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WO2024111758A1 - Four de réduction et procédé de production de fer réduit - Google Patents

Four de réduction et procédé de production de fer réduit Download PDF

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Publication number
WO2024111758A1
WO2024111758A1 PCT/KR2023/003103 KR2023003103W WO2024111758A1 WO 2024111758 A1 WO2024111758 A1 WO 2024111758A1 KR 2023003103 W KR2023003103 W KR 2023003103W WO 2024111758 A1 WO2024111758 A1 WO 2024111758A1
Authority
WO
WIPO (PCT)
Prior art keywords
burner
reducing gas
raw material
dispersion member
height
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/KR2023/003103
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English (en)
Korean (ko)
Inventor
윤시경
장권우
김용인
신명균
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Posco Holdings Inc
Original Assignee
Posco Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Posco Co Ltd filed Critical Posco Co Ltd
Priority to CN202380023996.5A priority Critical patent/CN118871597A/zh
Priority to EP23894694.1A priority patent/EP4624595A1/fr
Priority to JP2024551579A priority patent/JP2025506896A/ja
Publication of WO2024111758A1 publication Critical patent/WO2024111758A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • 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

Definitions

  • the present invention relates to a reduction furnace and a method for producing reduced iron, and more specifically, to a reduction furnace and a method for producing reduced iron that can facilitate the flow of raw materials.
  • the blast furnace process requires several auxiliary facilities such as coke manufacturing equipment and sinter ore manufacturing equipment.
  • auxiliary facilities such as coke manufacturing equipment and sinter ore manufacturing equipment.
  • environmental pollution occurs due to substances discharged from auxiliary equipment and the cost of environmental pollution prevention equipment increases.
  • This molten iron manufacturing facility includes a fluidized reduction furnace for producing reduced iron by reducing powdered iron ore, and a melting device for producing molten iron by melting the reduced iron provided from the fluidizing reduction furnace.
  • the fluidized reduction furnace includes a container and a dispersing member having a plurality of holes through which gas can pass.
  • the dispersing member is installed inside the container, reducing gas is supplied to the lower side of the dispersing member, and powdered iron ore is charged to the upper side of the dispersing member.
  • the reducing gas When reducing gas is supplied to the lower side of the dispersing member, the reducing gas passes through a plurality of holes provided in the dispersing member and is injected upward.
  • the powdered iron ore on the upper side of the dispersing member flows due to the reducing gas injected upward in this way. And while the powdered iron ore flows, it reacts with the reducing gas, and the powdered iron ore is reduced and produced into reduced iron.
  • the interior of the fluidized reduction furnace must be maintained above a predetermined temperature.
  • the reaction between powdered iron ore and reducing gas is a predominantly endothermic reaction, the temperature inside the fluidized reduction furnace may decrease during the reduction reaction.
  • a burner is installed in the fluidized reduction furnace to generate a flame, thereby heating the fluidized reduction furnace. At this time, the burner is installed to be located above the dispersion member.
  • the powdered iron ore particles may melt and stick together. And when the powdered iron ore particles clump together and form a lump, the powdered iron ore does not flow smoothly. As a result, a stagnation phenomenon occurs in which powdered iron ore does not flow or only small flows occur.
  • the temperature of the dispersion member becomes high.
  • the powdered iron ore particles are melted by the heat of the dispersing member and become entangled together, which causes the holes of the dispersing member to become clogged. If the hole of the dispersion member is blocked, the reducing gas cannot pass through, so there is a problem in that the flow of powdered iron ore on the upper side of the dispersion member is not smooth.
  • Patent Document 1 Korean Patent Publication 10-2007-0068210
  • the present invention provides a reduction furnace and a method for producing reduced iron that can suppress or prevent stagnation of the flow of raw materials.
  • the present invention provides a reduction furnace and a method for producing reduced iron that can suppress or prevent the holes of the dispersion member from being closed.
  • the present invention provides a reduction furnace capable of lowering the temperature of the flame and a method for producing reduced iron.
  • a reduction reactor includes a container having an internal space capable of accommodating a raw material including iron ore and a reducing gas; a dispersing member installed inside the container and having a plurality of holes through which the reducing gas can pass; and a burner installed on an upper side of the dispersion member at a height spaced apart from the dispersion member determined using the target flow rate of the reducing gas to be supplied into the container and capable of generating a flame inside the container.
  • the installation height of the burner is a height determined using at least one of the diameter of the hole provided in the dispersion member (d or ) and the flow rate (u or ) of the reducing gas, which are adjusted according to the target flow rate of the reducing gas.
  • the height at which the burner is installed may be greater than or equal to the depth (l j ) at which the reducing gas penetrates into the raw material layer made of raw materials supplied to the upper side of the dispersing member, and may be less than or equal to the upper height of the raw material layer.
  • the burner includes a body extending in one direction; and a plurality of nozzles installed inside the main body, which extend in the direction in which the main body extends and whose distance between them becomes closer as they get closer to one end of the main body.
  • the tilt angle of each of the plurality of nozzles may be 20° to 45°.
  • the plurality of nozzles may be provided symmetrically with respect to the radial center of the main body.
  • the method for producing reduced iron is to determine the installation height (H b ) of the burner based on the dispersion member installed inside the container using the target flow rate of the reducing gas to be supplied to the container of the reduction furnace. procedure; A process of installing a burner in the container such that the distance from the dispersion member to the upper side is the determined installation height (H b ); A process of supplying raw materials including iron ore to the upper side of the dispersing member; A process of passing a reducing gas through a hole of the dispersion member to flow the raw material on the upper side of the dispersion member; A process of generating a flame inside the container using the burner; and a process of reducing the raw material by reacting the raw material with a reducing gas.
  • determining a target flow rate of the reducing gas Before determining a height (H b ) to install the burner, determining a target flow rate of the reducing gas; and determining the flow rate (u or ) of the reducing gas to be supplied to the container using the determined target flow rate of the reducing gas and the diameter (d or ) of the hole provided in the dispersion member.
  • the process of determining the installation height (H b ) of the burner is the depth ( The process of predicting l j ); And it may include a process of determining the height (H b ) at which the burner will be installed at a height higher than the predicted penetration depth (l j ).
  • the process of predicting the depth (l j ) at which the reducing gas penetrates into the raw material layer includes the diameter of the hole (d or ), the flow rate of the reducing gas (u or ), the density of the reducing gas ( ⁇ g ), and the raw material particles. It may include a process of calculating the penetration depth (l j ) of the reducing gas using the density ( ⁇ s ), the particle size of the raw material particles (d p ), and the dynamic viscosity ( ⁇ ) of the reducing gas.
  • the height (H b ) at which the burner is to be installed may be determined in a range that is greater than or equal to the predicted penetration depth (l j ) and less than or equal to the upper height of the raw material layer.
  • the process of generating a flame inside the container using the burner includes supplying an oxidizing agent to each of a plurality of nozzles provided in the burner; forming an oxidizing agent stream by spraying an oxidizing agent from each of the plurality of nozzles; A process of colliding a plurality of the oxidant streams to spread the oxidant streams; and a process of generating a flame by reacting the oxidizing agent stream with the reducing gas.
  • the process of spraying the oxidizing agent from each of the plurality of nozzles may include spraying the oxidizing agent from each of the plurality of nozzles so that the oxidizing agent injected from each of the plurality of nozzles has an inclined flow that becomes closer to the radial center of the burner as the distance from the burner increases. You can.
  • the oxidizing agent may include oxygen (O) and nitrogen (N 2 ).
  • It may include a process of adjusting the flow rate of the oxidant sprayed from each of the plurality of nozzles to 80 m/sec to 100 m/sec.
  • the reducing gas may include hydrogen (H 2 ) gas.
  • the dispersion member it is possible to suppress or prevent the dispersion member from being heated to a high temperature by the heat of the flame generated from the burner. Additionally, it is possible to generate a flame at a lower temperature than before. Accordingly, agglomeration due to melting of raw material particles can be suppressed or prevented, and thus the formation of a stagnation layer can be suppressed or prevented. Therefore, raw materials can flow smoothly inside the reduction furnace.
  • FIG. 1 is a diagram schematically showing a molten iron manufacturing facility of the present invention.
  • Figure 2 is a diagram showing a reduction furnace according to an embodiment of the present invention.
  • Figure 3 is an enlarged cross-sectional view of a portion of the reduction furnace.
  • Figure 4 is a front cross-sectional view of a burner according to an embodiment of the present invention.
  • Figure 5 is a plan view of a burner according to an embodiment of the present invention.
  • Figure 6 is a diagram explaining the flow of oxidant sprayed from a burner according to an embodiment of the present invention.
  • Figure 7 is a diagram schematically showing an experimental reduction reactor.
  • Figure 8 shows the results of measuring the temperature in the horizontal direction at a predetermined height of the experimental reduction furnace.
  • Figure 9 shows the results of measuring the temperature of the area from the dispersion member to a predetermined height upward in the experimental reduction furnace.
  • Figure 10 is a result showing the temperature distribution by height inside the container when a first type burner with one nozzle is installed in the container of an experimental reduction furnace to generate a flame.
  • Figure 11 is a result showing the temperature distribution by height inside the vessel when a second type of burner having first and second nozzles is installed in the vessel of an experimental reduction furnace to generate a flame.
  • FIG. 1 is a diagram schematically showing a molten iron manufacturing facility of the present invention.
  • the molten iron production facility includes a reduced iron production device 2000 having a reduction unit 2100 capable of producing reduced iron and a dissolution device 3000 capable of dissolving reduced iron. Includes.
  • the molten iron manufacturing facility includes a raw material supply device 1000 installed to supply raw materials to the reduction unit 2100 and a melting device 3000 to supply exhaust gas discharged from the melting device 3000 to the reduction section 2100. It may include an exhaust gas supply line 4000 installed to connect the reduction unit 2100.
  • the molten iron manufacturing facility may further include a molding device (not shown) that molds the powdered reduced iron produced in the reduced iron manufacturing device 2000.
  • the raw material supply device 1000 is installed to supply raw materials to the reduction unit 2100.
  • the raw material may include iron ore, and the iron ore may include finely divided iron ore whose particle size is greater than 0 mm and less than or equal to 0 mm.
  • the raw material supply device 1000 may include, for example, a storage device capable of storing raw materials. Raw materials may be stored in the internal space of the storage unit for a long time, or may be temporarily stored before supplying the raw materials to the reduced iron manufacturing apparatus 2000.
  • a reservoir may include, for example, a hopper.
  • the dissolution device 3000 receives reduced iron from the reduced iron production device 2000 and dissolves the supplied reduced iron. At this time, the dissolving device 3000 may be fine reduced iron or reduced iron prepared by agglomerating fine reduced iron in a molding device.
  • the dissolution device 3000 may be a device that dissolves reduced iron using, for example, electric heat. That is, the dissolving device 3000 may be a device that dissolves reduced iron using electrical energy.
  • the melting device 3000 may receive additional iron scrap in addition to reduced iron and melt the reduced iron and iron scrap together.
  • This dissolution device 3000 may include an electric furnace having a dissolution space capable of dissolving reduced iron using electric heat.
  • Such an electric furnace may include an electric furnace main body 3100 having a dissolution space and an electrode 3200 at least partially disposed in the dissolution space to generate electric heat. In an electric furnace, when reduced iron is charged into the dissolution space, power is applied to the electrode 3200 to melt the reduced iron, thereby producing molten iron. Additionally, the exhaust gas generated during the manufacture of molten iron in an electric furnace may be supplied to the reduction unit 2100 through the exhaust gas supply line 4000.
  • the gas generated and discharged from the dissolution device 3000 (hereinafter referred to as exhaust gas) is recovered and supplied to the reduction section of the reduced iron production device. And in the reduced iron production device, iron ore is reduced using exhaust gas supplied from the dissolution device 3000. At this time, the exhaust gas discharged from the dissolving device 3000 may be supplied to the reduction unit 2100 through the exhaust gas supply line 4000.
  • the dissolution device 3000 includes an electric furnace.
  • the melting device 3000 is not limited to this and may include a melting gasification furnace. Inside the melt gasifier, a coal-filled bed made of coal is formed. Reduced iron and auxiliary raw materials are then introduced into the melting gasifier, and oxygen is blown in through a number of tuyeres installed on the outer wall. Accordingly, the coal-filled bed is burned by blown oxygen, which melts the reduced iron and produces molten iron. Additionally, the exhaust gas generated during the production of molten iron in the melting gasifier may be supplied to the reduction unit 2100 through the exhaust gas supply line 4000.
  • the reduced iron production apparatus 2000 includes a reduction unit 2100 that reduces iron ore to produce reduced iron. Additionally, the reduced iron manufacturing apparatus 2000 may include a hydrogen gas supply unit 2200 that supplies a reducing gas containing hydrogen to the reduction unit 2100.
  • the hydrogen gas supply unit 2200 supplies hydrogen gas, which is a reducing gas for reducing the raw material, that is, iron ore, to the reduction unit 2100.
  • hydrogen gas which is a reducing gas for reducing the raw material, that is, iron ore
  • by-products generated when reducing raw materials in the reduction unit 2100 include water vapor, hydrogen gas, nitrogen gas, and carbon dioxide gas.
  • the hydrogen gas supply unit 2200 may be a means provided to process by-products generated and discharged from the reduction unit 2100 to produce hydrogen gas, and to supply this hydrogen gas to the reduction unit 2100.
  • This hydrogen gas supply unit 2200 includes an exhaust pipe 2210 connected to the reduction unit 2100 to discharge by-products generated in the reduction unit 2100, and an exhaust pipe 2210 to receive the by-products and extract hydrogen gas. ), an extractor 2220 connected to the extractor 2220, a supply pipe 2230 installed to connect the extractor 2220 and the reduction unit 2100 so that hydrogen gas extracted or generated in the extractor 2220 can be supplied to the reduction unit 2100, and It may include a heater 2240 installed on the extension path of the supply pipe 2230 to heat the hydrogen gas generated in the extractor 2220.
  • the hydrogen gas supply unit 2200 may further include a dust collector 2250 installed in the exhaust pipe 2210 to collect dust such as fine particles from by-products.
  • Carbon molecular sieve can be used as an adsorbent.
  • the hydrogen component adsorbed on the adsorbent can be desorbed and extracted as hydrogen gas, and the extractor 2220 can extract hydrogen gas from the by-product by repeatedly performing adsorption and desorption of the hydrogen component.
  • Hydrogen gas extracted from the extractor 2220 is supplied to the reduction unit 2100 through the supply pipe 2230.
  • the hydrogen gas supplied to the reduction unit 2100 can be used to reduce iron ore in the reduction unit 2100. That is, the hydrogen gas supplied to the reduction unit 2100 reduces iron ore. Accordingly, the hydrogen gas supplied to the reduction unit 2100 may be called 'reduction gas' that reduces iron ore.
  • the process of producing reduced iron by reducing iron ore using hydrogen gas, and producing molten iron by melting the reduced iron may be a process called 'hydrogen reduction iron making process'.
  • hydrogen gas is supplied to the reduction unit 2100 to reduce raw materials, and the hydrogen gas reacts with iron ore to generate water or steam and does not generate carbon dioxide. Therefore, when hydrogen gas is supplied to the reduction unit 2100 to reduce raw materials, there is an effect of reducing carbon emissions. That is, hydrogen reduction in which the raw material is reduced by supplying only hydrogen gas to the reduction unit 2100, or a gas mixed with the exhaust gas discharged from the dissolving device 3000 and hydrogen gas is supplied to the reduction unit 2100 to reduce the raw material.
  • the steelmaking process has the effect of reducing carbon emissions compared to the process of reducing raw materials using only exhaust gas.
  • the embodiment is not only a hydrogen reduction steelmaking process in which only hydrogen gas is supplied to the reduction unit 2100, or a mixture of exhaust gas discharged from the dissolution device 3000 and hydrogen gas is supplied to the reduction unit 2100, but also a dissolution device ( It can also be applied to a general steelmaking process in which only the exhaust gas discharged from 3000) is supplied to the reduction unit 2100.
  • the reduction unit 2100 reduces raw materials to produce reduced iron. That is, the reduction unit 2100 receives raw materials including iron ore from the raw material supply device 1000 and reacts the iron ore with the reducing gas to produce reduced iron.
  • the reducing gas supplied to the reduction unit 2100 may include at least one of hydrogen gas supplied from the hydrogen gas supply unit 2200 and exhaust gas discharged from the dissolving device 3000.
  • the reduction unit 2100 may include a reduction furnace that produces reduced iron while flowing raw materials. Additionally, a single reduction reactor may be provided, but a plurality of reduction reactors may be provided to effectively reduce low-grade iron ore or powdered iron ore with low iron content. When a plurality of reduction furnaces are provided in this way, the reduction unit 2100 includes a plurality of raw material transfer pipes (2111a to 2111c) and a plurality of gas transfer pipes (2112a to 2112c) installed to connect between the plurality of reduction furnaces (2100a to 2100d). ) may include.
  • a plurality of reduction furnaces 2100a to 2100d may be provided. And the plurality of reduction furnaces 2100a to 2100d may be connected to each other to sequentially move raw materials as shown in FIG. 1.
  • the number of reduction furnaces 2100a to 2100d is not particularly limited, but in order to sufficiently reduce the raw materials, the reduction unit 2100 includes four reduction furnaces (first to fourth reduction furnaces 2100a to 2100d). It can be provided. And when the reduction unit 2100 includes four reduction furnaces (2100a to 2100d), the reduction unit 2100 includes three raw material transfer pipes (2111a to 2111c) and three gas transfer pipes (2112a to 2112c). can do.
  • the raw material supply device 1000 and the exhaust pipe 2210 of the hydrogen gas supply unit 2200 may be connected to the first reduction furnace 2100a among the first to fourth reduction furnaces 2100a to 2100d. That is, the raw material supply device 1000 is installed to be connected to the first reduction furnace 2100a, and the raw material discharged from the raw material supply device 1000 is charged into the first reduction furnace 2100a. And, the exhaust pipe 2210 of the hydrogen gas supply unit 2200 is connected to the first reduction furnace 2100a. Accordingly, by-products discharged from the first reduction reactor 2100a are discharged through the exhaust pipe 2210.
  • At least one of the supply pipe 2230 of the hydrogen gas supply unit 2200 and the exhaust gas supply line 4000 is connected to the fourth reduction furnace 2100d among the first to fourth reduction reactors 2100a to 2100d. Accordingly, the hydrogen gas extracted from the extractor 2220 can be supplied to the fourth reduction furnace (2100d) through the supply pipe 2230, and the exhaust gas of the dissolving device 3000 may be supplied to the fourth reduction furnace through the exhaust gas supply line 4000. It can be supplied to the furnace (2100d).
  • Raw material transfer pipes 2111a to 2111c are installed to connect the first to fourth reduction furnaces 2100a to 2100d. That is, the first raw material transfer pipe 2111a is between the first reduction reactor (2100a) and the second reduction reactor (2100b), and the second raw material transfer pipe is between the second reduction reactor (2100b) and the third reduction reactor (2100c). (2111b), a third raw material transfer pipe 2111c is installed between the third reduction furnace 2100c and the fourth reduction furnace 2100d. Accordingly, the raw material supplied to the first reduction furnace (2100a) and subjected to primary reduction is supplied to the second reduction furnace (2100b) through the first raw material transfer pipe (2111a), and is secondarily reduced in the second reduction furnace (2100b).
  • the raw materials are supplied to the third reduction furnace (2100c) through the second raw material transfer pipe (2111b), and the raw materials tertiary reduced in the third reduction furnace (2100c) are supplied to the fourth reduction furnace through the third raw material transfer pipe (2111c). It is supplied to the furnace (2100d). And the fourth reduction raw material, that is, reduced iron, in the fourth reduction reactor (2100d) is supplied to the dissolution device (3000).
  • Gas transfer pipes 2112a to 2112c are installed to connect the first to fourth reduction reactors 2100a to 2100d. That is, the first gas transfer pipe 2112a is between the fourth reduction reactor (2100d) and the third reduction reactor (2100c), and the second gas transfer pipe is between the third reduction reactor (2100c) and the second reduction reactor (2100b). (2112b), a third raw material transfer pipe 2111c is installed between the second reduction furnace 2100b and the first reduction furnace 2100a. Accordingly, the reducing gas supplied to the fourth reduction reactor (2100d) is sequentially transferred to the second to fourth reduction reactors (2100a to 2100d) through the first to third gas transfer pipes (2112a to 2112b).
  • the reducing gas supplied to the fourth reduction reactor (2100d) is supplied to the third reduction reactor (2100c) through the first gas transfer pipe (2112a), and the reducing gas supplied to the third reduction reactor (2100c) is supplied to the third reduction reactor (2100c). It is supplied to the second reduction furnace (2100b) through the second gas transfer pipe (2112b), and the reduction gas supplied to the second reduction furnace (2100b) is supplied to the first reduction furnace (2100a) through the third gas transfer pipe (2112c). is supplied as At this time, the gas supplied to the third reduction reactor (2100c), the second reduction reactor (2100b), and the first reduction reactor (2100a) through the first to third gas transfer pipes (2112a to 2112c) is supplied to the fourth reduction reactor (2100d). ) may include not only the reducing gas supplied, but also the gas generated during the reduction reaction in each reduction furnace.
  • Figure 2 is a diagram showing a reduction furnace according to an embodiment of the present invention.
  • Figure 3 is an enlarged cross-sectional view of a portion of the reduction furnace.
  • each of the first to fourth reduction furnaces 2100a to 2100d includes a container 2110 having an internal space (reduction space) that can accommodate raw materials and reduce the raw materials, and a reducing gas. It is provided with a plurality of holes 2122 through which can pass, and may include a dispersion member 2120 installed inside the container 2110. In addition, at least a portion of the container 2110 may further include a cyclone 2140 installed to collect fine powder.
  • some of the first to fourth reduction furnaces 2100a to 2100d may include a burner 2130 that generates a flame.
  • the burner 2130 is preferably provided in reduction furnaces located at both ends of the first to fourth reduction furnaces 2100a to 2100d, that is, in reduction furnaces other than the first and fourth reduction furnaces 2100a and 2100d,
  • a burner 2130 may be provided in at least one of the second and third reduction furnaces 2100b and 2100c.
  • all of the first to fourth reduction furnaces 2100a to 2100d may be provided with a burner 2130.
  • at least one of the first and fourth reduction furnaces 2100a and 2100d disposed at both ends may be provided with a burner 2130.
  • the second and third reduction furnaces 2100b and 2100c among the first to fourth reduction furnaces 2100a to 2100d will be described as an example of having a burner 2130.
  • the second reduction reactor (2100b) and the third reduction reactor (2100c) have the same configuration, and the second and third reduction reactors (2100b, 2100c) are compared with the first and fourth reduction reactors (2100a to 2100d). Therefore, there is a difference in that an additional burner 2130 is provided.
  • the reduction furnace will be described below, and then the second reduction furnace 2100b, which is one of the reduction furnaces equipped with a burner, will be described as an example with reference to FIGS. 2 and 3. And description of the first reduction reactor 2100a and the third and fourth reduction reactors 2100c and 2100d will be omitted. And the second reduction reactor 2100b described below may be simply named 'reduction reactor 2100b'.
  • the reduction furnace 2100b includes a container 2110 having an internal space (reduction space) that can accommodate raw materials and reduce the raw materials, and a plurality of holes through which reducing gas can pass. (2122), a dispersion member 2120 installed inside the container 2110, and a burner 2130 installed in the container 2110 to be located on the upper side of the dispersion member 2120 to generate a flame inside the container 2110. ) may include.
  • the reduction furnace 2100b may further include a cyclone 2140 that is at least partially installed inside the container 2110 to collect fine powder.
  • the dispersion member 2120 includes a plate-shaped body 2121 having a predetermined area and a plurality of holes 2122 provided in the body 2121 to allow gas to pass through.
  • the dispersion member 2120 may be a plate-shaped perforated plate.
  • This dispersion member 2120 is installed inside the container 2110 to divide the internal space of the container 2110 in the vertical direction. At this time, the dispersion member 2120 is preferably installed closer to the lower wall of the container 2110 than the upper wall. Accordingly, the internal space of the container 2110 may be divided into a space below the dispersion member 2120 and a space above the dispersion member 2120.
  • a gas transfer pipe 2112b may be connected to the lower part of the container 2110 to communicate with the lower space of the dispersion member 2120, and a raw material transfer pipe 2111a may be connected to communicate with the upper space of the dispersion member 2120.
  • the reducing gas is supplied to the space below the dispersion member 2120 in the internal space of the container 2110, and the raw material is supplied to the space above the dispersion member 2120. At this time, the raw materials supplied into the container 2110 are loaded on the top of the dispersion member 2120.
  • the reducing gas supplied to the lower space of the dispersion member 2120 passes through the plurality of holes 2122 of the dispersion member 2120 and moves or is injected to the upper side of the dispersion member 2120. And the raw material on the upper side of the dispersing member 2120 flows by the reducing gas injected toward the upper side of the dispersing member 2120. That is, the raw material particles on the upper side of the dispersion member 2120 flow due to the upward flow of the reducing gas passing through the plurality of holes 2122 of the dispersion member 2120. Then, the raw material flows above the dispersion member 2120 and reacts with the reducing gas to be reduced.
  • a reduction reaction occurs between the hydrogen gas supplied from the hydrogen gas supply unit 2200 and at least one of the exhaust gas exhausted from the dissolving device 3000 and supplied from the exhaust gas supply line 4000 and the raw material including iron ore.
  • the reaction between iron ore and hydrogen gas and the reaction between iron ore and carbon monoxide (CO) contained in the exhaust gas are endothermic reactions. Accordingly, the temperature inside the reduction furnace 2100b may decrease due to the endothermic reaction, which becomes a factor in reducing the reduction rate of the raw material. Therefore, for a smooth reduction reaction, it is necessary to adjust the temperature inside the reduction furnace 2100b to a predetermined temperature or higher.
  • the burner 2130 is installed in the container 2110 to generate a flame (F) to heat the inside of the container 2110.
  • the burner 2130 may be a means of blowing an oxidizing agent containing oxygen (O) into the container 2110 to generate a flame (F) through a combustion reaction.
  • O oxidizing agent containing oxygen
  • the specific structure and shape of the burner 2130 will be described later.
  • the raw material particles are melted by the high heat of the dispersion member 2120 and become entangled with each other, which may block the hole 2122 of the dispersion member 2120. If the hole 2122 is blocked, the reducing gas cannot pass through, so there is a problem in that the raw material does not flow smoothly on the upper side of the dispersion member 2120. And if the flow of raw materials is not smooth, the reduction rate of the raw materials decreases.
  • the separation distance between the dispersion member 2120 and the burner 2130 is optimized.
  • the burner 2130 is installed at an optimized height.
  • the burner 2130 is installed to be located above the dispersion member 2120. Accordingly, the separation distance between the dispersion member 2120 and the burner 2130 is defined as 'height of the burner 2130' or 'installation height of the burner 2130'.
  • the installation height is first determined, and the burner 2130 is installed at the determined height.
  • the height at which the burner 2130 is to be installed (hereinafter referred to as installation height (H b )) may be determined according to the flow rate of the reducing gas to be supplied to the reduction furnace 2100b.
  • the installation height (H b ) of the burner 2130 is determined by the diameter (d or ) of the hole 2122 of the dispersion member 2120 and the flow rate (m/sec) of the reducing gas supplied to the reduction furnace (2100b). ) can be determined by the flow rate of the reducing gas determined by .
  • the flow rate of the reducing gas to be supplied to the reduction furnace 2100b is used to determine the depth at which the reducing gas penetrates into the raw material layer on the upper side of the dispersion member 2120 ( l j ) is calculated. Then, the height (H b ) at which the burner 2130 will be installed is determined using the calculated penetration depth (l j ).
  • the depth at which the reducing gas penetrates into the raw material layer will be described using FIGS. 2 and 3.
  • Raw materials including iron ore are supplied into the container 2110 of the reduction furnace 2100b, as shown in FIG. 3, and are loaded on the upper side of the dispersion member 2120. Accordingly, the raw materials are piled up to a predetermined thickness on the upper side of the dispersion member 2120.
  • the raw material piled up to a predetermined thickness on the upper side of the dispersing member 2120 is referred to as a 'raw material layer'.
  • the raw material layer may mean a fluidized layer.
  • the reducing gas supplied to the lower side of the dispersion member 2120 passes through the plurality of holes 2122 of the dispersion member 2120 and is injected to the upper side where the raw material layer is located. Accordingly, the reducing gas penetrates into the raw material layer above the dispersion member 2120. At this time, the reducing gas is injected upward from the upper surface of the dispersion member 2120 up to a predetermined distance. That is, the reducing gas penetrates into the raw material layer above the dispersion member 2120, and penetrates to a predetermined depth.
  • the penetration depth (l j ) of the reducing gas is based on the upper surface of the dispersion member 2120.
  • the flow rate of the reducing gas to be supplied to the reducing furnace 2100b is determined.
  • the target flow rate of the reducing gas may be determined by at least one of the amount of raw material to be supplied to the reducing furnace (2100b), the volume of the container 2110 of the reducing furnace (2100b), and the target reduction rate.
  • the flow rate of the reducing gas supplied to the reduction furnace 2100b varies depending on at least one of the diameter of the hole 2122 of the dispersion member 2120 and the flow rate of the reducing gas supplied to the reduction furnace. For example, when reducing gas is supplied at a predetermined target flow rate, the larger the flow rate of reducing gas (u or ), the diameter (d or ) of the hole 2122 decreases, and the flow rate of reducing gas (u or ) decreases. As this becomes smaller, the flow rate of the reducing gas can be adjusted by increasing the hole diameter (d or ).
  • the reducing gas to be supplied to the container 2110 is determined using the determined flow rate of the reducing gas and the diameter (d or ) of the hole provided in the dispersing member 2120. Determine the flow rate (u or ).
  • the depth (l j ) at which the reducing gas penetrates into the raw material layer is predicted using this.
  • the depth l j at which the reducing gas penetrates into the raw material layer may vary depending on the flow rate of the reducing gas supplied to the container 2110. That is, the penetration depth (l j ) of the reducing gas may be determined depending on the diameter (d or ) of the hole 2122 of the dispersion member 2120 and the flow rate (u or ) of the reducing gas supplied to the reduction furnace (2100b). .
  • the penetration depth (l j ) of the reducing gas is, in addition to the diameter (d or ) of the hole 2122 of the dispersion member 2120 and the flow rate (u or ) of the reducing gas, the density ( ⁇ g ) of the reducing gas, It can be determined by the dynamic viscosity of the gas ( ⁇ ), the particle density of the raw material ( ⁇ s ), and the particle diameter of the raw material (d p ).
  • the diameter of the hole 2122 of the dispersion member 2120 (d or ), the flow rate of the reducing gas (u or ), the density of the reducing gas ( ⁇ g ), the dynamic viscosity of the reducing gas ( ⁇ ), and the raw material.
  • the depth (l j ) through which the reducing gas penetrates into the raw material layer can be calculated by calculating the particle density ( ⁇ s ) and the particle diameter (d p ) of the raw material by applying Equation 1 below.
  • the density of the reducing gas ( ⁇ g ) and the dynamic viscosity ( ⁇ ) of the reducing gas are determined depending on the reducing gas used and are known values. That is, as the reducing gas supplied to the reduction furnace 2100b, at least one of the hydrogen gas provided from the hydrogen gas supply unit 2200 and the exhaust gas provided from the dissolving device 3000 is used, so the density of these gases ( ⁇ g ) and dynamic viscosity ( ⁇ ) are applied.
  • the particle density ( ⁇ s ) of the raw material and the particle diameter (d p ) of the raw material are determined depending on the raw material supplied to the reduction furnace 2100b for producing reduced iron, and are known values. That is, the particle density ( ⁇ s ) and particle diameter (d p ), which are physical properties of the raw material to be supplied to the reduction furnace (2100b), are determined and applied.
  • Calculating and calculating the penetration depth (l j ) of the reducing gas in this way is, in other words, predicting the depth (l j ) at which the reducing gas supplied to the reduction furnace (2100b) penetrates into the raw material layer during the reduced iron manufacturing process. It could be.
  • the height (H b ) at which the burner 2130 will be installed is determined using the calculated penetration depth (l j ).
  • the installation height (H b ) is determined to be greater than or equal to the calculated penetration depth (l j ) and less than or equal to the height of the raw material layer (H m ) (see relational equation 1).
  • the height (H m ) of the raw material layer may be the distance from the upper surface of the dispersion member 2120 to the upper surface of the raw material layer.
  • the height (H m ) of this raw material layer may be the height (H m ) of the upper surface of the raw material layer before supplying the reducing gas to the reduction furnace 2100b and before the raw material flows.
  • the installation height (H b ) of the burner 2130 is 580 mm to 650 mm ( It can be determined in the range of 580 mm or more and 650 mm or less.
  • the installation height (H b ) of the burner can be determined to be 600 mm.
  • the installation height (H b ) of the burner 2130 it is determined in the range of the calculated penetration depth (l j ) or less than the height of the raw material layer (H m ), so that the 'penetration depth (l j ) or more raw material
  • the range below the floor height (H m ) can be named ‘installation height condition’.
  • the burner 2130 is installed at the determined installation height (H b ). That is, the burner 2130 is installed so that the separation distance from the dispersion member 2120 is the determined installation height (H b ). In other words, the burner 2130 is installed on the upper side of the dispersion member 2120 so that the separation distance from the upper surface of the dispersion member 2120 is the determined installation height (H b ) value. At this time, it is preferable to install the burner 2130 so that the separation distance between the radial center of the burner 2130 and the upper surface of the dispersion member 2120 is the determined installation height (H b ) value.
  • the installation height (H b ) of the burner 2130 is too low and the separation distance between the burner 2130 and the dispersing member 2120 is too close, the flow of raw materials may not be smooth and may stagnate. That is, a stagnation layer can be formed, and the stagnation layer can be formed thick. This is because the closer the distance between the burner 2130 and the dispersion member 2120 is, the closer the distance between the flame F generated from the burner 2130 and the dispersion member 2120 is. Conversely, if the installation height (H b ) of the burner 2130 is too high and the separation distance between the burner 2130 and the dispersing member 2120 is too long, the reduction reaction of the raw material may not be smooth.
  • the temperature is low and reaction with the reducing gas may not occur or may not occur sufficiently.
  • the temperature of the raw material particles flowing on the upper side of the dispersion member 2120, that is, the fluidized bed, is low, so the reduction reaction may not sufficiently occur.
  • the installation height (H b ) is determined by the above-described method, and the burner 2130 is installed at the determined installation height (H b ). Due to this, the raw materials can be sufficiently reduced while allowing them to flow smoothly without stagnation.
  • the dispersion member 2120 is suppressed or prevented from being heated to a high temperature by the heat of the flame F generated by the burner 2130, so that the raw material particles melt and stick together at a location close to the dispersion member 2120.
  • aggregation can be suppressed and prevented. Accordingly, it is possible to suppress or prevent the raw material particles from not flowing or stagnating with little flow on the upper side of the dispersing member 2120 due to the heat of the dispersing member 2120.
  • the installation height (H b ) of the burner 2130 determined by the method according to the embodiment can be explained as a height that can sufficiently reduce the raw material while suppressing or preventing the formation of the entire layer.
  • Figure 4 is a front cross-sectional view of a burner according to an embodiment of the present invention.
  • Figure 5 is a plan view of a burner according to an embodiment of the present invention.
  • Figure 6 is a diagram explaining the flow of oxidant sprayed from a burner according to an embodiment of the present invention.
  • the burner 2130 includes a main body 2131 extending in one direction, and a plurality of nozzles 2132a and 2132b, each of which is extended in an extension direction of the main body 2131 and installed inside the main body 2131.
  • the main body 2131 may be provided in a circular or cylindrical shape as shown in FIG. 5.
  • the shape of the main body 2131 is not limited to this, and it may be of any shape as long as at least a portion of it can be installed to be inserted into the container 2110 and a plurality of nozzles 2132a and 2132b can be installed therein. .
  • a plurality of nozzles 2132a and 2132b may be provided.
  • two nozzles first and second nozzles 2132a and 2132b
  • Each of the first and second nozzles 2132a and 2132b extends in the federal direction of the main body 2131 and has an internal space through which the oxidizing agent can pass.
  • one end and the other end, which are both ends in the extending direction are open.
  • Each of the first nozzle 2132a and the second nozzle 2132b may have an inner diameter of, for example, 15 mm to 20 mm, and more specifically, 16 mm to 19 mm.
  • the inner diameters of each of the first and second nozzles 2132a and 2132b may be changed in various ways.
  • each of the first and second nozzles 2132a and 2132b is an opening (hereinafter referred to as an injection port) through which the oxidizing agent is discharged or sprayed outward. Additionally, the other ends of each of the first and second nozzles 2132a and 2132b are openings (hereinafter referred to as inlets) through which the oxidizing agent flows into the first and second nozzles 2132a and 2132b.
  • an oxidizing agent supply unit (not shown) may be connected to the other end of each of the first and second nozzles 2132a and 2132b.
  • the oxidizing agent supply unit may include a reservoir in which the oxidizing agent is stored, a supply pipe connected to the first and second nozzles 2132a and 2132b to supply the oxidizing agent, and a regulator installed in the supply pipe to control at least one of the supply flow rate and flow rate of the oxidizing agent. You can.
  • the oxidizing agent contains oxygen (O), and the oxygen (O) content of the entire oxidizing agent may be 50 wt% or more and less than 100 wt%. Additionally, the oxidizing agent further contains non-oxidizing substances in addition to oxygen (O), and the content of non-oxidizing substances in the total oxidizing agent may be greater than 0 wt% and less than 50 wt%. And, the non-oxidizing material may include nitrogen (N 2 ). That is, the oxidizing agent may include oxygen (O) and nitrogen (N 2 ), and the content of oxygen (O) in the total oxidizing agent is 50 wt% or more and less than 100 wt%, and the content of nitrogen (N 2 ) is 0 wt. % may be greater than 50 wt%.
  • the oxidizing agent is not made of 100% oxygen (O) and is prepared to contain more non-oxidizing substances in addition to oxygen (O) in order to lower the temperature of the flame generated when the oxidizing agent is burned inside the reduction furnace (2100b). am. That is, if the oxidizing agent consists of 100% oxygen (O), the temperature of the flame formed inside the reduction furnace 2100b due to the combustion reaction of the oxidizing agent is too high, so a stagnant layer may be formed, and a thick stagnant layer may form. can be formed.
  • the first nozzle 2132a and the second nozzle 2132b are not arranged side by side but intersect each other. At this time, each of the first and second nozzles 2132a and 2132b may be provided to become closer to the radial center of the main body 2131 from the other end to one end. To explain this in other words, the distance between the first nozzle 2132a and the second nozzle 2132b may become closer from the other end to the one end.
  • first and second nozzles 2132a and 2132b may be inclined or provided to be slanted.
  • an imaginary line connecting the radial center of one end of the main body 2131 and the center of the direct hit direction of the other end is defined as the 'baseline (L c )'.
  • the virtual line connecting one end and the other end of the first nozzle 2132a is called 'first nozzle extension line (L n1 )'
  • the virtual line connecting one end and the other end of the second nozzle 2132b is called 'second nozzle extension line ( It is defined as ‘L n2 )’.
  • the first and second nozzle extension lines L n1 and L n2 are provided to intersect the reference line L c rather than being parallel to it.
  • each of the first and second nozzles 2132a and 2132b is provided such that the angles ⁇ 1 and ⁇ 2 formed between the first and second nozzle extension lines L n1 and L n2 and the reference line L c are acute angles. do.
  • the first and second nozzles (2132a, 2132b) each have an angle ( ⁇ 1 , ⁇ 2 ) between the first and second nozzle extension lines (L n1 , L n2 ) and the reference line (L c ) of 20°. It is prepared to be at an angle of 45°.
  • the first nozzle 2132a and the second nozzle 2132b may be provided symmetrically with respect to the reference line L c .
  • each of the first and second nozzles (2132a, 2132b) is provided to intersect the reference line (L c ) rather than being parallel to it, so that the first and second nozzles (2132a, 2132b) are inclined with respect to the reference line (L c ) It can be explained as prepared. Additionally, the first nozzle 2132a and the second nozzle 2132b are not arranged side by side but intersect each other. Accordingly, the first nozzle 2132a may be described as being inclined with respect to the second nozzle 2132b, and the second nozzle 2132b may be described as being provided inclined with respect to the first nozzle 2132a.
  • the first and second nozzles (2132a, 2132b) are inclined so that the separation distance becomes closer toward one end of the main body to collide and spread the oxidant sprayed from each of the first and second nozzles (2132a, 2132b). am.
  • the oxidizing agents OM 1 and OM 2 discharged from the injection ports of each of the first and second nozzles 2132a and 2132b are sprayed forward of the injection ports.
  • the oxidizing agent (OM 1 , OM 2 ) moves to have a flow that gets closer to the radial center of the burner 2130 as it moves away from the injection nozzle.
  • the oxidizing agent injected from the first nozzle 2132a and the oxidizing agent injected from the second nozzle 2132b collide at a point spaced a predetermined distance forward from one end of the burner 2130. After the oxidant sprayed from each of the first and second nozzles 2132a and 2132b collides, the oxidant spreads widely.
  • the oxidant sprayed from each of the first and second nozzles is sprayed in a stream shape with a predetermined width. Accordingly, the flow of a certain width formed by the oxidant sprayed from each of the first and second nozzles is defined as an 'oxidant stream'.
  • the oxidizing agent stream generated from the first nozzle 2132a and the oxidizing agent stream generated from the second nozzle 2132b collide in front of the burner. And after the plurality of oxidant streams collide, the oxidant streams spread as shown in FIG. 6. That is, multiple oxidant streams collide and combine to form one stream and spread widely. Therefore, the width of the oxidant stream widens after the collision.
  • the oxidizing agent and the gas inside the container 2110 undergo a combustion reaction inside the container 2110, thereby generating a flame. That is, at least one of CO, H 2 , and CH 4 contained in the reducing gas supplied into the container 2110 and oxygen (O) among the oxidizing agents undergo a combustion reaction, and at this time, a flame is generated. And the inside of the container 2110 is heated by the heat of the flame.
  • the width W F of the flame F may vary depending on the width of the oxidant stream injected from the nozzles 2132a and 2132b. That is, the smaller the width of the oxidant stream, the smaller the width (W F ) of the flame (F), and the larger the width of the oxidant stream, the larger the width (W F ) of the flame (F). In addition, when the oxidizing agent is sprayed at the same flow rate, the narrower the width (WF) of the flame ( F ), the higher the flame temperature, and the wider the width (WF) of the flame ( F ), the lower the flame temperature.
  • the temperature of the flame (F) may mean the highest temperature in the flame (F) having a predetermined width (W F ). And the flame (F) has the highest temperature at the center of the width direction. Accordingly, the temperature of the flame F refers to the temperature at the center of the width direction.
  • a low temperature of the flame (F) means that the maximum temperature at the center of the width direction is relatively low
  • a high temperature of the flame (F) means that the maximum temperature at the center of the width direction is relatively high. do.
  • a burner capable of forming a flame with a wider width than before was provided. That is, a porous burner 2130 that can spread the oxidant widely by colliding with the injected oxidant is provided.
  • a plurality of nozzles (2132a, 2132b) are provided, each capable of spraying an oxidizing agent, and each nozzle (2132a, 2132b) increases in diameter of the main body (2131) toward one end of the main body (2131). It is tilted so that it approaches the center of direction.
  • the oxidant streams sprayed from each of the plurality of nozzles 2132a and 2132b collide, causing the oxidant streams to spread widely. Therefore, as the combustion reaction occurs in the oxidant stream having a wide width, a wide flame can be formed. And accordingly, the temperature of the flame can be lowered compared to before. That is, compared to the flame generated from a conventional single-hole burner with one nozzle, the temperature of the flame generated from the multi-hole burner 2130 with a plurality of nozzles 2132a and 2132b as in the embodiment is lower.
  • the burner 2130 is installed at the same height, the higher the temperature of the flame F generated from the burner 2130, the higher the temperature of the dispersion member 2120, so that the tablet layer is easily formed, and the purification layer is easily formed.
  • the thickness of the layer may be thick.
  • the burner 2130 has two nozzles 2132a and 2132b.
  • the nozzles may be provided in various numbers exceeding two.
  • angles ( ⁇ 1 , ⁇ 2 ) formed by each of the first nozzle 2132a and the second nozzle 2132b with the reference line L c are less than 20° or more than 45°, collisions between oxidant streams do not occur. Otherwise, the amount of conflict may be insufficient. That is, when the inclined angle ( ⁇ 1 , ⁇ 2 ) of at least one of the first nozzle 2132a and the second nozzle 2132b is less than 20° or exceeds 45°, the spray from the first nozzle 2132a The oxidizing agent stream and the oxidizing agent stream sprayed from the second nozzle 2132b may not collide, or the amount of collision may be small.
  • the diffusion of the oxidant stream may be insufficient, so a narrow-width flame (F) may be formed, and accordingly, the temperature of the flame (F) may be high. Therefore, the angles ( ⁇ 1 , ⁇ 2 ) of the first and second nozzles 2132a and 2132b are adjusted to 20° to 45°.
  • the oxidant stream sprayed from the first and second nozzles (2132a, 2132b) is formed to be inclined. do. That is, the oxidant streams injected from the first and second nozzles 2132a and 2132b are formed in an inclined shape so that the farther away they are from one end of the main body 2131, the closer they are to the center of the diameter of the main body 2131.
  • the flow rate of the oxidizing agent spraying from each nozzle 2132a and 2132b is adjusted to 80 m/s to 100 m/s.
  • the flow rate of the oxidant sprayed from the first and second nozzles (2132a, 2132b) is adjusted to 80 m/s to 100 m/s.
  • the flow rate of the oxidant sprayed from at least one of the first and second nozzles 2132a and 2132b is less than 80 m/s, the oxidant stream sprayed from the first nozzle 2132a and the oxidant sprayed from the second nozzle 2132b Streams may not collide, or the amount of collision may be small.
  • the flow rate of the oxidant sprayed from at least one of the first and second nozzles 2132a and 2132b exceeds 100 m/s, the temperature of the flame is high, which may promote the formation of a stagnation layer. Therefore, it is desirable to adjust the flow rate of the oxidant sprayed from the first and second nozzles 2132a and 2132b to 80 m/s to 100 m/s.
  • Figure 7 is a diagram schematically showing an experimental reduction reactor.
  • Figure 8 shows the results of measuring the temperature in the horizontal direction at a predetermined height of the experimental reduction furnace.
  • Figure 9 shows the results of measuring the temperature of the area from the dispersion member to a predetermined height upward in the experimental reduction furnace.
  • Figures 8 (a) and Figure 9 (a) show the results of an experiment when a burner (single-hole burner) with one nozzle was installed in an experimental reduction furnace to generate a flame.
  • Figures 8 (b) and Figure 9 (b) are the results of an experiment when a flame was generated by installing a burner (porous burner) with a plurality of nozzles according to the embodiment in the experimental reduction furnace. .
  • the experimental reduction reactor shown in FIG. 7 is similar in configuration to the actual reduction reactor shown in FIG. 2. That is, the experimental reduction furnace includes a container 21, a dispersion member 22 having a plurality of holes through which the reducing gas can pass, and a burner that generates a flame.
  • the experiment was conducted by installing a first type of burner with one nozzle in a container, and the experiment was performed by installing a second type of burner in the container. did.
  • the first type burner and the second type burner were installed at the same height. Accordingly, the first type of burner and the second type of burner will be described by referring to the same reference numeral '23a'.
  • a first type burner 23a is installed in the container.
  • the installation height (H b1 ) of the burner 23a was installed at a position 350 mm above the dispersion member 22 .
  • an oxidizing agent was supplied to the first type of burner 23a and a reducing gas was supplied into the container 21, thereby generating a flame inside the container 21.
  • hydrogen gas was used as the reducing gas.
  • the temperature inside the container 21 was measured. At this time, the temperature was measured in the horizontal direction at the height (H b1 ) (350 mm) where the first type of burner 23a is installed, and the results are shown in (a) of FIG. 8. Additionally, the temperature of a predetermined area was measured upward from the dispersing member 22, and the results are shown in (a) of FIG. 9.
  • the installation height (H b1 ) of the second type burner (23a) was set to 350 mm, the same as the height (H b1 ) of the first type burner (23a) described above.
  • an oxidizing agent was supplied to the second type of burner 23a and hydrogen gas, a reducing gas, was supplied into the container 21 to generate a flame inside the container 21.
  • the flow rates of the supplied oxidizing agent and reducing gas were the same as in the experiment using the first type of burner 23a.
  • the width (W F1 ) of the flame generated by the first type of burner 23a at the same position is greater than that of the flame generated by the second type of burner 23a.
  • the width of the flame (W F2 ) is wide. More specifically, when comparing the width of the flame at a position spaced apart from the first and second types of burners 23a by a first distance D 1 in the horizontal direction, the flame width is compared by the first type of burner 23a.
  • the width (W F2 ) of the flame generated by the second type of burner 23a ((b) in FIG. 8) is wider than the width (W F1 ) of the generated flame ((a) in FIG. 8). From this, it can be seen that when using the burner 2130 according to the embodiment, the width of the flame can be increased.
  • the temperature of the dispersion member 22 is lower in Figure 9 (b) than in Figure 9 (a).
  • the temperature of the dispersion member 22 located at a second distance D 2 in the horizontal direction from the first type of burner 23a is as high as about 1500°C.
  • the temperature of the dispersion member 22 located at a second distance D 2 in the horizontal direction from the second type of burner 23a is as low as about 1100°C. From this, it can be seen that when using the burner 2130 according to the embodiment, the temperature of the dispersion member 2120 can be lowered.
  • Figure 10 shows a burner of the first type having one nozzle installed in the vessel of an experimental reduction furnace to generate a flame
  • Figure 11 shows a burner of the second type having first and second nozzles in the vessel of the experimental reduction furnace. This is the result showing the temperature distribution by height inside the container when a burner is installed to generate a flame.
  • the second type of burner may be a burner according to the embodiment.
  • the first burner 23a the first type of burner installed at a relatively low height
  • the first type of burner installed relatively high compared to the first burner 23a is called the second burner 23b.
  • the first burner 23a was installed at a height (H b1 ) spaced 350 mm upward from the dispersion member 22, and the second burner 23b was installed at a height (H b1) spaced 600 mm upward from the dispersion member 2120. It was installed located at H b2 ).
  • 10(c) and 11(c) show the temperature distribution in the horizontal direction at a height where the first and second burners 23a and 23b are not installed and the separation distance from the dispersion member 2120 is close. This is the result of measurement. That is, the horizontal temperature distribution is below the first burner 23a, which has a relatively low height among the first and second burners 23a and 23b, and at a height spaced 100 mm upward from the dispersion member 22.
  • the temperature of the first area A 1 facing the first burner 23a of the first type at a height spaced 100 mm upward from the dispersion member 22 is about 1723°C. (2000K) or higher.
  • the temperature of the first area A 1 facing the first burner 23a of the second type at a height spaced 100 mm upward from the dispersion member 22 is It is lower than the temperature of the first area (A 1 ) in (c). That is, in Figure 11 (c), the temperature of the first area (A 1 ) is as low as 1650°C or lower.
  • the second type of burner is equipped with a plurality of nozzles and is equipped to collide the oxidizing agent, that is, the burner according to the embodiment is used
  • the temperature of the dispersion member and its surroundings can be lowered.
  • the temperature at the same height can be lowered when using the burner according to the embodiment compared to when using the first type of burner (conventional burner) equipped with one nozzle. there is.
  • the height (H b ) of the burner 2130 is optimized and installed as described above. That is, the burner 2130 is installed at a location where the separation distance from the dispersion member 2120 is optimized. Accordingly, it is possible to suppress or prevent the dispersion member 2120 from being heated to a high temperature by the heat of the flame F generated from the burner 2130. Therefore, it is possible to prevent the raw material particles from melting and sticking together or agglomerating at a location close to the dispersion member 2120. Accordingly, it is possible to suppress or prevent the formation of a stagnation layer on the upper part of the dispersion member 2120, and thus the raw materials can flow smoothly inside the reduction furnace. Additionally, sufficient heat can be applied to the raw materials and reducing gas to ensure that the reduction reaction occurs smoothly.
  • the temperature of the flame F can be lowered. That is, the burner 2130 according to the embodiment sprays the oxidizing agent using a plurality of nozzles 2132a and 2132b that are inclined to intersect each other, causing the oxidizing agent to collide and spread. Accordingly, the width of the oxidant stream injected in front of the burner 2130 can be increased, and thus a low-temperature flame F can be formed. Therefore, it is possible to prevent the dispersion member 2120 and the raw material from being heated to an excessively high temperature by a high-temperature flame. Accordingly, agglomeration due to melting of raw material particles can be suppressed, thereby suppressing or preventing the formation of a stagnation layer. Therefore, raw materials can flow smoothly inside the reduction furnace 2100b.
  • the dispersion member it is possible to suppress or prevent the dispersion member from being heated to a high temperature by the heat of the flame generated from the burner. Additionally, it is possible to generate a flame at a lower temperature than before. Accordingly, agglomeration due to melting of raw material particles can be suppressed or prevented, and thus the formation of a stagnation layer can be suppressed or prevented. Therefore, raw materials can flow smoothly inside the reduction furnace.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Manufacture Of Iron (AREA)

Abstract

Un four de réduction, selon un mode de réalisation de la présente invention, peut comprendre : un récipient ayant un espace interne apte à recevoir une matière première comprenant du minerai de fer et un gaz réducteur ; un élément de dispersion installé à l'intérieur du récipient et ayant une pluralité de trous à travers lesquels le gaz réducteur peut passer ; et un brûleur installé au-dessus de l'élément de dispersion à une hauteur espacée de l'élément de dispersion déterminé en utilisant un débit cible du gaz réducteur à fournir dans le récipient, et apte à générer une flamme à l'intérieur du récipient. Par conséquent, selon des modes de réalisation de la présente invention, il est possible d'empêcher ou d'éviter que l'élément de dispersion ne soit chauffé à une température élevée par la chaleur de la flamme générée à partir du brûleur. De plus, il est possible de générer une flamme à une température inférieure par rapport à l'état de la technique. Par conséquent, il est possible d'inhiber ou d'empêcher l'agglomération due à la fusion de particules de matière première, et ainsi d'inhiber ou d'empêcher la formation d'une couche de stagnation. Par conséquent, il est possible de permettre à la matière première de s'écouler sans à-coups à l'intérieur du four de réduction.
PCT/KR2023/003103 2022-11-22 2023-03-07 Four de réduction et procédé de production de fer réduit Ceased WO2024111758A1 (fr)

Priority Applications (3)

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CN202380023996.5A CN118871597A (zh) 2022-11-22 2023-03-07 还原炉和用于生产还原铁的方法
EP23894694.1A EP4624595A1 (fr) 2022-11-22 2023-03-07 Four de réduction et procédé de production de fer réduit
JP2024551579A JP2025506896A (ja) 2022-11-22 2023-03-07 還元炉及び還元鉄の製造方法

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KR10-2022-0157410 2022-11-22
KR1020220157410A KR20240076517A (ko) 2022-11-22 2022-11-22 환원로 및 환원철의 제조 방법

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Citations (6)

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