply from the tail gas of described direct melting container to move the fuel gas in the unitary burner unit as two or more of described equipment and/or described device external;
(d) the second fuel gas feeding mechanism is used for from another source supplying another fuel gas at least one burner unit of described operation unit, Sweet natural gas for example, and
(e) process controller is used for regulating the volumetric flow rate of burner unit supplied fuel gas at least one of described operation unit, to reach described equipment at least in order to move the selected requirement of this direct melting technology.
Depend on the circumstances, the term " fuel gas " that uses in above-mentioned paragraph (e) can refer to tail gas and/or such as another fuel gas of Sweet natural gas.
Although be not unique possible, a kind of operation unit can be a waste heat recovery unit, and it is used for producing steam using at described equipment, and/or be used for generating and use for described equipment or use outside described equipment.
Although be not unique possible, another kind of operation unit can be a plurality of stoves, is used to produce warm air air blast or hot oxygen-rich air air blast, to use in this direct melting technology.
The described second fuel gas feeding mechanism can be suitable for the fuel gas to described waste heat recovery unit and/or described stove supply such as Sweet natural gas.
Described process controller can be suitable for the volumetric flow rate of the fuel gas of the described burner unit that is supplied to described waste heat recovery unit is regulated.
Particularly, described process controller can be suitable for the volumetric flow rate such as the fuel gas of Sweet natural gas of the described burner unit that is supplied to described waste heat recovery unit via the second fuel gas feeding mechanism is regulated.
Described process controller can be suitable for the volumetric flow rate of the fuel gas of the described burner unit that is supplied to described stove is regulated.
Particularly, described process controller can be suitable for the volumetric flow rate such as the fuel gas of Sweet natural gas of the described burner unit that is supplied to described stove via the second fuel gas feeding mechanism is regulated.
As mentioned above, the HIsmelt technological design of the current proposition of applicant becomes in different " state " operation down, therefore under these states and in the process at given state, the volumetric flow rate of the tail gas that produces in the described direct melting container and caloric value can be different.In addition, the demand to steam (via described waste heat recovery unit) and/or warm air or oxygen-rich air (via described stove) can be different under different states in order to move described HIsmelt technology for equipment, and can change in the process of given state.Therefore, according to the utilizable flow and the caloric value of tail gas of arbitrary preset time of point, may need generation to (a) described HIsmelt equipment be used for described technology enough steam waste heat recovery unit and/or (b) generation of described HIsmelt equipment be used for the enough warm airs of described technology or the stove supply Sweet natural gas (and/or other fuel gas) of oxygen-rich air.
Preferably, described process controller requires and/or in response to the warm air or the oxygen-rich air requirement of described technology in response to the flow of tail gas and/or caloric value and in response to the steam of described equipment, thereby consider the flow of tail gas on the time point in office and/or the requirement of caloric value and described equipment and/or described technology, come to determine need by the volumetric flow rate such as the fuel gas of Sweet natural gas of the second fuel gas feeding mechanism to the burner unit supply of described stove and/or described waste heat recovery unit.
Preferably, described process controller is in response to the flame temperature of the described burner unit of described waste heat recovery unit.
More preferably, described process controller is higher than minimum temperature in response to the flame temperature of the described burner unit of described waste heat recovery unit so that described flame temperature is maintained in.
Preferably, as described above, described process controller passes through with reference to the desirable value of steam flow during the different running statuses of described technology or vapor pressure in response to the steam demand of described equipment.
Preferably, described process controller is suitable for the volumetric flow rate of the fuel gas of the described burner unit that is fed to described stove by the described second fuel gas feeding mechanism is regulated, and has predetermined flow and/or caloric value so that be fed to the associating fuel gas of the burner unit of described stove.
Preferably, described process controller is suitable for the flow of the fuel gas of the described burner unit that is fed to described stove by the described second fuel gas feeding mechanism is regulated, so that the burner unit of described stove is moved with the constant caloric value when the heating phase of described stove begins at least.
Preferably, described equipment comprises and is used for device that the exhaust gas heat value at the different positions place of described equipment is monitored.
Described exhaust gas heat value monitoring device can be for such as mass spectrometric any appropriate device.
Preferably, described process controller is in response to the monitoring value to caloric value.
Preferably, described equipment comprises the operation unit that is the pretreatment unit form, and this pretreatment unit is used for metal-containing supplying material is carried out pre-treatment.
Preferably, described equipment comprises the device that is used for from described direct melting container supply tail gas, and this tail gas is as the fluidizing agent in the described pretreatment unit.
Preferably, described equipment comprises a device, and the tail gas that this device is used for discharging from described direct melting container is divided into second plume that (i) is used for first plume of described stove and described waste heat recovery unit and (ii) is used for described pretreatment unit.
Preferably, described equipment comprises a device, and this device is used for and will forms the associating tail gas stream from tail gas of (i) described first plume and the tail gas by from described pretreatment unit discharge in (ii) described second plume.
Preferably, described exhaust gas heat value monitoring device is suitable for the caloric value of the tail gas in the described associating tail gas stream is monitored.
Preferably, described process controller is in response to the caloric value of the tail gas in the described associating tail gas stream being monitored gained.
Preferably, described process controller is suitable in response to the caloric value of described associating tail gas stream being monitored gained, and to being regulated to the volumetric flow rate of described waste heat recovery unit supplied fuel gas via the described second fuel gas feeding mechanism.
Preferably, described exhaust gas heat value monitoring device is suitable for the caloric value of the tail gas in described first plume and described second plume is monitored.
On wide in range meaning, also provide a kind of being used for to comprise in the direct melting technology based on molten metal bath of direct melting equipment from metal-containing supplying material production molten metal according to the present invention:
(a) in the direct melting container of the molten metal bath that comprises metal and slag metal-containing supplying material is carried out direct melting, and produce molten metal, slag and tail gas, this technology has different state of the art;
(b) tail gas that will during the melting operating period, produce in the described container act as a fuel that gas is fed to described equipment and/or described device external two or more move unitary burner unit, and
(c) another fuel gas of the supply of at least one to described operation unit such as Sweet natural gas from another source,
(d) in the process of described technology, the volumetric flow rate of the fuel gas that is fed to the unitary described burner unit of described operation is regulated, thereby satisfied the demand of described equipment at least.
Preferably, described operation unit comprises the recovery of heat stove of waste heat recovery unit, and described waste heat recovery unit is used to produce for the steam that uses in described equipment and/or produces the electric power that uses or use in described equipment outside described equipment.
Preferably, described operation unit comprises a plurality of stoves, and described a plurality of stoves are used to be created in and metal-containing supplying material are carried out used warm air air blast of direct melting or hot oxygen-rich air air blast in the described container.
Preferably, described technology also comprises is regulated the volumetric flow rate of another fuel gas of the burner unit that is fed to described waste heat recovery unit and/or described stove, thereby keeps predetermined amount of flow and/or the caloric value that leads to described burner unit.
Preferably, described technology comprises the caloric value of the tail gas at described equipment different positions place is monitored.
According to the present invention, also provide a kind of being used for to comprise by the direct melting equipment of direct melting technology from metal-containing supplying material production molten metal:
(a) direct melting container, it is used for producing molten metal, slag and tail gas by the technology in the direct melting metal-containing supplying material of described container;
(b) at least two tail gas treating units that are used to receive with combustion tail gas;
(c) the first fuel gas feeding mechanism, it is used for from described direct melting container supply tail gas, to use in the burner unit of described tail gas treating unit;
(d) the second fuel gas feeding mechanism, it is used for from another source another fuel gas to burner unit supply such as the Sweet natural gas of described at least two tail gas treating units;
(e) process controller is used for control:
I) volumetric flow rate of one tail gas in the described tail gas treating unit is led in control, with satisfied this unitary demand, and remaining tail gas is fed to other one or more tail gas treating units;
Ii) the volumetric flow rate of described another fuel gas of described tail gas treating unit is led in control.
Preferably, described tail gas treating unit comprises the stove and the waste heat recovery unit that is used to produce steam that is used for to described direct melting container supply hot-blast.
Preferably, described process controller is suitable for the supply of the tail gas that leads to described stove and another fuel gas is controlled, and makes the joint supply of the tail gas that leads to described stove and another fuel gas have the caloric value of constant.
Preferably, described process controller is suitable for the supply of another fuel gas of the described waste heat recovery unit of subtend in response to the variation of exhaust gas volumes flow to be controlled, thereby realizes the burning of tail gas in described waste heat recovery unit.
Preferably, described equipment comprises: one or more tail gas supply valves, described tail gas supply valve are used to control the volumetric flow rate of the tail gas that leads to described stove and are used to turn to into supplying tail gas to described waste heat recovery unit; And exhaust gas heat value sensing apparatus, this exhaust gas heat value sensing apparatus is used for the caloric value of sensing tail gas, and wherein, described process controller is suitable for monitoring the exhaust gas heat value, and be reduced under the predetermined threshold, and move described one or more tail gas supply valve so that tail gas is diverted to described waste heat recovery unit in response to the caloric value of described tail gas.
Preferably, described predetermined threshold is such value, that is, tail gas when this value no longer the caloric value to the associating fuel gas stream of tail gas and another fuel gas positive contribution is arranged.
Preferably, described predetermined threshold is 1.8MJ/Nm 3(the every standard cubic meter of megajoule).
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 coming melting to contain the iron supply material according to this melting equipment of HIsmelt process using described in International Application PCT/AU96/00197 of the applicant, thereby produce molten pig.Here, the disclosure in the patent specification that is comprised in conjunction with this international application this patent by cross reference.
This technology is based on the use of direct melting container 3.
Container 3 is containers of the sort of type described in detail in the applicant's International Application PCT/AU2004/000472 and PCT/AU2004/000473.By cross reference in conjunction with the disclosure in the patent specification that these international applications comprised.
Container 3 has: siege, this siege comprise bottom and the side that is formed by refractory brick; Sidewall, this sidewall form from the upwardly extending tube that roughly is cylindricality of the side of siege, and comprise top cylinder portion and doffing portion; Furnace roof; Be positioned at the exhaust pipe 9 on container 3 tops; Be used for discharging continuously the forehearth 67 of molten metal from container 3; And the slag notch that is used for regularly discharging slag from container 3.
Container 3 is equipped with water-cooled warm air air blast (" HAB ") spray gun 7 and eight water-cooled solid spray guns 5 of downward extension, this warm air air blast spray gun 7 extends into the upper space of container 3, and described solid spray gun 5 extends internally downwards and passes sidewall and enter in the slag.
In use, container 3 contains the molten pig molten bath.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) and directly injected the molten bath via solid spray gun 5.
Particularly, one group of spray gun 5 is used to inject ferruginous supply material and flux, and another group spray gun 5 is used to inject coal and flux.
Spray gun 5 is protected their not receptor 3 interior pyritous influences 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 be subjected to pre-treatment by being preheating to 600 to 700 ℃ of temperature in the scope, and before injecting the molten bath at fluidized-bed preheater 17 by prereduction.
Inject at ambient temperature before the molten bath, coal and flux are stored in a series of lock hoppers 25.Coal is fed to lock hopper 25 via coal drying and grinding equipment 71.
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 process 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 from the afterfire reaction in this zone of transition, and turn back to slag/iron bath, thus energy is transferred to the molten bath.
The oxygen-rich air that is injected into the heat in the container 3 via HAB spray gun 7 produces in hot blast stove 11 by this way, promptly, make oxygen-rich air (nominally oxygen level is 30 to 35% volumes) by stove 11, and, be responsible for 41 oxygen-rich air via hot-blast afterwards and be transported to HAB spray gun 7 heat to air heating.
The operation of stove 11 is adjusted to can guarantee to have in the person in charge 41 successive, unbroken hot oxygen-rich air to flow to HAB spray gun 7 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 time period in this heat exchange stage is longer than the heating phase.
During the heating phase of stove 11, heat stove 11 in the following manner, i.e. burning (a) is cooling and the fuel gas of cleaning of off-gas form and/or (b) optional another fuel gas from container 3, such as Sweet natural gas (being supplied) by the pipeline shown in the Reference numeral among Fig. 1 85, 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, be mixed in the charge air flow that gas blower 31 produced from the oxygen of breathing equipment 29.These oxygen-rich air streams pass through stove 11, and are heated in stove 11, thereby are the oxygen enrichment charge air flow that container 3 produces heat.These hot oxygen-rich air circulations often are called as " hot-blast " or " warm air air blast ".
The perfusion phase of stove 11 is such stages, that is, wherein in the stove closes substantially, and (with geseous fuel gas, such as Sweet natural gas) heating heat exchange of also not being subjected to carry out with airflow is cooled off neither to be subjected to combustion tail gas.
The time length of the perfusion phase of given stove 11 is at least and opens and closes the required time quantum of valve, (a) switches to heat exchange stage and (b) another stove from heat exchange stage switched to heating phase required from the heating phase given stove thereby the opening and closing of these valves are conversion tail gas and hot blast.
In flue gas desulfurization (FGD) system 13, purify the products of combustion that stove 11 is discharged in its heat-processed.This FGD removes usually with hydrogen sulfide (H from products of combustion 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 the tail gas of heating and combustion air.The tail gas of container and combustion air can be preheated to 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 being created in the steam of steam drum 35 inner accumulated.This tail gas cover can be a United States Patent (USP) 6,585, the tail gas cover of the sort of type of 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.
Washing tower 21 makes the tail gas quenching of flowing through wherein, and gets rid of microparticle material and soluble gaseous species and metallic vapor from flow through tail gas wherein.The temperature of tail gas drops to below 100 ℃ from about 1000 ℃ in washing tower, usually between 65 ℃ to 90 ℃.
Washing tower 21 comprises upper chamber 71, lower chambers 73 and makes upper chamber 71, lower chambers 73 interconnected extend perpendicular pipes 75.Washing tower 21 comprises the tail gas control valve 77 that is positioned at pipe 75 lower ends.This control valve 77 comprises the conical component 79 of hydraulic running, and this conical component energy vertical movement is to open or close the lower end of pipe 75.Washing tower 21 comprises water-jet 69 in upper chamber 71, and with respect to pipe 75 and controlling elements 79 localized other water-jet (not shown).Make up water and the recirculated water in washing tower are provided to water-jet.
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 being controlled to gauge pressure is 0.8 crust.
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 is produced is suitable for use as (a) stove 11 (as mentioned above) and (b) fuel gas in the WHR system 25.In addition, be suitable in dry and grinding equipment 71, coal being carried out drying through washing and refrigerative tail gas.
For above purpose, to be divided into three strands of air-flows from the tail gas of gas cooler 23, and the device by being generically and collectively referred to as " the first fuel gas feeding mechanism " is fed to the operation unit in downstream with this tail gas, and these operation unit are specially stove 11, WHR system 25 and drying and grinding equipment 71.Particularly, one air communication is to stove 11, another burst air communication to 25, the three bursts of air communication of WHR system to dry and grinding equipment 71.The flow of tail gas is controlled via tail gas supply valve (not shown) in the air-flow.
Tail gas stream from exhaust gas cooler 23 is high-load relatively tail gas.The air-flow that leads to WHR system 25 mixes by the cooling of preheater 17 and the tail gas of purification with as described below, and the tail gas of this cooling and purification is the tail gas of relative low levels, and this is because of the CO and the H that pass through in this preheater in the tail gas 2Carried out containing the prereduction of iron supply material.
As above describe in detail, under common Metal Production situation, the caloric value that tail gas stream had of associating makes it be suitable for the gaseous combustion that acts as a fuel.
The tail gas stream of associating, another source and the air that is the fuel gas (being supplied by the pipeline shown in the Reference numeral among Fig. 1 83) of Sweet natural gas form are supplied to WHR system 25, and burning within it.
It should be noted that under the situation of WHR system 25 supply Sweet natural gases, pipeline of mentioning 83 and previously mentioned pipeline 85 are the parts that are generically and collectively referred to as the fuel gas feeding mechanism of " the second fuel gas feeding mechanism " in the preceding paragraph.
The tail gas stream of associating is burning by this way in WHR system 25,, makes the destruction maximization of CO that is, makes NO simultaneously xFormation minimize.
Unite with tail gas from the tail gas that WHR system 25 discharges, lead to FGD system 13 then from stove 11.In FGD system 13, remove SO 2, and discharge the exhaust to atmosphere by chimney 45.
Another burst air communication that approximately contains the tail gas of 35-45% volume ratio is crossed the fluidized-bed preheater 17 that is used to contain the 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 the fluidizing agent in the preheater 17 and the source of energy.
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, thereby keep the fluidized state in the preheater 17, and (b) will contain the temperature of iron supply material preheater to constant, in technology is when producing molten metal, and it is controlled in 600 to 700 ℃ the scope.
The tail gas that discharges from preheater 17 passes through swirler 61, and the skidding dust is isolated 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 ℃.
Washing tower 63 is identical with the basic structure of above-mentioned wet type taper washing tower 21.Particularly, this washing tower 63 makes the tail gas quenching of flowing through wherein, and gets rid of microparticle material and soluble gaseous species and metallic vapor from the tail gas that flows through wherein.And, as the situation in washing tower 21, washing tower 63 comprises the exhaust flow control valve, and this control valve has the conical component of hydraulic running, this conical component can vertical movement opening and closing described valve, thereby the mobile of tail gas by washing tower controlled.
Then, by exhaust gas cooler 65, below this exhaust gas cooler 65 further cooled exhaust gas to 50 ℃, between 30 ℃ to 45 ℃, with the moisture from tail gas removal capacity, thereby tail gas can be used as fuel gas usually from the tail gas of washing tower 63.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 tail gas stream then through the tail gas of cooling and purification, and in waste heat recovery (WHR) system 25, be used as fuel gas from water cooler 23.
This WHR system 25 comprises:
Thermal oxidizer 37, that is, and burner assembly, and relevant combustion chamber;
WHR unit 39, that is, and boiler;
Steam drum; And
Heat exchanger unit is such as overheated spiral tube and softening water water economizer.
WHR system 25 produces saturation steam.This saturation steam mixes with saturation steam from the steam drum 35 of tail gas cover 15, thereby the overheated spiral tube of WHR system 25 produces superheated vapour from this saturation steam.
The steam generation device of WHR system 25 comprises:
Be used to protect the radiation shielding of downstream spiral tube;
Overheated of two-stage (wherein, cross heat and controlled by injecting softening water as required) with desuperheater control piece superheated vapour is maintained 420 ℃ temperature;
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, and remaining steam is by producing the turbine type alternator of 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 insulating.
In use, 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, the reason of this variation has a plurality of factors, comprise: (a) in the technology operational process, produce 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.In other words, the burner assembly 37 of WHR system is supplied and controlled, make and satisfying after stove 11 and other utilize the competitive demand of unit to tail gas of tail gas the tail gas that burning is remaining.To describe in detail as following, these demands can change along with the caloric value of tail gas.
Described process quilt is designed to have multiple " state " operation down of different operation conditions during the melting operating period, these states for example comprise following state of the art:
(a) start;
(b) production of thermometal promptly, 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 promptly, is not supplied hot ore and coal, the supply hot-blast; And
(e) calm, that is, do not supply hot ore and coal, do not supply hot-blast yet, do not supply fuel gas in some cases such as Sweet natural gas.
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 the speed of coal and supply with the warm air air blast in the molten bath in container 3.These parameter influences carbon content and CO in the tail gas and the CO in the tail gas 2Content.
Exhaust gas heat value during idling conditions is relatively low.Usually, have only the warm air air blast to be supplied to container 3 (together with purging nitrogen), thereby the composition of tail gas is similar to air by 5 supplies of solid spray gun.
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 does not improve.
When technology was in idling conditions, before container 3 combust fuel gases, the operator of container can shunt slag to minimum level, or even had arranged slag.Slag shunting makes and leave a certain minimum slag in container 3, and slag arranged will be all basically the slag amount discharge container.The slag amount that reduces in the container 3 makes that metal can be directly by the burning heating.Under these situations, slag has played the effect of shackle, has reduced the heat that metal can be subjected to.
Under 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, 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 under given state of the art.For example, in thermometal production status process, operational conditions is understood some and is changed, and these variations will cause the tail gas that produces different on amount and caloric value.For example, during the thermometal production status, especially in the technology perturbation process, the caloric value of tail gas can drop to 1.8MJ/Nm 3Below (the every standard cubic meter of megajoule).
In addition, the volumetric flow rate of WHR system 25 available fuel gas changed along with the stage of stove 11.Particularly, when stove 11 moved under 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 steps 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 steps of technology, the fuel gas demand of stove 11 is different.For example, during the thermometal production status, need the amount of fuel gas will be higher than idling conditions.
In view of this, during at least some states of technology, 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, this optional fuel gas is guaranteed can the burn lower tail gas of caloric value of other unit (for example stove) of the equipment of not being supplied to of this WHR system.
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 during the given state of melting operating period from the variable flow and the caloric value of the tail gas of container 3, to satisfy the steam demand of equipment.
In addition, in view of this, under at least some states of technology, 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 the target flow and the target caloric value of the fuel gas that is used for burner assembly.For example, during the thermometal production status, the associating fuel gas stream (it is associating tail gas and optional fuel gas) that will lead to stove is controlled to be has the constant caloric value.Owing to the caloric value of tail gas along with processing condition change, also change so lead to the required flow of the tail gas of stove along with processing condition.If the caloric value of tail gas is reduced to 1.8MJ/Nm 3Below, then make all tail gas redirect to the WHR system, this is because the caloric value of tail gas is too low, to such an extent as to all can not help the heating to stove 11 under which kind of flow.The caloric value of tail gas has determined the demand of stove to tail gas at least in part just.Remaining tail gas is supplied to the WHR system, and is burnt by the WHR system.
When technology is moved, need the optional fuel gas of supply especially, such as Sweet natural gas under calm, maintenance and idling conditions.During these states, the tail gas that flows to stove 11 is completely severed, or has the reduction of certain degree at least, keeps stove 11 and moves with desired level during these state of the art thereby need another fuel gas such as Sweet natural gas.
Therefore, the process controller of equipment is by changing the burner assembly 37 that moves WHR system 25 as the flow of the Sweet natural gas of additional fuel gas, so that the flow and the caloric value of required fuel gas to be provided at any time of technology point.
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 is also by changing the burner assembly that moves stove 11 as the flow of the Sweet natural gas of additional fuel gas, so that the flow and the caloric value of required fuel gas to be provided at any time of technology point.
Therefore, the process controller of equipment also moves the burner assembly 37 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, the tail gas that leads to burner assembly 37 demand of tail gas reduced in owing to stove 11 increase before, the process controller of equipment begins to improve the air flow quantity of the burner assembly 37 that leads to WHR system 25 in being generally 30 seconds predetermined amount of time.
Similarly, before the tail gas that leads to burner assembly 37 reduces the increase in demand of tail gas in owing to stove 11, the air flow quantity of the burner assembly 37 that the process controller of equipment begins to reduce to lead to WHR system 25 in being generally 30 seconds predetermined amount of time.
In a specific embodiment of aforesaid device operation, this process controller is controlled following aspect:
(a) volumetric flow rate of Sweet natural gas of the burner unit of stove 11 is led in control, so that during the heating phase of stove, the combined stream measurer of tail gas and Sweet natural gas has the caloric value of constant; And
(b) control the volumetric flow rate of the Sweet natural gas that leads to WHR system 25 in response to the variation of the volumetric flow rate of the tail gas that leads to the WHR system, to realize the burning of the intrasystem tail gas of WHR.
Under the situation of described specific example, about above-mentioned project (b), WHR system 25 needs a certain amount of fuel gas, and this a certain amount of fuel gas can be by tail gas and/or natural gas supply, so that minimum at least critical heat value to be provided.
For the flow of the required Sweet natural gas of the burner assembly of the burner assembly 37 of determining time WHR system 25 at any time and stove 11, the caloric value of the tail gas at equipment different positions place is an important parameters.
Equipment comprises mass spectrograph CV1, CV2 and the CV3 that is positioned at place, equipment selected location, 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 a part of determining the processing of required tail gas and gas discharge.
Selected position for tail gas cover 15 in (CV1), in exhaust gas cooler 23 downstreams with lead to stove 11 and upstream (CV2) that the tail gas of WHR system 25 is shunted, and in the downstream of preheater 61 (CV3).
The above-mentioned technology of operation also has influence to the pressure-controlling in the container 3 in the different states process under the scope of different states.
In addition, preheater 17 has and maintains a certain minimum gas stream requirement under the fluidized state with containing the iron supply material.Air-flow by preheater 17 is controlled by the control valve of the wet type taper washing tower 63 that is positioned at preheater 17 downstreams.
Foregoing description shows, when producing molten pig, when promptly moving under the thermometal production status, the control of container pressure is that the control valve 77 by wet type taper washing tower 21 carries out in described technology.
More specifically, equipment comprises the pressure transmitter P1 that is positioned at tail gas cover 15, and this pressure transmitter is monitored the pressure that flows through the tail gas of tail gas cover with the successive form.When technology was moved with the thermometal production status, the process controller of equipment was in response to the pressure of being monitored, and the control valve 77 of operation wet type taper washing tower 21, thereby regulates pressure as required, preferably keeps the constant container pressure.The time constant of the pilot circuit of control valve 77 is significantly faster than the time constant of the pilot circuit of the control valve in the washing tower 63 in preheater 17 downstreams.Therefore, pressure in control container 3 and control mainly are the control to container pressure in the Metal Production process with regard to the control between the gas flow of preheater 17.
During other states of this technology, especially during maintenance and idling conditions, still be necessary to keep 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 moving this technology under these states, the control valve 77 of wet type taper washing tower 21 is closed at least substantially, 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, the control valve in the wet type taper washing tower 63 becomes main pressure controller under maintenance and idling conditions.This has also guaranteed the gas stream by preheater, so that metal-containing material is maintained under the fluidized state.
In addition, when technology became maintenance and idling conditions, described process controller moved will be fed to the flow set point reduction of 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 crust from gauge pressure 0.8 crust.
Keep and idling conditions during, that part by preheater 17 in the tail gas is recycled, and with tail gas associating from container 3, thereby help to keep the interior fluidization conditions of preheater 17.
Under windless condition, not to the air blast of container supply warm air.The washing tower 63 in preheater 17 downstreams is closed, and all tail gas in the preheater 17 is 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 in the thermometal production process, compare, reduce total energy to stove 11 supplied fuel gases to the total energy of stove supplied fuel gas.Like this, under 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 (35)

1.一种直接熔炼设备，用于以直接熔炼工艺从含金属供给材料生产熔融金属，包括：1. A direct smelting plant for producing molten metal from metal-containing feed material in a direct smelting process, comprising: (a)直接熔炼容器，用于通过在所述容器中直接熔炼含金属供给材料的工艺而产生熔融金属、熔渣和尾气；(a) a direct smelting vessel for producing molten metal, slag and off-gas by a process of direct smelting metal-containing feed material in said vessel; (b)第一燃料气体供应装置，用于供应来自所述直接熔炼容器的尾气以用作所述设备的和/或所述设备外部的两个或更多个运行单元的燃烧器单元内的燃料气体；(b) a first fuel gas supply means for supplying off-gas from said direct smelting vessel for use as in the burner unit of said plant and/or of two or more operating units external to said plant fuel gas; (d)第二燃料气体供应装置，用于从另一源向所述运行单元中的至少一个的所述燃烧器单元供应另一燃料气体，例如天然气，以及(d) a second fuel gas supply means for supplying another fuel gas, such as natural gas, from another source to said burner unit of at least one of said operating units, and (e)工艺控制器，用于调节向所述运行单元中的至少一个的燃烧器单元供应的燃料气体的体积流量，以至少满足所述设备为了运行所述直接熔炼工艺的所选要求。(e) a process controller for adjusting the volume flow of fuel gas supplied to the burner unit of at least one of said operating units to at least meet the selected requirements of said plant for operating said direct smelting process. 2.根据权利要求1所述的设备，其中，所述运行单元包括(i)废热回收单元和/或(ii)多个炉子，该废热回收单元用于产生蒸汽以在所述设备中使用和/或用于发电以在所述设备中使用或在所述设备外使用，所述多个炉子用于产生热空气鼓风或热富氧空气鼓风，以在所述直接熔炼工艺中使用。2. The plant according to claim 1, wherein said operating unit comprises (i) a waste heat recovery unit and/or (ii) a plurality of furnaces for generating steam for use in said plant and/or (ii) a plurality of furnaces and/or for generating electricity for use in or outside the plant, the plurality of furnaces for generating hot air blasts or hot oxygen-enriched air blasts for use in the direct smelting process. 3.根据权利要求2所述的设备，其中，所述第二燃料气体供应装置适于向所述废热回收单元和/或所述炉子供应诸如天然气的燃料气体。3. The apparatus according to claim 2, wherein the second fuel gas supply means is adapted to supply fuel gas, such as natural gas, to the waste heat recovery unit and/or the furnace. 4.根据权利要求2或3所述的设备，其中，所述工艺控制器适于对供应至所述废热回收单元的所述燃烧器单元的燃料气体的体积流量进行调节。4. Apparatus according to claim 2 or 3, wherein the process controller is adapted to regulate the volume flow of fuel gas supplied to the burner unit of the waste heat recovery unit. 5.根据权利要求4所述的设备，其中，所述工艺控制器适于对经由所述第二燃料气体供应装置供应至所述废热回收单元的所述燃烧器单元的诸如天然气的燃料气体的体积流量进行调节。5. The apparatus according to claim 4, wherein the process controller is adapted to control the fuel gas such as natural gas supplied to the burner unit of the waste heat recovery unit via the second fuel gas supply means Volume flow is regulated. 6.根据权利要求2至5中的任一项所述的设备，其中，所述工艺控制器适于对供应至所述炉子的所述燃烧器单元的燃料气体的体积流量进行调节。6. Apparatus according to any one of claims 2 to 5, wherein the process controller is adapted to regulate the volumetric flow of fuel gas supplied to the burner units of the furnace. 7.根据权利要求6所述的设备，其中，所述工艺控制器适于对经由所述第二燃料气体供应装置供应至所述炉子的所述燃烧器单元的诸如天然气的燃料气体的体积流量进行调节。7. Apparatus according to claim 6, wherein the process controller is adapted to control the volumetric flow rate of fuel gas, such as natural gas, supplied to the burner unit of the furnace via the second fuel gas supply. Make adjustments. 8.根据权利要求2至7中任一项所述的设备，其中，所述工艺控制器响应于尾气的流量和/或热量值并响应于所述设备的蒸汽要求和/或响应于所述工艺的热空气或富氧空气要求，从而考虑到在任一时间点上尾气的流量和/或热量值以及所述设备和/或所述工艺的要求，来确定所述炉子和/或所述废热回收单元的所述燃烧器单元所需的经由所述第二燃料气体供应装置的诸如天然气的燃料气体的体积流量。8. The plant according to any one of claims 2 to 7, wherein the process controller is responsive to the flow and/or calorific value of the tail gas and to the steam requirement of the plant and/or to the The hot or oxygen-enriched air requirements of the process, whereby the furnace and/or the waste heat are determined taking into account the flow and/or calorific value of the tail gas at any point in time and the requirements of the plant and/or the process The volume flow of fuel gas, such as natural gas, required by the burner unit of the recovery unit via the second fuel gas supply. 9.根据权利要求8所述的设备，其中，所述工艺控制器响应于所述废热回收单元的所述燃烧器单元的火焰温度。9. The apparatus of claim 8, wherein the process controller is responsive to the flame temperature of the burner unit of the waste heat recovery unit. 10.根据权利要求9所述的设备，其中，所述工艺控制器响应于所述废热回收单元的所述燃烧器单元的火焰温度，以将所述火焰温度维持成高于最低温度。10. The apparatus of claim 9, wherein the process controller is responsive to a flame temperature of the burner unit of the waste heat recovery unit to maintain the flame temperature above a minimum temperature. 11.根据权利要求8至10中任一项所述的设备，其中，如这里所定义的，所述工艺控制器通过参考在所述工艺的不同运行状态期间的蒸汽流量或蒸汽压力的所需值而响应于所述设备的蒸汽需求。11. Apparatus according to any one of claims 8 to 10, wherein, as defined herein, the process controller is controlled by reference to the required steam flow or steam pressure during different operating states of the process value in response to the steam demand of the device. 12.根据权利要求8至11中任一项所述的设备，其中，所述工艺控制器适于对通过所述第二燃料气体供应装置供应到所述炉子的所述燃烧器单元的燃料气体的体积流量进行调节，以使供应到所述炉子的燃烧器单元的联合燃料气体具有预定的流量和/或热量值。12. Apparatus according to any one of claims 8 to 11, wherein the process controller is adapted to control the fuel gas supplied to the burner unit of the furnace by the second fuel gas supply means The volumetric flow rate is adjusted so that the combined fuel gas supplied to the burner units of the furnace has a predetermined flow rate and/or calorific value. 13.根据权利要求8至12中任一项所述的设备，其中，所述工艺控制器适于对通过所述第二燃料气体供应装置供应到所述炉子的所述燃烧器单元的燃料气体的流量进行调节，以使所述炉子的燃烧器单元至少在所述炉子的加热阶段开始时以恒定的热量值运行。13. Apparatus according to any one of claims 8 to 12, wherein the process controller is adapted to control the fuel gas supplied to the burner unit of the furnace by the second fuel gas supply means The flow rate of the furnace is adjusted so that the burner units of the furnace operate at a constant calorific value at least at the beginning of the heating phase of the furnace. 14.根据权利要求8至13中任一项所述的设备，包括用于对所述设备的不同位置处的尾气的热量值进行监控的装置。14. Apparatus according to any one of claims 8 to 13, comprising means for monitoring the calorific value of the off-gas at different locations of the apparatus. 15.根据权利要求14所述的设备，其中，所述尾气热量值监控装置为质谱仪。15. The device according to claim 14, wherein the exhaust gas calorific value monitoring device is a mass spectrometer. 16.根据权利要求14或15所述的设备，其中，所述工艺控制器响应于对热量值的监控值。16. Apparatus according to claim 14 or 15, wherein the process controller is responsive to the monitored value of the heating value. 17.根据前述权利要求中任一项所述的设备，包括呈预处理单元形式的运行单元，该预处理单元用于对含金属供给材料进行预处理。17. Apparatus according to any one of the preceding claims, comprising an operating unit in the form of a pretreatment unit for pretreatment of metal-containing feed material. 18.根据权利要求17所述的设备，包括用于从所述直接熔炼容器供应尾气的装置，该尾气用作所述预处理单元内的流化气体。18. Apparatus according to claim 17, comprising means for supplying off-gas from the direct smelting vessel for use as fluidizing gas in the pre-treatment unit. 19.根据权利要求18所述的设备，包括一装置，该装置用于将从所述直接熔炼容器排出的尾气分为(i)用于所述炉子和所述废热回收单元的第一股流以及(ii)用于所述预处理单元的第二股流。19. Apparatus according to claim 18 including means for dividing off-gas exiting said direct smelting vessel into (i) a first stream for said furnace and said waste heat recovery unit and (ii) a second stream for said pretreatment unit. 20.根据权利要求19所述的设备，包括一装置，该装置用于将来自(i)所述第一股流中的尾气和(ii)所述第二股流中的被从所述预处理单元排出的尾气形成联合尾气流。20. Apparatus according to claim 19, comprising means for converting tail gas from (i) said first stream and (ii) exhaust gas from said pre-stream into said second stream. The tail gas discharged from the treatment unit forms a combined tail gas stream. 21.根据权利要求20所述的设备，其中，所述尾气热量值监控装置适于对所述联合尾气流中的尾气的热量值进行监控。21. The apparatus according to claim 20, wherein the off-gas calorific value monitoring means is adapted to monitor the calorific value of the off-gas in the combined off-gas flow. 22.根据权利要求21所述的设备，其中，所述工艺控制器响应于对所述联合尾气流中的尾气进行监控所得的热量值。22. The apparatus of claim 21, wherein the process controller is responsive to a calorific value obtained by monitoring off-gas in the combined off-gas stream. 23.根据权利要求22所述的设备，其中，所述工艺控制器适于响应于对所述联合尾气流的热量值进行监控所得的值，而对经由所述第二燃料气体供应装置向所述废热回收单元供应的燃料气体的体积流量进行调节。23. The apparatus of claim 22, wherein the process controller is adapted to respond to a value obtained by monitoring the calorific value of the combined off-gas flow to the The volume flow rate of the fuel gas supplied by the waste heat recovery unit is adjusted. 24.根据权利要求21所述的设备，其中，所述尾气热量值监控装置适于对所述第一股流和所述第二股流中的尾气的热量值进行监控。24. Apparatus according to claim 21, wherein said off-gas calorific value monitoring means is adapted to monitor the calorific value of off-gas in said first stream and said second stream. 25.一种基于熔融熔池的直接熔炼工艺，用于在直接熔炼设备中从含金属供给材料生产熔融金属，包括：25. A molten bath based direct smelting process for producing molten metal from metal-containing feed material in a direct smelting plant, comprising: (a)在包含金属和炉渣的熔融熔池的直接熔炼容器中对含金属供给材料进行直接熔炼，并产生熔融金属、熔渣和尾气，该工艺具有不同的工艺状态；(a) direct smelting of metal-containing feed material in a direct smelting vessel containing a molten bath of metal and slag and producing molten metal, slag and off-gas, the process having various process states; (b)将在熔炼运行期期间所述容器内产生的尾气作为燃料气体供应至所述设备的和/或所述设备外部的两个或更多个运行单元的燃烧器单元，以及(b) a burner unit for supplying tail gas generated in said vessel during a smelting operation period as fuel gas to two or more operating units of said plant and/or external to said plant, and (c)从另一源向所述运行单元的至少一个的所述燃烧器单元供应诸如天然气的另一燃料气体，(c) supplying another fuel gas, such as natural gas, to said burner unit of at least one of said operating units from another source, (d)在所述工艺的过程中，对供应到所述运行单元的所述燃烧器单元的燃料气体的体积流量进行调节，从而至少满足所述设备的需求。(d) During said process, the volumetric flow of fuel gas supplied to said burner units of said operating units is adjusted so as to at least meet the needs of said plant. 26.根据权利要求25所述的工艺，其中，所述运行单元包括(i)废热回收单元的热回收炉和/或(ii)多个炉子，所述废热回收单元用于产生供在所述设备内使用的蒸汽和/或产生供在所述设备内使用或在所述设备外使用的电力，所述多个炉子用于产生在所述容器内对含金属供给材料进行直接熔炼所用的热空气鼓风或热富氧空气鼓风。26. A process according to claim 25, wherein said operating unit comprises (i) a heat recovery furnace of a waste heat recovery unit and/or (ii) a plurality of furnaces for generating Steam for use within and/or generation of electricity for use within or outside of said facility, said plurality of furnaces for generating heat for direct smelting of metal-containing feed material within said vessel Air blast or hot oxygen-enriched air blast. 27.根据权利要求26所述的工艺，包括对供应到所述废热回收单元和/或所述炉子的所述燃烧器单元的所述另一燃料气体的体积流量进行调节，从而维持通向所述燃烧器单元的预定流量和/或热量值。27. A process according to claim 26, comprising adjusting the volume flow of said further fuel gas supplied to said waste heat recovery unit and/or said burner unit of said furnace so as to maintain a flow to said The predetermined flow rate and/or calorific value of the burner unit mentioned above. 28.根据权利要求27所述的工艺，包括对所述设备不同位置处的尾气热量值进行监控。28. A process according to claim 27 including monitoring the calorific value of the off-gas at various locations in the plant. 29.一种直接熔炼设备，用于以直接熔炼工艺从含金属供给材料生产熔融金属，包括：29. A direct smelting plant for producing molten metal from metal-containing feed material in a direct smelting process, comprising: (a)直接熔炼容器，用于以在所述容器中直接熔炼含金属供给材料的工艺而产生熔融金属、熔渣和尾气；(a) a direct smelting vessel for producing molten metal, slag and off-gas in a process for directly smelting metal-containing feed material in said vessel; (b)至少两个用于接收和燃烧尾气的尾气处理单元；(b) At least two exhaust treatment units for receiving and combusting exhaust; (c)第一燃料气体供应装置，用于从所述直接熔炼容器供应尾气，以在所述尾气处理单元的燃烧器单元内使用；(c) a first fuel gas supply means for supplying off-gas from said direct smelting vessel for use in a burner unit of said off-gas treatment unit; (d)第二燃料气体供应装置，用于从另一源向所述至少两个尾气处理单元的燃烧器单元供应诸如天然气的另一燃料气体；(d) a second fuel gas supply means for supplying another fuel gas, such as natural gas, from another source to the burner units of said at least two tail gas treatment units; (e)工艺控制器，用于：(e) Process controllers for: i)控制通向所述尾气处理单元中的一个的尾气的体积流量，以满足该单元的需求，而将剩下的尾气供应到剩余的一个或多个尾气处理单元；i) controlling the volumetric flow of off-gas to one of said off-gas treatment units to meet the needs of that unit, while supplying the remaining off-gas to the remaining one or more off-gas treatment units; ii)控制通向所述尾气处理单元的所述另一燃料气体的体积流量。ii) controlling the volumetric flow of said further fuel gas to said tail gas treatment unit. 30.根据权利要求29所述的设备，其中，所述尾气处理单元包括用于向所述直接熔炼容器供应热鼓风的炉子和用于产生蒸汽的废热回收单元。30. The apparatus of claim 29, wherein the tail gas treatment unit comprises a furnace for supplying hot blast to the direct smelting vessel and a waste heat recovery unit for generating steam. 31.根据权利要求30所述的设备，其中，所述工艺控制器适于对通向所述炉子的尾气和所述另一燃料气体的供应进行控制，使得通向所述炉子的尾气和所述另一燃料气体的联合供应具有大致恒定的热量值。31. The apparatus of claim 30, wherein the process controller is adapted to control the supply of the off-gas to the furnace and the further fuel gas such that the off-gas to the furnace and the The combined supply of the further fuel gas has a substantially constant calorific value. 32.根据权利要求30或31所述的设备，其中，所述工艺控制器适于响应于尾气体积流量的变化而对向所述废热回收单元的所述另一燃料气体的供应进行控制，从而在所述废热回收单元内实现尾气的燃烧。32. Apparatus according to claim 30 or 31 , wherein the process controller is adapted to control the supply of the further fuel gas to the waste heat recovery unit in response to a change in tail gas volume flow, whereby Combustion of exhaust gas is realized in the waste heat recovery unit. 33.根据权利要求30至32中任一项所述的设备，包括：一个或多个尾气供应阀，所述尾气供应阀用于控制通向所述炉子的尾气的体积流量并用于转向为向所述废热回收单元供应尾气；以及尾气热量值感测装置，该尾气热量值感测装置用于感测尾气的热量值，而且其中，所述工艺控制器适于监控尾气热量值，并响应于所述尾气的热量值降低到预定阈值之下，而运行所述一个或多个尾气供应阀以使尾气转向至所述废热回收单元。33. Apparatus according to any one of claims 30 to 32, comprising one or more off-gas supply valves for controlling the volumetric flow of off-gas to the furnace and for diverting to The exhaust heat recovery unit supplies exhaust gas; and an exhaust gas calorific value sensing device for sensing the exhaust gas calorific value, and wherein the process controller is adapted to monitor the exhaust gas calorific value and respond to The calorific value of the exhaust gas falls below a predetermined threshold and the one or more exhaust gas supply valves are operated to divert the exhaust gas to the waste heat recovery unit. 34.根据权利要求33所述的设备，其中，所述预定阈值为这样的值，即，在该值时尾气不再对尾气和所述另一燃料气体的联合燃料气体流的热量值有积极的贡献。34. The apparatus of claim 33, wherein the predetermined threshold is a value at which the exhaust gas no longer contributes positively to the calorific value of the combined fuel gas flow of the exhaust gas and the further fuel gas. contribution. 35.根据权利要求33所述的设备，其中，所述预定阈值为1.8MJ/Nm3(兆焦耳每标准立方米)。35. The apparatus of claim 33, wherein the predetermined threshold is 1.8 MJ/ Nm3 (megajoules per standard cubic meter).
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