WO2022227801A1 - 一种含铁物料复合喷吹方法及系统 - Google Patents

一种含铁物料复合喷吹方法及系统 Download PDF

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WO2022227801A1
WO2022227801A1 PCT/CN2022/076645 CN2022076645W WO2022227801A1 WO 2022227801 A1 WO2022227801 A1 WO 2022227801A1 CN 2022076645 W CN2022076645 W CN 2022076645W WO 2022227801 A1 WO2022227801 A1 WO 2022227801A1
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iron
injection
containing material
stage
fluidization device
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PCT/CN2022/076645
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English (en)
French (fr)
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张冠琪
王金霞
陈庆孟
张晓峰
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山东墨龙石油机械股份有限公司
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Publication of WO2022227801A1 publication Critical patent/WO2022227801A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • 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
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0066—Preliminary conditioning of the solid carbonaceous reductant

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  • the present application relates to the technical field of raw fuel pretreatment of smelting reduction process, in particular to a method and system for composite injection of iron-containing materials.
  • the iron bath smelting reduction process is a smelting reduction metallurgical process using non-coking coal pulverized coal and iron ore powder, and a smelting method of reducing iron oxides into metallic iron with carbon in a high temperature melting state.
  • the smelting reduction production process is mainly based on the "two-step method", that is, the "pre-reduction” + “final reduction” process.
  • the fluidized bed technology used in the iron bath smelting reduction process uses the high-temperature gas generated by the smelting reduction furnace to preheat the ore powder, but the traditional fluidized bed process directly uses the gas generated by the smelting reduction furnace.
  • the gas has a high degree of oxidation and high quality. Poor, the reduction ability is poor, and only through the first-stage circulating fluidized bed pre-reduction, resulting in poor pre-reduction effect of iron-containing materials, the pre-reduction degree is lower than 20%.
  • the pulverized coal and ore powder are transported by two different conveying pipelines, connected with different solid lances and injected into the smelting reduction furnace, and the mixing effect of the pulverized coal and the smelting reduction furnace after entering the smelting reduction furnace Poor, the coal powder enters the furnace with low temperature and low surface activity, which seriously affects the heat transfer and mass transfer reaction rate of the smelting reduction reaction.
  • the pulverized coal needs to absorb a large amount of heat to reach the reaction temperature before the smelting reduction reaction can proceed, the reaction time is prolonged, and the reaction is not sufficient, and some material particles will be carried out of the furnace with the rising gas, resulting in waste of materials.
  • the pretreatment stage of raw fuel becomes the limiting link of the whole smelting reduction process.
  • the present application provides a method and system for composite injection of iron-containing materials.
  • the iron-containing material composite injection method and system provided by the present application can increase the preheating temperature of the iron-containing material, increase the pre-reduction degree of the iron-containing material, and the iron-containing material is pre-mixed with pulverized coal and flux in the conveying pipeline.
  • the large amount of sensible heat carried by the iron-containing material after preheating is efficiently used to preheat the pulverized coal and the flux, which increases the temperature of the pulverized coal entering the smelting reduction furnace, optimizes the reaction conditions of the molten pool, and improves the reaction rate of the molten pool.
  • the production capacity of the smelting reduction process is effectively improved, the comprehensive utilization efficiency of energy is improved, the coal consumption is reduced, and the energy consumption index of the smelting reduction technology is improved.
  • the iron-containing material is crushed and ground, the iron-containing material is subjected to dehydration and drying treatment and a first-stage preheating and pre-reduction treatment, and the temperature of the first reducing gas of the first-stage preheating and pre-reduction treatment is 500- 700°C, CO content is 10-20%;
  • the dehydration and drying treatment and the first-stage preheating and pre-reduction treatment of the iron-containing material include:
  • the iron-containing material enters the first-stage fluidization device through the first inlet at the bottom of the first-stage fluidization device, and the first reducing gas enters the first-stage fluidization device through the first air inlet at the bottom of the first-stage fluidization device.
  • Convective heat exchange is performed between the material and the first reducing gas, and the first reducing gas performs dehydration and drying treatment and a first-stage preheating and pre-reduction treatment on the iron-containing material
  • the iron-containing material and the first reducing gas are discharged through the first discharge port on the upper part of the first-stage fluidization device and enter the first cyclone for gas-solid separation to obtain the iron-containing material after the first-stage preheating and pre-reduction treatment.
  • material and the first reduction waste gas the first reduction waste gas is discharged through the exhaust port at the top of the first cyclone separator and enters the reduction waste gas storage tank,
  • the pre-reduction degree of the iron-containing material after the first-stage preheating and pre-reduction treatment is 0%-20%, and the temperature of the first reduction waste gas is 150°C-250°C,
  • the reduction reactions in the first-stage fluidized device are: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 .
  • the second-level preheating and pre-reduction treatment of the iron-containing material after the first-stage preheating and pre-reduction treatment includes:
  • the iron-containing material after the first-stage preheating and pre-reduction treatment enters the second-stage fluidization device through the second feed port at the bottom of the second-stage fluidization device, and the second reducing gas passes through the second feed at the bottom of the second-stage fluidization device.
  • the gas port enters the second-stage fluidization device, and the iron-containing material after the first-stage preheating and pre-reduction treatment conducts convective heat exchange with the second reducing gas, and the second reducing gas preheats the first-stage
  • the iron-containing material after pre-reduction treatment is subjected to secondary preheating and pre-reduction treatment,
  • the iron-containing material after the first-stage preheating and pre-reduction treatment and the second reducing gas are discharged through the second discharge port on the upper part of the second-stage fluidization device and enter the second cyclone for gas-solid separation to obtain two.
  • the iron-containing material after preheating and pre-reduction treatment in the second stage and the second reduction waste gas are recycled into the first-stage fluidization device as the first reducing gas, and the iron-containing material after the second-stage preheating and pre-reduction treatment is recycled. It is discharged to the pretreatment sealed tank through the discharge port at the bottom of the second cyclone separator or circulated back to the second-stage fluidization device through the return material.
  • the temperature of the iron-containing material after the secondary preheating and pre-reduction treatment is 600°C-800°C, and the pre-reduction degree is 40%-70%,
  • the reactions occurring in the second-stage fluidization device are: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 , Fe 3 O 4 +CO ⁇ CO 2 +3FeO, FeO+CO ⁇ CO 2 +Fe.
  • the iron-containing materials described in step (1) are iron concentrate, hematite powder, limonite powder, siderite powder, red mud, etc.
  • the iron content in the iron-containing material is not less than 30%; the particle size of the iron-containing material after crushing and grinding is less than 3 mm; the injection volume of the iron-containing material It is 20 ⁇ 280t/h.
  • the proportion of the coal powder in step (3) is 40%-50% of the iron-containing material
  • the pulverized coal is one or more of injection coal, bituminous coal, semi-coke, blue charcoal, and peat, the carbon content of the pulverized coal is greater than 70%, and the particle size is less than 5 mm; and/or
  • step (3) the mixing ratio of the flux is 13%-17% of the iron-containing material
  • Described flux is basic flux, and described flux is the mixture of dolomite and lime,
  • the content of magnesium oxide in the dolomite is not less than 17%, the particle size of the dolomite is less than 10mm,
  • the content of calcium oxide in the lime is not less than 70%, the particle size of the lime is less than 3mm,
  • the mixing ratio of the dolomite and the lime is determined by the binary basicity and the quaternary basicity of the slag, and the mixing ratio of the lime and the dolomite is:
  • R 2 CaO/SiO 2
  • R 4 (CaO+MgO)/(SiO 2 +Al 2 O 3 ).
  • the carrier gas flow rate of the iron-containing material injection carrier gas in step (4) is 0-15000Nm 3 /h, and the injection pressure is 100-500kPa ;and / or
  • the carrier gas flow rate of the pulverized coal and flux injection carrier gas in step (4) is 0-8000Nm 3 /h, and the injection pressure is 100-500kPa; and/or
  • the injection pressure of the carrier gas for the mixture material is 100-500kPa.
  • an iron-containing material composite injection system based on any one of the above-mentioned iron-containing material composite injection methods, wherein:
  • the system includes an iron-containing material pretreatment subsystem and a composite injection subsystem;
  • the iron-containing material pretreatment subsystem includes a first-stage fluidization device, a second-stage fluidization device, a first cyclone separator, and a second cyclone separator,
  • the first-stage fluidization device and the second-stage fluidization device are arranged in series, and the second-stage fluidization device is provided between the first outlet of the first-stage fluidization device and the second inlet of the second-stage fluidization device.
  • a cyclone separator the second cyclone separator is arranged between the second outlet of the second-stage fluidization device and the first air inlet of the first-stage fluidization device,
  • the one-stage fluidization device adopts one of a circulating fluidization device, a bubbling fluidization device, and an annular fluidization device, and/or
  • the second-stage fluidization device adopts a circulating fluidization device
  • the composite injection subsystem includes a hot ore injection device, a pulverized coal/flux injection device, a composite injection pipeline, and a solid injection gun,
  • the hot ore injection device is connected with the second-stage fluidization device, and the hot ore injection device includes a hot ore injection tank, a rotary feeder, and a first injection pipeline connected in sequence,
  • the pulverized coal/flux injection device includes a pulverized coal injection device, a flux injection device, and a second injection pipeline,
  • the pulverized coal injection device and the flux injection device are jointly connected to the second injection pipeline,
  • the second injection line merges with the first injection line to form the composite injection line, and the composite injection line is connected to the solid lance of the smelting reduction furnace.
  • the composite injection subsystem further includes:
  • a flow regulating and pressure regulating valve is arranged in front of the junction of the first injection line and the second injection line, and the flow and pressure regulating valve is used to adjust the flow of the medium in the pipeline and carry out Pressure regulation in the range of large differential pressure;
  • the pneumatic three-way ball valve ball valve group is set at the junction of pipelines, and consists of a pneumatic actuator and a T-type pneumatic three-way ball valve.
  • the pneumatic actuator is used to receive control signals, synchronously drive and control three
  • the action and opening and closing state of the ball valve, the T-type pneumatic three-way ball valve is used to control the confluence of the medium in the pipeline;
  • the pressure transmitter is arranged before the confluence of the flow regulating and pressure regulating valve, the first injection line and the second injection line, and the pressure transmitter is used to regulate the The injection pressure of the carrier gas in the first injection line and the second injection line.
  • the end of the composite injection pipeline is separated into several branch pipes, which are respectively connected to each solid injection gun of the smelting reduction furnace;
  • the flow rate of the mixed material in the branch pipes; each branch pipe is equipped with an air supply device for supplementing the carrier gas;
  • the number of solid spray guns is at least two, and the solid spray guns are provided with anti-blocking parts to prevent slag iron from blocking the Solid spray gun.
  • the iron-containing material pretreatment subsystem further includes:
  • a pretreatment sealing tank which is connected to the second cyclone separator and the second-stage fluidization device;
  • the hot ore injection tank is connected with the pretreatment sealing tank, iron-containing materials are transported between the pretreatment sealing tank and the hot ore injection tank by gravity, the pretreatment A high temperature dome feed valve and a rotary exhaust valve are arranged between the sealing tank and the hot ore injection tank, and a rotary discharge valve is also provided at the discharge port of the hot ore injection tank.
  • the method for composite injection of iron-containing materials provided by this application, by setting a first-stage fluidization device and a second-stage fluidization device, carries out secondary preheating and pre-reduction reaction to iron-containing materials, which greatly improves the iron-containing materials.
  • Pre-reduction degree, high degree of recycling of the first reducing gas and second reducing gas, high energy utilization rate, the temperature of the iron-containing material after the secondary preheating and pre-reduction treatment reaches 600 °C -800 °C The degree reaches 40%-70%.
  • the temperature of the furnace can reach more than 200 °C, the reaction conditions in the smelting reduction furnace are optimized, the smelting efficiency of the molten pool is improved, the kinetic conditions of the reduction reaction are improved, and the melting reaction of pulverized coal in the smelting reduction furnace is promoted.
  • the absorption rate of pulverized coal in the smelting reduction furnace is increased by more than 10%, the amount of pulverized coal particles in the flue gas is reduced, and the carbon content of the dust dust is reduced by more than 20%; , pulverized coal and flux are fully mixed during the conveying process, which improves the mixing uniformity, is conducive to the full reaction of materials in the smelting reduction furnace, and reduces material loss.
  • the second reducing waste gas discharged from the second-stage fluidization device is cyclically transported to the first-stage fluidization device, and used as the first reducing gas in the first-stage fluidization device.
  • the iron-containing material is subjected to dehydration and drying treatment and first-stage preheating and pre-reduction treatment, which improves the degree of gas recycling and energy utilization.
  • Fig. 1 is used to illustrate a kind of schematic flow diagram of the composite injection method of iron-containing material in one or more embodiments of the present application;
  • FIG. 2 is used to illustrate a schematic structural diagram of the iron-containing material composite injection system in one or more embodiments of the present application.
  • the existing smelting reduction production process directly utilizes the coal gas produced by the smelting reduction furnace, so that the coal gas has a high degree of oxidation, poor quality and poor reducing ability, and is pre-reduced only by the first-stage circulating fluidized bed, resulting in the pre-reduction effect of iron-containing materials. Poor, the pre-reduction degree is less than 20%.
  • the pulverized coal and the iron-containing material are transported by two different conveying pipelines, so that the mixing effect of the pulverized coal and the iron-containing material is poor, the temperature of the pulverized coal entering the furnace is low, and the surface activity is low. , which seriously affects the heat transfer and mass transfer reaction rates of the smelting reduction reaction. Therefore, the pretreatment stage of the raw fuel becomes the limiting link of the existing smelting reduction process.
  • a composite injection method for iron-containing materials as shown in FIG. 1 , the method includes the following steps:
  • the iron-containing material is crushed and ground, the iron-containing material is subjected to dehydration and drying treatment and first-stage preheating and pre-reduction treatment.
  • the temperature of the first reducing gas in the first-stage preheating and pre-reduction treatment is 500-700 ° C, CO
  • the content is 10-20%;
  • the premixed mixture is injected into the smelting reduction furnace, wherein the iron-containing material injection carrier gas, coal powder and flux injection carrier gas, and the mixture material injection carrier gas are all first-stage preheating and prereduction The treated first reduction exhaust gas.
  • the dehydration and drying treatment and the first-stage preheating and pre-reduction treatment of the iron-containing material include:
  • the iron-containing material enters the first-stage fluidization device 41 through the first feed port 412 at the bottom of the first-stage fluidization device 41, and the first reducing gas enters the first-stage fluidization device 41 through the first air inlet 411 at the bottom of the first-stage fluidization device 41,
  • the iron-containing material is subjected to convection heat exchange with the first reducing gas, and the first reducing gas is used to dehydrate and dry the iron-containing material and perform a first-stage preheating and pre-reduction treatment.
  • the iron-containing material and the first reducing gas are discharged through the first discharge port 413 in the upper part of the first-stage fluidization device 41 and enter the first cyclone separator 43 for gas-solid separation to obtain the iron-containing material after the first-stage preheating and pre-reduction treatment. and the first reduction waste gas, the first reduction waste gas is discharged through the exhaust port at the top of the first cyclone separator 43 and enters the reduction waste gas storage tank 5,
  • the pre-reduction degree of the iron-containing material after the first-stage preheating and pre-reduction treatment is 0%-20%, and the temperature of the first reduction waste gas is 150°C-250°C,
  • the reduction reactions occurring in the first-stage fluidization device 41 are: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 .
  • performing the secondary preheating and prereduction treatment on the iron-containing material after the primary preheating and prereduction treatment includes:
  • the iron-containing material after the first-stage preheating and pre-reduction treatment enters the second-stage fluidization device through the second feed port 422 at the bottom of the second-stage fluidization device 42, and the second reducing gas passes through the second-stage fluidization device 42.
  • the air inlet 421 enters the second-stage fluidization device 42, and the iron-containing material after the first-stage preheating and pre-reduction treatment is subjected to convective heat exchange with the second reducing gas, and the second reducing gas is used for the first-stage preheating and pre-reduction treatment.
  • the iron-containing material is subjected to secondary preheating and prereduction treatment.
  • the iron-containing material and the second reducing gas after the first-stage preheating and pre-reduction treatment are discharged through the second discharge port 423 at the upper part of the second-stage fluidization device 42 and enter the second cyclone separator 44 for gas-solid separation to obtain a second-stage fluidization device 44.
  • the iron-containing material and the second reduction waste gas after preheating and pre-reduction treatment are preheated.
  • the second reduction waste gas is circulated into the first-stage fluidization device 41 as the first reducing gas, and the iron-containing material after the second-stage preheating and pre-reduction treatment is passed through the second cyclone.
  • the discharge port at the bottom of the separator 44 is discharged to the pretreatment sealing tank 427 or recycled to the second-stage fluidization device 42 through the return material 426,
  • the temperature of the iron-containing material after the secondary preheating and pre-reduction treatment is 600°C-800°C, and the pre-reduction degree is 40%-70%.
  • the reactions occurring in the second-stage fluidization device 42 are: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 , Fe 3 O 4 +CO ⁇ CO 2 +3FeO, and FeO+CO ⁇ CO 2 +Fe.
  • the iron-containing material is iron powder, hematite iron-containing material, limonite iron-containing material, siderite iron-containing material, red mud and other industrial solid wastes, iron oxide scales and other industrial solid wastes.
  • the iron content in the iron-containing material is not less than 30%; the particle size of the iron-containing material after crushing and grinding is less than 3mm; the injection volume of the iron-containing material is 20-280t/h.
  • the proportion of coal powder in step (3) is 40%-50% of the iron-containing material
  • the pulverized coal is one or more of injection coal, bituminous coal, semi-coke, blue charcoal, and peat, the carbon content of the pulverized coal is greater than 70%, and the particle size is less than 5 mm; and/or
  • the proportion of the flux is 13%-17% of the iron-containing material
  • the flux is an alkaline flux, and the flux is a mixture of dolomite and lime,
  • the content of magnesium oxide in dolomite is not less than 17%, the particle size of dolomite is less than 10mm,
  • the content of calcium oxide in lime is not less than 70%, the particle size of lime is less than 3mm,
  • the proportion of dolomite and lime is determined by the binary alkalinity and quaternary alkalinity of the slag.
  • the proportion of lime and dolomite is as follows:
  • R 2 CaO/SiO 2
  • R 4 (CaO+MgO)/(SiO 2 +Al 2 O 3 ).
  • the carrier gas flow rate of the iron-containing material jetting the carrier gas is 0-15000Nm 3 /h, and the jetting pressure is 100-500kPa; and/or
  • step (4) the carrier gas flow rate of pulverized coal and flux injection carrier gas is 0-8000Nm 3 /h, and the injection pressure is 100-500kPa; and/or
  • step (4) the injection pressure of the carrier gas for the mixture material is 100-500kPa.
  • Embodiment 1 of the present application provides a composite injection method for iron-containing materials, comprising the following steps:
  • the iron-containing material is crushed and ground by the ball mill 1, it is transported to the first-stage fluidization device 41 at a fixed speed through the belt conveyor 2 and the screw feeder 3, and the iron-containing material passes through the first-stage fluidization device 41.
  • the feed port 412 enters the first-stage fluidization device 41
  • the first reducing gas enters the first-stage fluidization device 41 through the first air inlet 411 at the bottom of the first-stage fluidization device 41
  • the iron-containing material conducts convective heat exchange with the first reducing gas.
  • the first reducing gas performs dehydration and drying treatment on iron-containing materials and a first-stage preheating and pre-reduction treatment.
  • the temperature of the first reducing gas in the first-stage preheating and pre-reduction treatment is 500-700 °C, and the CO content is 10-20 %
  • the iron-containing material and the first reducing gas are discharged together through the first discharge port 413 in the upper part of the first-stage fluidization device 41 and enter the first cyclone separator 43, where the iron-containing material and the first cyclone separator 43
  • the reducing gas undergoes gas-solid separation to obtain the iron-containing material after the first-stage preheating and pre-reduction and the first reduction waste gas.
  • the iron-containing material after the first-stage preheating and pre-reduction is discharged through the discharge port at the bottom of the first cyclone 43, And rely on gravity to enter the second-stage fluidization device 42 through the feed port at the bottom of the second-stage fluidization device 42, and the first reduction waste gas is discharged to the reduction waste gas storage tank 5 through the exhaust port at the top of the first cyclone separator 43;
  • the obtained reformed coal gas is used as the second reducing gas.
  • the feed port 422 enters the second-stage fluidization device, and the second reducing gas enters the second-stage fluidization device 42 through the second air inlet 421 at the bottom of the second-stage fluidization device 42.
  • the iron-containing Convective heat exchange is performed between the material and the second reducing gas, and the iron-containing material after the first-stage preheating and pre-reduction treatment is subjected to a second-stage preheating and pre-reduction treatment by the second reducing gas.
  • the second discharge port 423 in the upper part of the stage fluidization device 42 is discharged and enters the second cyclone separator 44.
  • the iron-containing material and the second reducing gas are subjected to gas-solid separation to obtain a secondary preheater.
  • the iron-containing material and the second reduction waste gas after the thermal pre-reduction treatment, the iron-containing material after the second-stage preheating and pretreatment is discharged to the pretreatment sealing tank 427 through the discharge port at the bottom of the second cyclone separator 44 or circulated through the return material 426
  • the second reduced waste gas is discharged through the exhaust port at the top of the second cyclone separator 44 , and circulated as the first reducing gas through the first air inlet 411 at the top of the first-stage fluidization device 41 .
  • the premixed mixed material enters each solid lance 64 of the smelting reduction furnace 7 through the composite injection line 63 and several branch pipes 632, and is mixed and injected into the smelting reduction furnace 7 through each solid lance 64, wherein the iron-containing material
  • the injection carrier gas, the pulverized coal and flux injection carrier gas, and the mixed material injection carrier gas are the first reduction waste gas of the first-stage preheating and prereduction treatment.
  • the iron-containing material is one or more of industrial solid wastes such as iron concentrate, hematite powder, limonite powder, siderite powder, red mud, and iron oxide scale, and the iron content in the iron-containing material is not Below 30%, the particle size of the iron-containing material after crushing and grinding is less than 3mm, and the injection rate of the iron-containing material is 20-280t/h.
  • the proportion of pulverized coal is 40%-50% of the iron-containing material
  • the pulverized coal is one or more of injection coal, bituminous coal, semi-coke, blue charcoal, and peat
  • the carbon content of the pulverized coal is More than 70%
  • the particle size is less than 5mm.
  • the mixing ratio of the flux is 13%-17% of the iron-containing material
  • the flux is an alkaline flux
  • the flux is a mixture of dolomite and lime, wherein the particle size of the dolomite is less than 10 mm, and the content of magnesium oxide in the dolomite is less than 10 mm.
  • the particle size of the lime is less than 3mm, and the content of calcium oxide in the lime is not less than 70%.
  • the flux is used to remove acid impurities in raw materials, generate low melting point substance Ca 2 SiO 4 , reduce slag viscosity and melting temperature, and make slag flow easily.
  • the carrier gas flow rate of the iron-containing material injection carrier gas is 0-15000Nm 3 /h, and the injection pressure is 100-500kPa.
  • the carrier gas flow rate of the pulverized coal and flux injection carrier gas is 0-8000Nm 3 /h, and the injection pressure is 100-500kPa.
  • the injection pressure of the mixture material to inject the carrier gas is 100-500 kPa.
  • the above-mentioned iron-containing material pretreatment method has small solid-gas ratio, fast heat transfer and mass transfer rate, and can effectively improve the pre-reduction degree of iron-containing material and the limit value of preheating temperature; two-stage preheating pretreatment can realize grading utilization of energy , in a limited reaction time, improve the utilization of energy.
  • the iron-containing material undergoes the above-mentioned two-stage preheating and pre-reduction treatment, which is beneficial to improve the rate of the smelting reduction reaction; at the same time, it is beneficial to further increase the production capacity, reduce the coal consumption, and improve the energy consumption index of the smelting reduction technology.
  • Table 1 the temperature and prereduction degree of iron-containing materials under different parameters are shown in Table 1.
  • the above composite injection method can efficiently utilize a large amount of sensible heat carried by the iron-containing material after preheating, effectively reduce the energy loss in the process of hot ore transportation; effectively increase the temperature of pulverized coal, increase the layered and pore structure of the pulverized coal surface, and develop pulverization.
  • the specific surface area increases, the kinetic conditions of the smelting reduction reaction are improved, and the reaction rate of the molten pool is improved; the jet flow of the pulverized coal is improved, which is beneficial to pneumatic conveying;
  • the absorption rate of the powder in the molten iron pool further reduce the carry-out of the coal powder in the flue gas, and reduce the carbon content of the dust removal; at the same time, it is beneficial to reduce the coal consumption and improve the energy consumption index of the smelting reduction technology.
  • the above-mentioned composite injection method for iron-containing materials has high processing efficiency, short process and high comprehensive utilization rate of energy for iron-containing materials, which can reduce the coal consumption of the iron bath smelting reduction process to less than 850kg/t, and increase the thermal efficiency by 3-5%.
  • a composite injection system for iron-containing materials based on any one of the above-mentioned composite injection methods for iron-containing materials is provided, as shown in FIG. 2 , wherein:
  • the composite injection system includes the iron-containing material pretreatment subsystem 4 and the composite injection subsystem 6;
  • the iron-containing material pretreatment subsystem 4 includes a first-stage fluidization device 41, a second-stage fluidization device 42, a first cyclone separator 43, and a second cyclone separator 44.
  • the first-stage fluidization device 41 and the second-stage fluidization device 42 are arranged in series.
  • a second cyclone separator 44 is arranged between the second outlet 423 of the upper part of the second-stage fluidization device 42 and the first air inlet 411 of the first-stage fluidization device 41,
  • the first-stage fluidization device 41 adopts one of a circulating fluidization device, a bubbling fluidization device, and an annular fluidization device, and/or
  • the second-stage fluidization device 42 adopts a circulating fluidization device
  • the composite injection subsystem 6 includes a hot ore injection device 61, a pulverized coal/flux injection device 62, a composite injection pipeline 63, and a solid injection gun 64,
  • the hot ore injection device 61 is connected with the second-stage fluidization device 42, and the hot ore injection device 61 includes a hot ore injection tank 611, a first rotary feeder 612, and a first injection line 613 connected in sequence,
  • the pulverized coal/flux injection device 62 includes a pulverized coal injection device, a flux injection device, and a second injection pipeline 629,
  • the pulverized coal injection device and the flux injection device are jointly connected to the second injection pipeline 629,
  • the second injection line 629 merges with the first injection line 613 to form a composite injection line 63 , and the composite injection line 63 is connected to the solid lance 64 of the smelting reduction furnace 7 .
  • the iron-containing material enters the first-stage fluidization device 41 through the first feed port 412 at the bottom of the first-stage fluidization device 41 , and the first reducing gas passes through the first inlet at the bottom of the first-stage fluidization device 41 .
  • the port 411 enters the first-stage fluidization device 41, and the iron-containing material conducts convective heat exchange with the first reducing gas.
  • the iron-containing material and the first reducing gas are discharged through the first discharge port 413 in the upper part of the first-stage fluidization device 41 and enter the first cyclone separator 43 for gas-solid separation to obtain the iron-containing material after the first-stage preheating and pre-reduction treatment. and the first reduction waste gas, the first reduction waste gas is discharged through the exhaust port at the top of the first cyclone separator 43 and enters the reduction waste gas storage tank 5,
  • the temperature of the first reducing gas is 500°C-700°C, the CO content is 10%-20%, and the pre-reduction degree of the iron-containing material after the first-stage preheating and pre-reduction treatment is 0%-20%.
  • the temperature of the reduction exhaust gas is 150°C-250°C,
  • the reduction reactions occurring in the first-stage fluidization device 41 are: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 .
  • the iron-containing material after the first-stage preheating and pre-reduction treatment enters the second-stage fluidization device 42 through the second feed port 422 at the lower part of the second-stage fluidization device 42, and the second reducing gas passes through the second-stage fluidization device 42.
  • the second air inlet 421 at the bottom of the second-stage fluidization device 42 enters the second-stage fluidization device 42, and the iron-containing material after the first-stage preheating and pre-reduction treatment is subjected to convective heat exchange with the second reducing gas, and the second reducing gas
  • the iron-containing material after the first-stage preheating and pre-reduction treatment is subjected to the second-stage preheating and pre-reduction treatment,
  • the iron-containing material and the second reducing gas after the first-stage preheating and pre-reduction treatment are discharged through the second discharge port 423 at the upper part of the second-stage fluidization device 42 and enter the second cyclone separator 44 for gas-solid separation to obtain a second-stage fluidization device 44.
  • the iron-containing material and the second reduction waste gas after preheating and pre-reduction treatment are preheated.
  • the second reduction waste gas is circulated into the first-stage fluidization device 41 as the first reducing gas, and the iron-containing material after the second-stage preheating and pre-reduction treatment is passed through the second cyclone.
  • the discharge port at the bottom of the separator 44 is discharged to the pretreatment sealing tank 427 or circulated back to the second-stage fluidization device 42 through the return material 426,
  • the second reducing gas is the reformed gas of the smelting reduction furnace 7
  • the flow rate of the second reducing gas is 70000-120000Nm 3 /h
  • the flow velocity is 6m/s-10m/s
  • the temperature is 800-1000°C
  • the CO The content is more than 50% and the oxidation degree is less than 20%.
  • the temperature of the iron-containing material after the secondary preheating and prereduction treatment is 600°C-800°C
  • the pre-reduction degree is 40%-70%.
  • the reactions occurring in the second-stage fluidization device 42 are: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 , Fe 3 O 4 +CO ⁇ CO 2 +3FeO, and FeO+CO ⁇ CO 2 +Fe.
  • the composite blowing subsystem 6 further includes:
  • the flow regulating and pressure regulating valve is arranged in front of the junction of the first injection line 613 and the second injection line 629, and the flow regulating and pressure regulating valve is used to adjust the flow of the medium in the pipeline and carry out the pressure adjustment within the large pressure difference range. pressure regulation;
  • Pneumatic three-way ball valve ball valve group pneumatic three-way ball valve ball valve group is set at the junction of pipelines, consisting of a pneumatic actuator and a T-type pneumatic three-way ball valve.
  • the pneumatic actuator is used to receive control signals, synchronously drive and control the action of the three-way ball valve In the open and closed state, the T-type pneumatic three-way ball valve is used to control the confluence of the medium in the pipeline;
  • Pressure transmitter the pressure transmitter is arranged before the junction of the flow regulating and pressure regulating valve, the first injection line 613 and the second injection line 629, and the pressure transmitter is used to regulate the first injection line 613 and the second injection line 613.
  • the end of the composite injection line 63 is separated into a number of branch pipes 632, which are respectively connected to the solid lances 64 of the smelting reduction furnace 7;
  • the flow rate of the mixed material in the branch pipes 632; each branch pipe 632 is equipped with a gas supplement device for supplementing the carrier gas;
  • the number of solid spray guns 64 is at least two, and the solid spray gun is provided with anti-blocking parts to prevent slag iron from blocking solids Spray gun 64.
  • the iron-containing material pretreatment subsystem further includes:
  • the pretreatment sealing tank is connected with the second cyclone separator and the second-stage fluidization device;
  • Hot ore injection tank the hot ore injection tank is connected with the pretreatment sealing tank, the iron-containing material is transported between the pretreatment sealing tank and the hot ore injection tank by gravity, and between the pretreatment sealing tank and the hot ore injection tank It is equipped with a high temperature dome feed valve and a rotary exhaust valve, and a rotary discharge valve is also provided at the discharge port of the hot ore injection tank.
  • Embodiment 2 of the present application provides an iron-containing material composite injection system, which includes an iron-containing material pretreatment subsystem 4 and a composite injection subsystem 6 .
  • the iron-containing material pretreatment subsystem 4 includes a first-stage fluidization device 41, a second-stage fluidization device 42, a first cyclone 43, and a second cyclone 44;
  • the composite injection subsystem 6 includes a hot ore injection device 61.
  • the first-stage fluidization device 41 is connected to the second-stage fluidization device 42, and a first cyclone 43 and a second cyclone 44 are arranged between the first-stage fluidization device 41 and the second-stage fluidization device 42.
  • the second-stage fluidization device The device 42 is connected to the hot ore blowing tank 611 .
  • the first injection line 613 and the second injection line 629 merge to form a compound injection line 63 , and the compound injection line 63 is connected to the solid injection gun 64 .
  • first-stage fluidization device 41 By setting up a first-stage fluidization device 41, the iron-containing material is subjected to dehydration and drying treatment and a first-stage preheating and pre-reduction treatment, and a second-stage fluidization device 42 is installed to perform a second-stage preheating and pre-reduction treatment for the iron-containing material, which greatly improves the content of the iron-containing material.
  • Pre-reduction degree of iron material set the first injection line 613 to inject pre-reduced iron-containing material, and the second injection line 629 to inject pulverized coal and flux, so that the pre-reduced iron-containing material, coal powder and flux It is mixed in the composite injection line 63, so that a large amount of sensible heat carried by the iron-containing material after pre-reduction is efficiently utilized to preheat the pulverized coal.
  • the surface structure of the preheated pulverized coal changes significantly, and the layered and pore structure increases , the development of pulverization, the increase of the specific surface area, the looser pulverized coal, the improvement of the jet flow of the pulverized coal, the easy fluidization of the pulverized coal, and the benefit of pneumatic conveying; at the same time, the temperature of the pulverized coal entering the smelting reduction furnace 7 can be increased to Above 200 °C, the reaction conditions are optimized, the smelting efficiency of the molten pool is improved, the kinetic conditions of the reduction reaction are improved, the melting reaction of the pulverized coal in the smelting reduction furnace 7 is promoted, and the absorption rate of the pulverized coal in the smelting reduction furnace 7 is improved.
  • the first-stage fluidization device 41 adopts one of a circulating fluidization device, a bubbling fluidization device, and an annular fluidization device;
  • the second-stage fluidization device 42 adopts a circulating fluidization device.
  • the iron-containing material composite injection system also includes a grinding device and a conveying device that are connected in sequence. After the iron-containing material is crushed and ground by the grinding device, the iron-containing material is transported to the first-stage fluidization device 41 at a constant speed through the conveying device for processing. Dehydration and drying treatment and first-stage preheating and pre-reduction treatment.
  • the type of the grinding device is not limited, as long as it can realize the crushing treatment of iron-containing materials.
  • the grinding device is a ball mill 1, and the particle size of the iron-containing material after being crushed and ground by the ball mill 1 is less than 3 mm, so as to ensure that the iron-containing material can be fully reduced and melted.
  • the conveying device includes a belt conveyor 2 and a screw feeder 3, the belt conveyor 2 is used to control the constant speed conveying of iron-containing materials and the lifting of iron-containing materials, and the screw feeder 3 is used to control the iron-containing materials. Quantitative delivery.
  • the screw feeder 3 is a single screw feeder, and the feeding amount of the iron-containing material is controlled by controlling the rotation speed of the single screw feeder, wherein the feeding amount of the iron-containing material is 20-280t/ h, under this feeding amount, it can be ensured that the iron-containing material is fully pre-reduced in the first-stage fluidization device 41 and the second-stage fluidization device 42, and fully reduced in the subsequent smelting reduction furnace 7.
  • the discharge port of the ball mill 1 is connected with the feed chute at the bottom of the belt conveyor 2, the discharge chute at the upper part of the belt conveyor 2 is connected with the feed port of the screw feeder 3, and the discharge port of the screw feeder 3 It is connected with the first feed port 412 in the lower part of the first-stage fluidization device 41 .
  • a first cyclone separator 43 is disposed between the first-stage fluidization device 41 and the second-stage fluidization device 42. Specifically, the first outlet 413 of the first-stage fluidization device 41 and the second-stage fluidization device A first cyclone 43 is provided between the second feed ports 422 of 42 .
  • the iron-containing material enters the first-stage fluidization device 41 through the first feed port 412 at the bottom of the first-stage fluidization device 41, and the first reducing gas enters the first-stage fluidization device 41 through the air inlet at the bottom of the first-stage fluidization device 41.
  • Convective heat exchange with the first reducing gas is carried out, and the iron-containing material is subjected to dehydration and drying treatment and first-stage preheating and pre-reduction treatment under the action of high temperature and reducing atmosphere.
  • the iron-containing material and the first reducing gas pass through a first-stage fluidization device
  • the first discharge port 413 at the upper part of 41 is discharged and enters the first cyclone separator 43 for gas-solid separation to obtain the iron-containing material after the first-stage preheating and pre-reduction treatment and the first reduction waste gas.
  • the first reduction waste gas passes through the first cyclone.
  • the exhaust port at the top of the separator 43 is discharged and enters the reduction waste gas storage tank 5 .
  • the iron-containing material enters the first-stage fluidization device 41 through the first feed port 412 at the bottom of the first-stage fluidization device 41, and the first reducing gas enters the first-stage fluidization device through the first air inlet 411 at the bottom of the first-stage fluidization device 41.
  • the first reducing gas not only suspends the particles of the iron-containing material and realizes effective contact between the gas and the solid, but can also undergo a reduction reaction with the iron-containing material at the same time.
  • the bottom is in a state of turbulent flow, which greatly increases the mass transfer and heat transfer efficiency between the first reducing gas and the iron-containing material. more than 10 times.
  • the temperature of the first reducing gas is 500°C-700°C, and the CO content is 10%-20%; the reduction reaction in the first-stage fluidization device 41 is: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 ; the pre-reduction degree of the iron-containing material after the first-stage preheating and pre-reduction treatment is 0%-20%, and the temperature of the first reduction waste gas is 150°C-250°C.
  • the iron-containing material and the first reducing gas conduct convective heat exchange, and the crystal water in the iron-containing material is completely removed under the high temperature of the first reducing gas, and is reduced with the first reducing gas.
  • part of Fe 2 O 3 is reduced to Fe 3 O 4 , and the pre-reduction degree is 0-20%;
  • the iron-containing material after the reaction is discharged together with the first reducing gas through the first outlet 413 in the upper part of the first-stage fluidization device 41 , and enter the first cyclone separator 43, in the first cyclone separator 43, the reacted iron-containing material and the first reducing gas undergo gas-solid separation to obtain the iron-containing material after the first-stage preheating and pre-reduction treatment and
  • the first reduction waste gas the temperature of the first reduction waste gas is 150°C-250°C; the iron-containing material after the first-stage preheating and pre-reduction treatment is discharged through the discharge port at the bottom of the first cyclone separat
  • the iron-containing material is transported by gravity from the discharge port of the first cyclone separator 43 to the feed port of the second-stage fluidization device 42; preferably, in order to prevent the second reducing gas in the second-stage fluidization device 42 from leaking into the
  • the first cyclone separator 43 is provided with a mechanical butterfly valve between the first cyclone separator 43 and the second-stage fluidization device 42 .
  • thermocouples are provided at the bottom and the top of the first-stage fluidization device 41 to detect the temperature of the first reducing gas entering and exiting the first-stage fluidization device 41, so as to obtain the iron-containing material after the first-stage preheating and pre-reduction treatment.
  • the temperature of the first reducing gas can be adjusted to regulate the feeding amount of the first reducing gas or the feeding amount of the iron-containing material.
  • the operating pressure of the first-stage fluidization device 41 is 70-90 kPa, preferably 80 kPa.
  • a second cyclone separator 44 is arranged between the second-stage fluidization device 42 and the first-stage fluidization device 41 .
  • a second cyclone 44 is provided between the first air inlets 411 of the device 41 .
  • the iron-containing material enters the second-stage fluidization device 42 through the second feed port 422 at the bottom of the second-stage fluidization device 42
  • the second reducing gas enters the second-stage flow through the first air inlet 421 at the bottom of the second-stage fluidization device 42 .
  • the iron-containing material and the second reducing gas conduct convection heat exchange, and the iron-containing material is subjected to secondary preheating and pre-reduction treatment; the iron-containing material and the second reducing gas pass through the second-stage fluidization device
  • the second discharge port 423 discharges and enters the second cyclone separator 44 for gas-solid separation to obtain the iron-containing material after the secondary preheating and prereduction treatment and the second reduction waste gas.
  • the iron-containing material enters the second-stage fluidization device 42 through the second inlet port 422 at the bottom of the second-stage fluidization device 42
  • the second reducing gas enters the second-stage fluidization device 42 through the second inlet port 421 at the bottom of the second-stage fluidization device 42.
  • the second reducing gas not only suspends the particles of the iron-containing material, realizes effective contact between the gas and the solid, but can also have a reduction reaction with the iron-containing material at the same time.
  • the bottom of the fluidization device 42 is in a turbulent state, which greatly increases the mass transfer and heat transfer efficiency between the second reducing gas and the iron-containing material, and the heat transfer coefficient is 350-1660W/(m 2 ⁇ K), which is
  • the stacking state reaction is more than 10 times, which greatly shortens the time of the secondary preheating and prereduction reaction.
  • the flow rate of the second reducing gas is 70000-120000Nm 3 /h, the flow rate is 6m/s-10m/s, the temperature is 800-1000°C, the CO content is more than 50%, and the oxidation degree is not more than 20%.
  • the second reducing gas is the reformed gas of the smelting reduction furnace 7; the second reducing waste gas enters the first-stage fluidization device 41 as the first reducing gas; the reaction of the second-stage preheating and pre-reduction treatment is: 3Fe 2 O 3 +CO ⁇ CO 2 +2Fe 3 O 4 , Fe 3 O 4 +CO ⁇ CO 2 +3FeO, FeO+CO ⁇ CO 2 +Fe; the temperature of the iron-containing material after the secondary preheating and prereduction treatment is 600°C-800°C, The degree of reduction is 40%-70%.
  • the iron-containing material conducts convective heat exchange with the second reducing gas, and undergoes a reduction reaction with the second reducing gas, and the reacted iron-containing material and the second reducing gas pass through the second outlet in the upper part of the second-stage fluidization device 42 together.
  • the material is discharged from the material port 422 and enters the second cyclone separator 44; in the second cyclone separator 44, the iron-containing material and the second reducing gas undergo gas-solid separation, and the iron-containing material after the secondary preheating and pre-reduction treatment
  • the discharge port at the bottom of the second cyclone separator 44 is discharged, and the second reduction waste gas is discharged through the exhaust port at the top of the second cyclone separator 44 , and passes through the first intake air at the bottom of the first-stage fluidization device 41 as the first reducing gas.
  • Port 411 enters one stage of fluidization device 41 .
  • the upper part of the smelting reduction furnace 7 is communicated with the reformed gas transmission pipe 82 through the vaporization flue 81, and the reformed gas transmission pipe 82 is communicated with the second air inlet 421 at the bottom of the second-stage fluidization device 42, so as to
  • the upgraded gas of the smelting reduction furnace 7 is used as the second reducing gas to perform secondary preheating and pre-reduction treatment on the iron-containing material in the second-stage fluidization device 42 .
  • connection position of the vaporizing flue 81 and the reformed gas transmission pipeline 82 is 5-10 m away from the upper end of the vaporizing flue 81 .
  • the reformed gas transmission pipeline 82 is provided with a flow regulating valve and a flow meter, so as to adjust the reformed gas transmission flow in the reformed gas transmission pipeline 82 according to the value of the flow meter, so as to maintain a constant reformed gas transmission flow.
  • a flow regulating and pressure regulating valve is provided at one end of the reformed gas transmission pipeline 82 close to the second-stage fluidization device 42, which is used to precisely control the flow of the reformed gas and ensure that the reformed gas enters the second-stage fluidization device at a constant flow rate. 42.
  • it can also realize the adjustment within the working pressure difference range of 1MPa, and keep the pressure after the flow regulating and pressure regulating valve stable.
  • the inner surface of the modified gas transmission pipeline 82 is built with refractory bricks.
  • the transport flow of the modified gas transmission pipeline 82 accounts for 30-50% of the gas flow generated by the smelting reduction furnace 7, and the rest of the modified gas enters the waste heat power generation system 9 through the vaporization flue 81 to generate electricity, and is converted into power resources for use.
  • the iron-containing material after the secondary preheating and pre-reduction treatment is discharged through the discharge port at the bottom of the second cyclone 44 and passed through the return material 426, and is recycled from the return material 426 through the circulating material inlet 425. to the second-stage fluidization device 42 .
  • the reverter 426 has a U-shaped structure. By arranging the returner 426 , the iron-containing material in the second-stage fluidization device 42 can be circulated and returned, and a gas seal can be provided to prevent the gas from flowing back into the second-stage fluidization device 42 .
  • the bottom of the returner 426 is provided with a circulating air cap.
  • the circulating fluidizing gas is sprayed on the returner 426 to fluidize the iron-containing material in the returner 426, and the iron-containing material is removed from the return material.
  • the device 426 is sent back to the second-stage fluidization device 42, so as to realize the circulating fluidized secondary preheating and pre-reduction treatment of iron-containing materials.
  • the circulating fluidizing gas injected at the bottom of the returner 426 may be one or more of reformed coal gas, the first reducing waste gas or the inert gas, and the flow rate of the circulating fluidizing gas accounts for 5% of the flow rate of the second reducing gas. -10%, preferably, the flow rate of the circulating fluidizing gas is 5000-20000 Nm 3 /h.
  • the lower part of the second-stage fluidization device 42 is provided with a third discharge port 424 , the third discharge port 424 is connected with the pretreatment sealing tank 427 , and the pretreatment sealing tank 427 is connected with the hot ore injection device 61 . .
  • the pretreatment sealed tank 427 By setting the pretreatment sealed tank 427, the iron-containing material after the secondary preheating and prereduction treatment can be temporarily stored, wherein the temperature of the iron-containing material after the secondary preheating and prereduction treatment is 600-800°C, and the prereduction degree is 40%-70%.
  • combustion-supporting air can also be introduced into the second-stage fluidization device 42 to generate a large amount of heat through the combustion reaction of CO and H2 to increase the temperature of the second reducing gas, thereby increasing the reduction in the second-stage fluidization device 42.
  • temperature further, the combustion-supporting air can use the oxygen-enriched hot air produced by the hot blast stove, the oxygen-enriched content is 30-40%, and the hot air flow rate is controlled at 0-5000Nm 3 /h.
  • thermocouples are provided at the bottom and the top of the second-stage fluidization device 42 to detect the temperature of the second reducing gas when entering and exiting the second-stage fluidization device 42, so as to obtain the preheating and pre-reduction treatment of the secondary
  • the temperature of the iron material is used to control the amount of the second reducing gas or the amount of iron-containing material to be discharged.
  • the operating pressure of the second-stage fluidization device 42 is 70-90 kPa, preferably 80 kPa.
  • reaction time of the iron-containing material in the second-stage fluidization device 42 is within 10 minutes.
  • the iron-containing material composite injection system further includes: a flow regulating and pressure regulating valve, a pneumatic three-way ball valve group and a pressure transmitter.
  • the flow regulating and pressure regulating valve is arranged in front of the junction of the first injection line 613 and the second injection line 629.
  • the flow regulating and pressure regulating valve is used to adjust the flow of the medium in the pipeline and to adjust the pressure within a large pressure difference range;
  • the ball valve group is set at the junction of the pipeline and consists of a pneumatic actuator and a T-type pneumatic three-way ball valve.
  • the pneumatic actuator is used to receive control signals, synchronously drive and control the action and opening and closing status of the three-way ball valve.
  • the T-type pneumatic three-way ball valve The ball valve is used to control the confluence of the medium in the pipeline; the pressure transmitter is arranged in front of the confluence of the flow regulating and pressure regulating valve, the first injection line 613 and the second injection line 629, and the pressure transmitter is used to regulate the first injection The injection pressure of the carrier gas in the line 613 and the second injection line 629.
  • the flow of the first injection line 613 and the second injection line 629 are respectively controlled to maintain a constant flow, and at the same time, the Ensure that the pressure of the first injection line 613 and the second injection line 629 is close when they meet, and ensure that the iron-containing material in the first injection line 613 and the pulverized coal and flux in the second injection line 629 can smoothly enter the composite injection Blow line 63 for mixing.
  • the first injection line 613 and the second injection line 629 are respectively provided with flow regulating and pressure regulating valves.
  • the flow regulating and pressure regulating valves are respectively arranged at a distance of 2.5-3.5m from the confluence, preferably at a distance of 3m.
  • the first injection line 613 and the second injection line 629 are respectively provided with pressure transmitters, and the pressure transmitters are respectively disposed at positions 1-2m away from the confluence.
  • the end of the composite injection line 63 is separated into several branch pipes 632, which are respectively connected to the solid spray guns 64 of the smelting reduction furnace 7; a distributor is provided at the separation place to control the flow rate of the mixed material in each branch pipe 632;
  • the branch pipe 632 is provided with an air supply device for supplementing the carrier gas;
  • the number of solid spray guns 64 is at least two, and the solid spray gun 64 is provided with an anti-blocking member to prevent the solid spray gun 64 from being blocked by slag iron.
  • the composite injection line 63 is separated into several branch pipes 632 .
  • the length of the composite injection line 63 is 50-60 m
  • the conveying speed of the mixed material in the composite injection line 63 is 15-25 m/s
  • the mixed material enters the composite injection line 63 and is conveyed to the inlet of the solid spray gun 64
  • the time is not less than 3s to ensure that the iron-containing material, the pulverized coal and the flux are fully mixed in the composite injection line 63 .
  • the pretreatment sealing tank 427 is directly connected to the hot ore injection tank 611, the iron-containing material is transported by gravity, and a high temperature dome feeding valve and a rotary exhaust valve are arranged between the hot ore injection tank.
  • the 611 discharge port is equipped with a rotary discharge valve.
  • a high temperature dome feeding valve and a rotary exhaust valve are arranged between the pretreatment sealing tank 427 and the hot ore injection tank 611, so that the hot ore injection tank 611 can be decompressed and exhausted before feeding, so as to prevent iron-containing materials Particle leakage ensures the reliable sealing of the hot mineral injection tank 611.
  • a rotary discharge valve is provided at the discharge port of the hot ore injection tank 611 .
  • two parallel first rotary feeders 612 are connected to the outlet of the hot ore injection tank 611 , and the iron-containing material after the secondary preheating and pre-reduction treatment is conveyed by the two first rotary feeders 612 to the first injection line 613; the pulverized coal passes through the pulverized coal storage tank 621, the pulverized coal intermediate tank 622 and the pulverized coal injection tank 623 in sequence, and then is transported to the second injection line 629 through the second rotary feeder 628, After the flux passes through the flux batching bin 624 , the flux storage tank 625 , the flux intermediate tank 626 and the flux injection tank 627 in sequence, it is transported to the second injection line 629 through the second rotary feeder 628 .
  • the iron-containing material in the first injection line 613 and the pulverized coal and flux in the second injection line 629 are pre-mixed in the composite injection line 63 to form a mixed material, and the iron-containing material that has been preheated and pre-reduced is brought into the mixture.
  • the sensible heat is used to preheat the pulverized coal and the flux, and the mixed material is mixed and injected into the smelting reduction furnace 7 through the solid spray gun 64 .
  • a second rotary feeder 628 By setting two parallel first rotary feeders 612 in the hot ore injection tank 611, a second rotary feeder 628 after the pulverized coal injection tank 623 and the flux injection tank 627, respectively, to control each injection
  • the feeding amount of the tank and accurately control the ratio between iron-containing materials, pulverized coal, and flux, and control the injection precision.
  • the proportion of the powder is 40%-50% of the iron-containing material, and the proportion of the flux is 13%-17% of the iron-containing material.
  • the reduction waste gas storage tank 5 is communicated with the first injection line 613 , the second injection line 629 and the composite injection line 63 respectively.
  • the injection carrier gas of the injection line 63 is the first reduction waste gas of the first-stage fluidization device 41 .
  • This setting method can realize the recycling and reuse of the first reduction waste gas and the waste gas, and improve the utilization rate of the energy of the system; and reduce the heat loss of the iron-containing material after preheating; reduce the amount of nitrogen entering the furnace in the system, thereby reducing the The formation of nitrogen oxides in the flue gas; in addition, the CO2 carried in the injection carrier gas easily reacts with the pulverized coal to generate CO, thereby increasing the reducing atmosphere and improving the kinetic conditions of the smelting reduction furnace 7.
  • the flow rate of the injection carrier gas in the first injection line 613 is 0-15000Nm 3 /h; the flow rate of the injection carrier gas in the second injection line 629 is 0-8000Nm 3 /h; the first injection line
  • the injection pressures of the carrier gas in 613 , the second injection line 629 and the composite injection line 63 are all 100-500 kPa.
  • the first injection line 613 , the second injection line 629 and the injection carrier gas lines of the composite injection line 63 are all provided with flow control valves for controlling the first injection line 613 , the second injection line 613 and the second injection line 63 .
  • the iron-containing material pretreatment subsystem has a small solid-gas ratio, fast heat transfer and mass transfer rate, and can effectively improve the pre-reduction degree and the limit value of the pre-heating temperature of the iron-containing material; two-stage preheating pretreatment can realize energy classification Utilize, in limited reaction time, improve the utilization rate of energy.
  • the iron-containing material undergoes the above-mentioned two-stage preheating and pre-reduction treatment, which is beneficial to improve the rate of the smelting reduction reaction; at the same time, it is beneficial to further increase the production capacity, reduce the coal consumption, and improve the energy consumption index of the smelting reduction technology.
  • the above-mentioned composite injection subsystem can efficiently utilize a large amount of sensible heat carried by the iron-containing material after preheating, effectively reducing the energy loss in the process of hot ore conveying; development, the specific surface area increases, the kinetic conditions of the smelting reduction reaction are improved, and the reaction rate of the molten pool is improved; the jet flow of pulverized coal is improved, which is beneficial to pneumatic conveying; The absorption rate of pulverized coal in the molten iron pool; further reduce the carry-out of pulverized coal particles in the flue gas, and reduce the carbon content of dust removal; at the same time, it is beneficial to reduce coal consumption and improve the energy consumption index of smelting reduction technology.
  • the above iron-containing material composite injection system has high processing efficiency, short process and high comprehensive energy utilization rate for iron-containing materials, which can reduce the coal consumption of the iron bath smelting reduction process to below 850kg/t, and increase the thermal efficiency by 3-5%.
  • the terms “installed”, “connected”, “connected”, “fixed” and other terms should be understood in a broad sense, for example, it may be a fixed connection or a detachable connection , or integrated; it can be a mechanical connection, an electrical connection, or a communication; it can be a direct connection or an indirect connection through an intermediate medium, and it can be the internal connection of the two elements or the interaction between the two elements. .
  • installed may be a fixed connection or a detachable connection , or integrated; it can be a mechanical connection, an electrical connection, or a communication; it can be a direct connection or an indirect connection through an intermediate medium, and it can be the internal connection of the two elements or the interaction between the two elements.

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Abstract

一种含铁物料复合喷吹方法及系统，其中方法包括下述步骤：(i)将含铁物料破碎研磨后，对含铁物料进行脱水干燥处理及一级预热预还原处理；(ii)将一级预热预还原处理后的含铁物料进行二级预热预还原处理；(iii)将煤粉、熔剂与二级预热预还原处理后的含铁物料在喷吹入熔融还原炉（7）之前在喷吹管线内进行预混合，以使含铁物料携带的显热对煤粉和熔剂进行预热；(iv)将预混合后的混合物料喷吹入熔融还原炉（7）。本方法对含铁物料的处理效率高、流程短、能源综合利用率高，可降低铁浴熔融还原工艺的煤耗至850kg/t以下，使热效率增加3-5％。

Description

一种含铁物料复合喷吹方法及系统
本申请要求于2021年4月27日提交中国专利局、申请号为202110460161.9、发明名称为"一种含铁物料预处理及复合喷吹方法及系统"的中国专利申请的优先权,其全部内容通过引用结合在本申请中。
技术领域
本申请涉及熔融还原工艺原燃料预处理技术领域，尤其涉及一种含铁物料复合喷吹方法及系统。
背景技术
铁浴熔融还原工艺是利用非焦煤煤粉和铁矿粉的熔融还原冶金工艺，在高温熔融状态下用碳把铁氧化物还原成金属铁的冶炼方法，具有原料适应性强、工艺流程短、对环境污染小、铁水质量好等优点，是解决我国焦煤资源贫乏和环保问题的先进炼铁技术。
熔融还原生产工艺目前以“两步法”为主，即“预还原”+“终还原”流程。运用在铁浴熔融还原工艺上的流化床技术利用熔融还原炉产生的高温煤气对矿粉进行预热，但传统的流化床工艺直接利用熔融还原炉产生的煤气，煤气氧化度高，质量差，还原能力差，且只经一级循环流化床预还原，造成含铁物料的预还原效果差，预还原度低于20％。
同时，传统的铁浴熔融还原工艺中煤粉和矿粉采用两条不同的输送管线进行输送，连接不同的固体喷枪喷吹进入熔融还原炉，进入熔融还原炉后煤粉和矿粉的混合效果差，煤粉的入炉温度低，表面活性低，严重影响了熔融还原反应的传热及传质反应速率。煤粉需要先吸收大量热量达到反应温度，熔融还原反应才得以进行，反应时间延长，且反应不够充分，部分物料颗粒会随上升煤气带出炉外，造成了物料的浪费。原燃料的预处理阶段成为整个熔融还原流程的限制性环节。
因此，目前需要研发出一种新型的含铁物料预处理及复合喷吹方法及系统，以克服和改善上述现有技术中的一个或多个缺点，或者至少提出一种有效的可选方法来解决上述问题。
发明内容
根据本申请的各种实施例，本申请提供了一种含铁物料复合喷吹方法及系统。本申请提供的含铁物料复合喷吹方法及系统，能够提高对含铁物料的预热温度、提高含铁物料的预还原度，含铁物料在输送管线中与煤粉及熔剂进行预混合，高效利用了预热后含铁物料携带的大量显热对煤粉及熔剂进行预热，提高了煤粉进入熔融还原炉的温度，优化了熔池的反应条件，提高了熔池的反应速率，有效地提高了熔融还原工艺的生产能力，提高了能量的综合利用效率，有利于降低煤耗，提高熔融还原技术的能耗指标。
根据本申请的一个方面，提供了一种含铁物料复合喷吹方法，其中，包括下述步骤：
(1)将含铁物料破碎研磨后，对所述含铁物料进行脱水干燥处理及一级预热预 还原处理，所述一级预热预还原处理的第一还原性气体的温度为500-700℃，CO含量为10-20％；
(2)将一级预热预还原处理后的含铁物料进行二级预热预还原处理，所述二级预热预还原处理的第二还原性气体为改质煤气，温度为800-1000℃，CO含量至少50％，氧化度不超过20％；
(3)将煤粉、熔剂与二级预热预还原处理后的含铁物料在喷吹入熔融还原炉之前在喷吹管线内进行预混合，以使所述含铁物料携带的显热对煤粉和熔剂进行预热；
(4)将预混合后的混合物料喷吹入熔融还原炉，其中，含铁物料喷吹载气、煤粉及熔剂喷吹载气、混合物料喷吹载气均为所述一级预热预还原处理的第一还原废气。
在含铁物料复合喷吹方法的一种优选的实施方式中，所述对所述含铁物料进行脱水干燥处理及一级预热预还原处理包括：
所述含铁物料经一段流化装置下部的第一进料口进入一段流化装置，第一还原性气体经一段流化装置底部的第一进气口进入一段流化装置，所述含铁物料与所述第一还原性气体进行对流换热，所述第一还原性气体对所述含铁物料进行脱水干燥处理及一级预热预还原处理，
所述含铁物料与所述第一还原性气体经一段流化装置上部的第一出料口排出并进入第一旋风分离器进行气固分离，得到一级预热预还原处理后的含铁物料和第一还原废气，所述第一还原废气经第一旋风分离器顶部的排气口排出并进入还原废气储罐，
所述一级预热预还原处理后的含铁物料的预还原度为0％-20％，所述第一还原废气的温度为150℃-250℃，
一段流化装置内发生的还原反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4。
在含铁物料复合喷吹方法的一种优选的实施方式中，所述将一级预热预还原处理后的含铁物料进行二级预热预还原处理包括：
所述一级预热预还原处理后的含铁物料经二段流化装置下部的第二进料口进入二段流化装置，第二还原性气体经二段流化装置底部的第二进气口进入二段流化装置，所述一级预热预还原处理后的含铁物料与所述第二还原性气体进行对流换热，所述第二还原性气体对所述一级预热预还原处理后的含铁物料进行二级预热预还原处理，
所述一级预热预还原处理后的含铁物料与所述第二还原性气体经二段流化装置上部的第二出料口排出并进入第二旋风分离器进行气固分离，得到二级预热预还原处理后的含铁物料和第二还原废气，所述第二还原废气作为第一还原性气体循环进入一段流化装置，所述二级预热预还原处理后的含铁物料经第二旋风分离器底部出料口排出至预处理密封罐或经返料器循环回到二段流化装置，
所述二级预热预还原处理后的含铁物料的温度为600℃-800℃，预还原度为40％-70％，
二段流化装置内发生的反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4，Fe 3O 4+CO→CO 2+3FeO，FeO+CO→CO 2+Fe。
在含铁物料复合喷吹方法的一种优选的实施方式中，步骤(1)中所述含铁物料为铁精粉、赤铁矿粉、褐铁矿粉、菱铁矿粉、赤泥等工业固体废物、氧化铁皮中的一种或多种，所述含铁物料中铁含量不低于30％；破碎研磨后的所述含铁物料的粒度小于3mm；所述含铁物料的喷吹量为20～280t/h。
在含铁物料复合喷吹方法的一种优选的实施方式中，步骤(3)中所述煤粉的配加比例为所述含铁物料的40％-50％，
所述煤粉为喷吹煤、烟煤、半焦、兰炭、泥煤中的一种或多种，所述煤粉的碳含量大于70％，粒度小于5mm；和/或
步骤(3)中所述熔剂的配加比例为所述含铁物料的13％-17％，
所述熔剂为碱性熔剂，所述熔剂为白云石与石灰的混合物，
其中，所述白云石中氧化镁的含量不低于17％，所述白云石的粒度小于10mm，
所述石灰中氧化钙的含量不低于70％，所述石灰的粒度小于3mm，
所述白云石与所述石灰的配加比例由炉渣的二元碱度与四元碱度确定，所述石灰与所述白云石的配加比例为：
石灰：白云石＝1：1.2(2R 4-R 2)～1:2.5(2R 4-R 2)，
其中，R 2＝CaO/SiO 2，R 4＝(CaO+MgO)/(SiO 2+Al 2O 3)。
在含铁物料复合喷吹方法的一种优选的实施方式中，步骤(4)中所述含铁物料喷吹载气的载气流量为0-15000Nm 3/h，喷吹压力为100-500kPa；和/或
步骤(4)中所述煤粉及熔剂喷吹载气的载气流量为0-8000Nm 3/h，喷吹压力为100-500kPa；和/或
步骤(4)中所述混合物料喷吹载气的喷吹压力为100-500kPa。
根据本申请的另一个方面，提供了一种基于上述任一项所述的含铁物料复合喷吹方法的含铁物料复合喷吹系统，其中：
所述系统包括含铁物料预处理子系统及复合喷吹子系统；
所述含铁物料预处理子系统包括一段流化装置、二段流化装置、第一旋风分离器、第二旋风分离器，
所述一段流化装置与所述二段流化装置串联设置，所述一段流化装置的第一出料口与所述二段流化装置的第二进料口之间设置有所述第一旋风分离器，所述二段流化装置的第二出料口与所述一段流化装置的第一进气口之间设置有所述第二旋风分离器，
所述一段流化装置采用循环流化装置、鼓泡流化装置、环形流化装置其中的一种，和/或
所述二段流化装置采用循环流化装置；
所述复合喷吹子系统包括热矿喷吹装置、煤粉/熔剂喷吹装置、复合喷吹管线、固体喷枪，
所述热矿喷吹装置与所述二段流化装置连接，所述热矿喷吹装置包括依次连接的热矿喷吹罐、旋转给料机、第一喷吹管线，
所述煤粉/熔剂喷吹装置包括煤粉喷吹装置、熔剂喷吹装置、第二喷吹管线，
所述煤粉喷吹装置与熔剂喷吹装置共同连接至所述第二喷吹管线，
所述第二喷吹管线与所述第一喷吹管线汇合构成所述复合喷吹管线，所述复合喷吹管线与熔融还原炉的所述固体喷枪连接。
在含铁物料复合喷吹系统的一种优选的实施方式中，所述复合喷吹子系统还包括：
调流调压阀，所述调流调压阀设置于所述第一喷吹管线与所述第二喷吹管线汇合处前方，所述调流调压阀用以调节管线内介质流量及进行大压差范围内的压力调节；
气动三通球阀球阀组，所述气动三通球阀球阀组设置于管线汇合处，由气动执行机构和T型气动三通球阀组成，所述气动执行机构用于接收控制信号，同步驱动和控制三通球阀的动作和开闭状态，所述T型气动三通球阀用于控制管路中介质的合流；
压力变送器，所述压力变送器设置于所述调流调压阀与所述第一喷吹管线与所述第二喷吹管线汇合处之前，所述压力变送器用以调控所述第一喷吹管线与所述第二喷吹管线内载气的喷吹压力。
在含铁物料复合喷吹系统的一种优选的实施方式中，所述复合喷吹管线末端分离为若干支管，分别连接至熔融还原炉各个固体喷枪；分离处设置有分配器，用于控制各支管的混合物料的流量；各支管安装有补气装置，用于进行载气补充；固体喷枪的数量至少为两个，所述固态喷枪上设有防堵件，用于防止渣铁堵塞所述固体喷枪。
在含铁物料复合喷吹系统的一种优选的实施方式中，所述含铁物料预处理子系统还包括：
预处理密封罐，所述预处理密封罐与所述第二旋风分离器及所述二段流化装置连接；
热矿喷吹罐，所述热矿喷吹罐与所述预处理密封罐连接，含铁物料依靠重力在所述预处理密封罐与所述热矿喷吹罐之间输送，所述预处理密封罐与所述热矿喷吹罐之间设有高温圆顶进料阀与旋转式排气阀，所述热矿喷吹罐出料口还设置有旋转卸料阀。
通过本申请实施例技术方案，可以达到以下有益效果：
(1)本申请所提供的含铁物料复合喷吹的方法，通过设置一段流化装置和二段流化装置，对含铁物料进行二级预热预还原反应，大大提高了含铁物料的预还原度，对第一还原性气体和第二还原性气体的循环利用程度高，能量利用率高，二级预热预还原处理后的含铁物料的温度达到600℃-800℃，预还原度达到40％-70％。
(2)本申请所提供的含铁物料复合喷吹的方法，通过设置第一喷吹管线喷吹预还原后的含铁物料，第二喷吹管线喷吹煤粉和熔剂，含铁物料和煤粉、熔剂在复合喷吹管线中预混合，从而高效利用了预还原后含铁物料携带的大量显热，对煤粉进行预热，预热后的煤粉表面结构发生明显变化，层状和孔隙结构增加，粉末化发展，比表面积增加，煤粉更加疏松，改善了煤粉的喷流性，使煤粉易于被流化，有利于气力输送；同时，还可以提高煤粉进入熔融还原炉的温度，使其达到200℃以上，优化了熔融还原炉内的反应条件，提高了熔池冶炼效率，改善了还原反应的动力学条 件，促进煤粉在熔融还原炉中熔融反应的前移，使煤粉在熔融还原炉中的吸收率提高10％以上，降低了烟气中煤粉颗粒的带出量，使除尘灰的含碳量降低20％以上；此外，还可以使含铁物料、煤粉及熔剂在输送过程中进行充分混合，提高了混合均匀度，有利于物料在熔融还原炉中充分反应，减少了物料损失。
(3)本申请所提供的含铁物料复合喷吹的方法，将二段流化装置排出的第二还原废气循环输送至一段流化装置，在一段流化装置中作为第一还原性气体对含铁物料进行脱水干燥处理及一级预热预还原处理，提高了气体的循环利用程度及能量利用率。
(4)本申请所提供的含铁物料复合喷吹的方法，将熔融还原炉中产生的煤气经改质处理后，得到的改质煤气作为第二还原性气体，为二段流化装置提供了还原性气体，大大提高了含铁物料的预还原度。
附图说明
图1用以说明本申请中一个或多个实施例中的含铁物料复合喷吹方法的一种流程示意图；
图2用以说明本申请中一个或多个实施例中的含铁物料复合喷吹系统的一种结构示意图。
附图标记：
1、球磨机；2、皮带输送机；3、螺旋给料机；4、含铁物料预处理子系统；5、还原废气储罐；6、复合喷吹子系统；7、熔融还原炉；8、煤气处理系统；9、余热发电系统；41、一段流化装置；42、二段流化装置；43、第一旋风分离器；44、第二旋风分离器；411、第一进气口；412、第一进料口；413、第一出料口；421、第二进气口；422、第二进料口；423、第二出料口；424第三出料口；425、循环料入口；426、返料器；427、预处理密封罐；61、热矿喷吹装置；62、煤粉/熔剂喷吹装置；63、复合喷吹管线；64、固体喷枪；611、热矿喷吹罐；612、第一旋转给料机；613、第一喷吹管线；621、煤粉储料罐；622、煤粉中间罐；623、煤粉喷吹罐；624、熔剂配料仓；625、熔剂储料罐；626、熔剂中间罐；627、熔剂喷吹罐；628、第二旋转给料机；629、第二喷吹管线；632、支管；81、汽化烟道；82、改质煤气输送管道。
实施方式
在下文中，仅简单地描述了某些示例性实施例。正如本领域技术人员可认识到的那样，在不脱离本申请的精神和范围的情况下，可通过各种不同方式修改所描述的实施例。因此，附图和描述被认为本质上是示例性的而非限制性的。
首先，对本申请所揭示的技术方案的技术构思进行说明。现有的熔融还原生产工艺直接利用熔融还原炉产生的煤气，使煤气的氧化度高、质量差、还原能力差，且只经一级循环流化床预还原，造成含铁物料的预还原效果差，预还原度低于20％。同时，传统的铁浴熔融还原生产工艺中，煤粉和含铁物料采用两条不同的输送管线进行输送，使煤粉和含铁物料的混合效果差，煤粉入炉温度低、表面活性低，严重影响了熔融还原反应的传热及传质反应速率。因此，原燃料的预处理阶段成为现有的熔融还原工艺的限制性环节。
考虑到现有技术存在的上述问题，本申请提供了一种新型的含铁物料复合喷吹方法及系统。下面结合说明书附图，对本申请进行说明。
具体采取的方案是：
根据本申请的一个方面，提供了一种含铁物料复合喷吹方法，如图1所示，所述方法包括下述步骤：
(1)将含铁物料破碎研磨后，对含铁物料进行脱水干燥处理及一级预热预还原处理，一级预热预还原处理的第一还原性气体的温度为500-700℃，CO含量为10-20％；
(2)将一级预热预还原处理后的含铁物料进行二级预热预还原处理，二级预热预还原处理的第二还原性气体为改质煤气，还原温度为800-1000℃，CO含量至少50％，氧化度不超过20％；
(3)将煤粉、熔剂与二级预热预还原处理后的含铁物料在喷吹入熔融还原炉之前在喷吹管线内进行预混合，以使含铁物料携带的显热对煤粉和熔剂进行预热；
(4)将预混合后的混合物料喷吹入熔融还原炉，其中，含铁物料喷吹载气、煤粉及熔剂喷吹载气、混合物料喷吹载气均为一级预热预还原处理的第一还原废气。
在一种优选的实施方式中，对含铁物料进行脱水干燥处理及一级预热预还原处理包括：
含铁物料经一段流化装置41下部的第一进料口412进入一段流化装置41，第一还原性气体经一段流化装置41底部的第一进气口411进入一段流化装置41，含铁物料与第一还原性气体进行对流换热，第一还原性气体对含铁物料进行脱水干燥处理及一级预热预还原处理，
含铁物料与第一还原性气体经一段流化装置41上部的第一出料口413排出并进入第一旋风分离器43进行气固分离，得到一级预热预还原处理后的含铁物料和第一还原废气，第一还原废气经第一旋风分离器43顶部的排气口排出并进入还原废气储罐5，
一级预热预还原处理后的含铁物料的预还原度为0％-20％，第一还原废气的温度为150℃-250℃，
一段流化装置41内发生的还原反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4。
在一种优选的实施方式中，将一级预热预还原处理后的含铁物料进行二级预热预还原处理包括：
一级预热预还原处理后的含铁物料经二段流化装置42下部的第二进料口422进入二段流化装置，第二还原性气体经二段流化装置42底部的第二进气口421进入二段流化装置42，一级预热预还原处理后的含铁物料与第二还原性气体进行对流换热，第二还原性气体对一级预热预还原处理后的含铁物料进行二级预热预还原处理，
一级预热预还原处理后的含铁物料与第二还原性气体经二段流化装置42上部的第二出料口423排出并进入第二旋风分离器44进行气固分离，得到二级预热预还原处理后的含铁物料和第二还原废气，第二还原废气作为第一还原性气体循环进入一段流化装置41，二级预热预还原处理后的含铁物料经第二旋风分离器44底部出料口排出至预处理密封罐427或经返料器426循环回到二段流化装置42，
二级预热预还原处理后的含铁物料的温度为600℃-800℃，预还原度为40％-70％，
二段流化装置42内发生的反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4，Fe 3O 4+CO→CO 2+3FeO，FeO+CO→CO 2+Fe。
在一种优选的实施方式中，步骤(1)中含铁物料为铁精粉、赤铁含铁物料、褐铁含铁物料、菱铁含铁物料、赤泥等工业固体废物、氧化铁皮中的一种或多种，含铁物料中铁含量不低于30％；破碎研磨后的含铁物料的粒度小于3mm；含铁物料的喷吹量为20～280t/h。
在一种优选的实施方式中，步骤(3)中煤粉的配加比例为含铁物料的40％-50％，
煤粉为喷吹煤、烟煤、半焦、兰炭、泥煤中的一种或多种，煤粉的碳含量大于70％，粒度小于5mm；和/或
步骤(3)中熔剂的配加比例为含铁物料的13％-17％，
熔剂为碱性熔剂，熔剂为白云石与石灰的混合物，
其中，白云石中氧化镁的含量不低于17％，白云石的粒度小于10mm，
石灰中氧化钙的含量不低于70％，石灰的粒度小于3mm，
白云石与石灰的配加比例由炉渣的二元碱度与四元碱度确定，石灰与白云石的配加比例为：
石灰：白云石＝1：1.2(2R 4-R 2)～1:2.5(2R 4-R 2)，
其中，R 2＝CaO/SiO 2，R 4＝(CaO+MgO)/(SiO 2+Al 2O 3)。
在一种优选的实施方式中，步骤(4)中含铁物料喷吹载气的载气流量为0-15000Nm 3/h，喷吹压力为100-500kPa；和/或
步骤(4)中煤粉及熔剂喷吹载气的载气流量为0-8000Nm 3/h，喷吹压力为100-500kPa；和/或
步骤(4)中混合物料喷吹载气的喷吹压力为100-500kPa。
为了便于对本申请实施例的理解，下面对本申请实施例示例的含铁物料复合喷吹方法做进一步的描述：
实施例1
本申请的实施例1提供了一种含铁物料复合喷吹方法，包括下述步骤：
(1)含铁物料经球磨机1进行破碎研磨处理后，经皮带输送机2及螺旋给料机3定量定速输送至一段流化装置41，含铁物料经一段流化装置41下部的第一进料口412进入一段流化装置41，第一还原性气体经一段流化装置41底部的第一进气口411进入一段流化装置41，含铁物料与第一还原性气体进行对流换热，第一还原性气体对含铁物料进行脱水干燥处理及一级预热预还原处理，一级预热预还原处理的第一还原性气体的温度为500-700℃，CO含量为10-20％，含铁物料与第一还原性气体一同经一段流化装置41上部的第一出料口413排出并进入第一旋风分离器43，在第一旋风分离器43内含铁物料与第一还原性气体发生气固分离，得到一级预热预还原后的含铁物料及第一还原废气，一级预热预还原后的含铁物料经第一旋风分离器43底部出料口排出，并依靠重力经二段流化装置42下部的进料口进入二段流化装置42，第一还原废气经第一旋风分离器43顶部的排气口排出至还原废气储罐5；
(2)熔融还原炉7产生煤气经改质处理后，得到的改质煤气作为第二还原性气体，一级预热预还原处理后的含铁物料经二段流化装置42下部的第二进料口422进 入二段流化装置，第二还原性气体经二段流化装置42底部的第二进气口421进入二段流化装置42，一级预热预还原处理后的含铁物料与第二还原性气体进行对流换热，第二还原性气体对一级预热预还原处理后的含铁物料进行二级预热预还原处理，含铁物料与第二还原性气体经二段流化装置42上部的第二出料口423排出并进入第二旋风分离器44，在第二旋风分离器44内，含铁物料与第二还原性气体进行气固分离，得到二级预热预还原处理后含铁物料和第二还原废气，二级预热预处理后的含铁物料经第二旋风分离器44底部出料口排出至预处理密封罐427或经返料器426循环回到二段流化装置42，第二还原废气经第二旋风分离器44顶部的排气口排出，并作为第一还原性气体经一段流化装置41上部的第一进气口411循环进入一段流化装置41；
(3)二级预热预还原处理后的含铁物料经预处理密封罐427排出至热矿喷吹罐611，并经过第一旋转给料机612定量输送至第一喷吹管线613；煤粉依次经过煤粉储料罐621、煤粉中间罐622及煤粉喷吹罐623后，经第二旋转给料机628定量输送至第二喷吹管线629，熔剂依次经过熔剂配料仓624、熔剂储料罐625、熔剂中间罐626及熔剂喷吹罐627后，经第二旋转给料机628定量输送至第二喷吹管线629；第一喷吹管线628和第二喷吹管线629在进入熔融还原炉7的固体喷枪64前进行汇合，合并为一条复合喷吹管线63，使煤粉、熔剂与二级预热预还原处理后的含铁物料在喷吹入熔融还原炉之前在复合喷吹管线63内进行预混合，以使含铁物料携带的显热对煤粉和熔剂进行预热；
(4)预混合后的混合物料经复合喷吹管线63及若干支管632，进入熔融还原炉7的各固体喷枪64，经各固体喷枪64混合喷吹进入熔融还原炉7，其中，含铁物料喷吹载气、煤粉及熔剂喷吹载气、混合物料喷吹载气均为一级预热预还原处理的第一还原废气。
具体的，含铁物料为铁精粉、赤铁矿粉、褐铁矿粉、菱铁矿粉、赤泥等工业固体废物、氧化铁皮中的一种或多种，且含铁物料中铁含量不低于30％，破碎研磨后的含铁物料的粒度小于3mm，含铁物料的喷吹量为20～280t/h。
具体的，煤粉的配加比例为含铁物料的40％-50％，煤粉为喷吹煤、烟煤、半焦、兰炭、泥煤中的一种或多种，煤粉的碳含量大于70％，粒度小于5mm。
具体的，熔剂的配加比例为含铁物料的13％-17％，熔剂为碱性熔剂，熔剂为白云石与石灰的混合物，其中，白云石的粒度小于10mm，白云石中氧化镁的含量不低于17％，石灰的粒度小于3mm，石灰中氧化钙的含量不低于70％。该熔剂用于脱除原料中的酸性杂质，生成低熔点物质Ca 2SiO 4，降低炉渣粘度及熔化性温度，使得炉渣易于流动。
具体的，在熔剂配料仓624内进行白云石与石灰的配料预混合，通过控制炉渣二元碱度R 2＝CaO/SiO 2与炉渣四元碱度R 4＝(CaO+MgO)/(SiO 2+Al 2O 3)来确定熔剂配比；石灰与白云石配比为：
石灰：白云石＝1：1.2(2R 4-R 2)～1:2.5(2R 4-R 2)。
具体的，含铁物料喷吹载气的载气流量为0-15000Nm 3/h，喷吹压力为100-500kPa。
具体的，煤粉及熔剂喷吹载气的载气流量为0-8000Nm 3/h，喷吹压力为100-500kPa。
具体的，混合物料喷吹载气的喷吹压力为100-500kPa。
上述含铁物料预处理方法固气比小，传热及传质速率快，能有效提高含铁物料的预还原度和预热温度的极限值；两级预热预处理可实现能量的分级利用，在有限的反应时间内，提高能量的利用率。含铁物料经过上述两级预热预还原处理，有利于提高了熔融还原反应的速率；同时，有利于进一步提高产能，降低煤耗，提高熔融还原技术的能耗指标。经过两级预热预还原处理，在不同参数下含铁物料的温度及预还原度见表1。
表1
Figure PCTCN2022076645-appb-000001
上述复合喷吹方法可高效利用预热后含铁物料携带的大量显热，有效减少热矿输送过程中的能量损失；有效提高煤粉温度，煤粉表面层状和孔隙结构增加，粉化发展，比表面积增加，改善熔融还原反应的动力学条件，提高熔池反应速率；提高煤粉的喷流性，有利于气力输送；促进煤粉在熔融还原炉7中熔融反应的前移，提高煤粉在铁水熔池中的吸收率；进一步降低烟气中煤粉颗粒的带出量，降低除尘灰的含碳量；同时，有利于降低煤耗，提高熔融还原技术的能耗指标。经过复合喷吹方法处理，在不同参数下煤粉的温度及吸收率见表2。
表2
Figure PCTCN2022076645-appb-000002
上述含铁物料复合喷吹方法对含铁物料的处理效率高、流程短、能源综合利用率高，可降低铁浴熔融还原工艺煤耗至850kg/t以下，热效率增加3-5％。
根据本申请的另一个方面，提供了一种基于上述任一项的含铁物料复合喷吹方法的含铁物料复合喷吹系统，如图2所示，其中：
复合喷吹系统包括含铁物料预处理子系统4及复合喷吹子系统6；
含铁物料预处理子系统4包括一段流化装置41、二段流化装置42、第一旋风分 离器43、第二旋风分离器44，
一段流化装置41与二段流化装置42串联设置，一段流化装置41下部的第一出料口413与二段流化装置42的第二进料口422之间设置有第一旋风分离器43，二段流化装置42上部的第二出料口423与一段流化装置41的第一进气口411之间设置有第二旋风分离器44，
一段流化装置41采用循环流化装置、鼓泡流化装置、环形流化装置其中的一种，和/或
二段流化装置42采用循环流化装置；
复合喷吹子系统6包括热矿喷吹装置61、煤粉/熔剂喷吹装置62、复合喷吹管线63、固体喷枪64，
热矿喷吹装置61与二段流化装置42连接，热矿喷吹装置61包括依次连接的热矿喷吹罐611、第一旋转给料机612、第一喷吹管线613，
煤粉/熔剂喷吹装置62包括煤粉喷吹装置、熔剂喷吹装置、第二喷吹管线629，
煤粉喷吹装置与熔剂喷吹装置共同连接至第二喷吹管线629，
第二喷吹管线629与第一喷吹管线613汇合构成复合喷吹管线63，复合喷吹管线63与熔融还原炉7的固体喷枪64连接。
在一种优选的实施方式中，含铁物料经一段流化装置41下部的第一进料口412进入一段流化装置41，第一还原性气体经一段流化装置41底部的第一进气口411进入一段流化装置41，含铁物料与第一还原性气体进行对流换热，第一还原性气体对含铁物料进行脱水干燥处理及一级预热预还原处理，
含铁物料与第一还原性气体经一段流化装置41上部的第一出料口413排出并进入第一旋风分离器43进行气固分离，得到一级预热预还原处理后的含铁物料和第一还原废气，第一还原废气经第一旋风分离器43顶部的排气口排出并进入还原废气储罐5，
其中，第一还原性气体的温度为500℃-700℃，CO含量为10％-20％，一级预热预还原处理后的含铁物料的预还原度为0％-20％，第一还原废气的温度为150℃-250℃，
一段流化装置41内发生的还原反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4。
在一种优选的实施方式中，一级预热预还原处理后的含铁物料经二段流化装置42下部的第二进料口422进入二段流化装置42，第二还原性气体经二段流化装置42底部的第二进气口421进入二段流化装置42，一级预热预还原处理后的含铁物料与第二还原性气体进行对流换热，第二还原性气体对一级预热预还原处理后的述含铁物料进行二级预热预还原处理，
一级预热预还原处理后的含铁物料与第二还原性气体经二段流化装置42上部的第二出料口423排出并进入第二旋风分离器44进行气固分离，得到二级预热预还原处理后的含铁物料和第二还原废气，第二还原废气作为第一还原性气体循环进入一段流化装置41，二级预热预还原处理后的含铁物料经第二旋风分离器44底部出料口排出至预处理密封罐427或经返料器426循环回到二段流化装置42，
其中，第二还原性气体为熔融还原炉7的改质煤气，第二还原性气体的流量为70000-120000Nm 3/h,流速为6m/s-10m/s，温度为800-1000℃，CO含量大于50％以上， 氧化度小于20％，二级预热预还原处理后的含铁物料的温度为600℃-800℃，预还原度为40％-70％，
二段流化装置42内发生的反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4，Fe 3O 4+CO→CO 2+3FeO，FeO+CO→CO 2+Fe。
在一种优选的实施方式中，复合喷吹子系统6还包括：
调流调压阀，调流调压阀设置于第一喷吹管线613与第二喷吹管线629汇合处前方，调流调压阀用以调节管线内介质流量及进行大压差范围内的压力调节；
气动三通球阀球阀组，气动三通球阀球阀组设置于管线汇合处，由气动执行机构和T型气动三通球阀组成，气动执行机构用于接收控制信号，同步驱动和控制三通球阀的动作和开闭状态，T型气动三通球阀用于控制管路中介质的合流；
压力变送器，压力变送器设置于调流调压阀与第一喷吹管线613与第二喷吹管线629汇合处之前，压力变送器用以调控第一喷吹管线613与第二喷吹管线629内载气的喷吹压力。
在一种优选的实施方式中，复合喷吹管线63末端分离为若干支管632，分别连接至熔融还原炉7各个固体喷枪64；复合喷吹管线63末端分离处设置有分配器，用于控制各支管632的混合物料的流量；各支管632安装有补气装置，用于进行载气补充；固体喷枪64的数量至少为两个，固态喷枪上设有防堵件，用于防止渣铁堵塞固体喷枪64。
在一种优选的实施方式中，含铁物料预处理子系统还包括：
预处理密封罐，预处理密封罐与第二旋风分离器及二段流化装置连接；
热矿喷吹罐，热矿喷吹罐与预处理密封罐连接，含铁物料依靠重力在预处理密封罐与热矿喷吹罐之间输送，预处理密封罐与热矿喷吹罐之间设有高温圆顶进料阀与旋转式排气阀，热矿喷吹罐出料口还设置有旋转卸料阀。
为了便于对本申请实施例的理解，下面对本申请实施例示例的含铁物料复合喷吹系统做进一步的描述：
实施例2
本申请的实施例2提供了一种含铁物料复合喷吹系统，其包括含铁物料预处理子系统4与复合喷吹子系统6。其中，含铁物料预处理子系统4包括一段流化装置41、二段流化装置42、第一旋风分离器43、第二旋风分离器44；复合喷吹子系统6包括热矿喷吹装置61、煤粉/熔剂喷吹装置62、复合喷吹管线63、固体喷枪64。其中，一段流化装置41与二段流化装置42连接，一段流化装置41与二段流化装置42之间设置有第一旋风分离器43、第二旋风分离器44，二段流化装置42与热矿喷吹罐611连接。第一喷吹管线613与第二喷吹管线629汇合构成复合喷吹管线63，复合喷吹管线63与固体喷枪64连接。
通过设置一段流化装置41，对含铁物料进行脱水干燥处理及一级预热预还原处理，设置二段流化装置42，对含铁物料进行二级预热预还原处理，大大提高了含铁物料的预还原度；设置第一喷吹管线613喷吹预还原后的含铁物料，第二喷吹管线629喷吹煤粉和熔剂，使预还原后的含铁物料和煤粉、熔剂在复合喷吹管线63中混合，从而高效利用了预还原后含铁物料携带的大量显热，对煤粉进行预热，预热后 的煤粉表面结构发生明显变化，层状和孔隙结构增加，粉末化发展，比表面积增加，煤粉更加疏松，改善了煤粉的喷流性，使煤粉易于被流化，有利于气力输送；同时还可以提高煤粉进入熔融还原炉7的温度至200℃以上，优化反应条件，提高熔池冶炼效率，改善了还原反应的动力学条件，促进煤粉在熔融还原炉7中熔融反应的前移，使煤粉在熔融还原炉7中的吸收率提高10％以上，降低了烟气中煤粉颗粒的带出量，除尘灰的含碳量降低20％以上；此外，还可以使含铁物料、煤粉及熔剂在输送过程中进行充分混合，提高了混合均匀度，有利于在熔融还原炉7中充分反应，减少了物料的损失。
具体的，一段流化装置41采用循环流化装置、鼓泡流化装置、环形流化装置其中的一种；二段流化装置42采用循环流化装置。
作为一种实施方式，该含铁物料复合喷吹系统还包括依次连接的研磨装置及输送装置，含铁物料经研磨装置破碎研磨处理后，经输送装置定量定速输送至一段流化装置41进行脱水干燥处理及一级预热预还原处理。
具体的，本实施例对研磨装置的类型不做限定，只要能实现对含铁物料的破碎处理即可。优选的，研磨装置为球磨机1，含铁物料经球磨机1破碎研磨后的粒度小于3mm，以保证含铁物料能够充分被还原熔融。
具体的，本实施例对输送装置的类型不做限定，只要能实现对含铁物料的定量定速输送即可。优选的，输送装置包括皮带输送机2和螺旋给料机3，皮带输送机2用于控制含铁物料的定速输送及含铁物料的提升，螺旋给料机3用于控制含铁物料的定量输送。更优选地，螺旋给料机3为单螺旋给料机，通过控制该单螺旋给料机的转速以控制含铁物料的给料量，其中，含铁物料的给料量为20-280t/h，该给料量下可以确保含铁物料在一段流化装置41及二段流化装置42中被充分预还原，并在后续的熔融还原炉7中充分还原。
其中，球磨机1的出料口与皮带输送机2底部的进料槽相连，皮带输送机2上部的出料槽与螺旋给料机3的进料口相连，螺旋给料机3的出料口与一段流化装置41下部的第一进料口412相连。
作为一种实施方式，一段流化装置41与二段流化装置42之间设置有第一旋风分离器43，具体的，一段流化装置41的第一出料口413与二段流化装置42的第二进料口422之间设置有第一旋风分离器43。含铁物料经一段流化装置41下部的第一进料口412进入一段流化装置41，第一还原性气体经一段流化装置41底部的进气口进入一段流化装置41，含铁物料与第一还原性气体进行对流换热，在高温及还原性氛围作用下对含铁物料进行脱水干燥处理及一级预热预还原处理，含铁物料与第一还原性气体经一段流化装置41上部的第一出料口413排出并进入第一旋风分离器43进行气固分离，得到一级预热预还原处理后的含铁物料和第一还原废气，第一还原废气经第一旋风分离器43顶部的排气口排出并进入还原废气储罐5。
通过使含铁物料经一段流化装置41下部的第一进料口412进入一段流化装置41，第一还原性气体经一段流化装置41底部的第一进气口411进入一段流化装置41，第一还原性气体不仅使含铁物料的颗粒悬浮，实现气、固间有效地接触，且可以同时与含铁物料发生还原反应，在该过程中，含铁物料在一段流化装置41的底部处于紊 流状态，极大地增加了第一还原性气体与含铁物料之间的传质及传热效率，传热系数为350-1660W/(m 2·K)，为堆积态反应穿的10倍以上。
具体的，第一还原性气体的温度为500℃-700℃，CO含量为10％-20％；一段流化装置41内发生的还原反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4；一级预热预还原处理后的含铁物料的预还原度为0％-20％，第一还原废气的温度为150℃-250℃。
在一段流化装置41内，含铁物料与第一还原性气体进行对流换热，含铁物料内结晶水在第一还原性气体的高温作用下全部除去，并与第一还原性气体发生还原反应，部分Fe 2O 3还原为Fe 3O 4，预还原度为0-20％；反应后的含铁物料与第一还原性气体一同经一段流化装置41上部第一出料口413排出，并进入第一旋风分离器43，在第一旋风分离器43内，反应后的含铁物料与第一还原性气体发生气固分离，得到一级预热预还原处理后的含铁物料及第一还原废气，第一还原废气的温度为150℃-250℃；一级预热预还原处理后的含铁物料经第一旋风分离器43底部的出料口排出，并经二段流化装置42下部的第二进料口422进入二段流化装置42，第一还原废气经过第一旋风分离器43顶部的排气口排出至还原废气储罐5。
具体的，含铁物料依靠重力从第一旋风分离器43出料口输送至二段流化装置42的进料口；优选，为了避免二段流化装置42中的第二还原性气体泄漏进入第一旋风分离器43，第一旋风分离器43与二段流化装置42之间设置机械蝶阀。
具体的，一段流化装置41的底部和顶部均设置有热电偶，以检测第一还原性气体进出一段流化装置41时的温度，从而得到经过一级预热预还原处理后的含铁物料的温度，以调控第一还原性气体的通入量或含铁物料的下料量。
具体的，一段流化装置41的操作压力为70-90kPa，优选为80kPa。
作为一种实施方式，二段流化装置42与一段流化装置41之间设置有第二旋风分离器44，具体的，二段流化装置42上部的第一出料口423与一段流化装置41的第一进气口411之间设置有第二旋风分离器44。含铁物料经二段流化装置42下部的第二进料口422进入二段流化装置42，第二还原性气体经二段流化装置42底部的第一进气口421进入二段流化装置42，含铁物料与第二还原性气体进行对流换热，对含铁物料进行二级预热预还原处理；含铁物料与第二还原性气体经二段流化装置42上部的第二出料口423排出并进入第二旋风分离器44进行气固分离，得到二级预热预还原处理后的含铁物料和第二还原废气。
通过使含铁物料经二段流化装置42下部的第二进料口422进入二段流化装置42，第二还原性气体经二段流化装置42底部的第二进气口421进入二段流化装置42，第二还原性气体不仅使含铁物料的颗粒悬浮，实现气、固间有效地接触且可以同时与含铁物料发生还原反应，在该过程中，含铁物料在二段流化装置42的底部处于紊流状态，极大地增加了第二还原性气体与含铁物料之间的传质及传热效率，传热系数为350-1660W/(m 2·K)，为堆积态反应的10倍以上，极大地缩短了二级预热预还原反应的时间。
具体的，第二还原性气体的流量为70000-120000Nm 3/h,流速为6m/s-10m/s，温度为800-1000℃，CO含量大于50％以上，氧化度不超过20％，第二还原性气体为熔融还原炉7的改质煤气；第二还原废气作为第一还原性气体进入一段流化装置41； 二级预热预还原处理的反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4，Fe 3O 4+CO→CO 2+3FeO，FeO+CO→CO 2+Fe；二级预热预还原处理后的含铁物料的温度为600℃-800℃，预还原度为40％-70％。
含铁物料与第二还原性气体进行对流换热，并与第二还原性气体发生还原反应，反应后的含铁物料和第二还原性气体一同经二段流化装置42上部的第二出料口422排出，而进入第二旋风分离器44；在第二旋风分离器44内，含铁物料与第二还原性气体发生气固分离，二级预热预还原处理后的含铁物料经第二旋风分离器44底部的出料口排出，第二还原废气经第二旋风分离器44顶部的排气口排出，并作为第一还原性气体经一段流化装置41底部的第一进气口411进入一段流化装置41。
作为一种实施方式，熔融还原炉7的上部通过汽化烟道81与改质煤气输送管道82相通，改质煤气输送管道82与二段流化装置42底部的第二进气口421相通，以使得熔融还原炉7的改质煤气作为第二还原性气体对二段流化装置42中的含铁物料进行二级预热预还原处理。
具体的，汽化烟道81与改质煤气输送管道82的连接位置距汽化烟道81的上端5-10m。
具体的，改质煤气输送管道82设置有流量调节阀及流量计，以便于根据流量计的数值调节改质煤气输送管道82中的改质煤气输送流量，从而保持恒定的改质煤气输送流量。进一步的，改质煤气输送管道82靠近二段流化装置42的一端设置有调流调压阀，用于精确控制改质煤气的流量，保证改质煤气以恒定的流量进入二段流化装置42，此外，还可以实现1MPa工作压差范围内的调节，保持调流调压阀后的压力稳定。
优选的，为了保证改质煤气输送管道82可以承受高温改质煤气的输送，改质煤气输送管道82内表面砌筑有耐火砖。
具体的，改质煤气输送管道82的输送流量占熔融还原炉7产生的煤气流量的30-50％，其余的改质煤气经汽化烟道81进入余热发电系统9进行发电，转化为电力资源加以利用。
作为一种实施方式，二级预热预还原处理后的含铁物料经第二旋风分离器44底部出料口排出并经返料器426，并从返料器426经循环料入口425循环回到二段流化装置42。具体的，返料器426为U型结构。通过设置返料器426，可以实现二段流化装置42中含铁物料的循环回送，并提供气体密封，防止气体反串回二段流化装置42。
具体的，返料器426底部设置有循环风帽，通过设置循环风帽对返料器426喷吹循环流化气体，对返料器426内的含铁物料进行流化，将含铁物料从返料器426回送入二段流化装置42，从而实现含铁物料的循环流化二级预热预还原处理。进一步，返料器426底部喷吹的循环流化气体可以为改质煤气、第一还原废气或惰性气体中的一种或几种，循环流化气体的流量占第二还原性气体流量的5-10％，优选地，循环流化气体的流量为5000-20000Nm 3/h。
作为一种实施方式，二段流化装置42的下部设置有第三出料口424，第三出料口424与预处理密封罐427连通，预处理密封罐427与热矿喷吹装置61相连。通过 设置预处理密封罐427，可以暂时存储二级预热预还原处理后的含铁物料，其中，二级预热预还原处理后的含铁物料的温度为600-800℃，预还原度为40％-70％。
具体的，二段流化装置42还可以通入一定量助燃空气，通过CO、H2的燃烧反应，生成大量的热量提高第二还原性气体的温度，进而提高二段流化装置42内的还原温度；进一步地，助燃空气可以使用热风炉生产的富氧热风，富氧含量在30-40％，热风流速控制在0-5000Nm 3/h。
具体的，二段流化装置42的底部和顶部均设置有热电偶，以检测第二还原性气体进出二段流化装置42时的温度，从而得到经过二级预热预还原处理后的含铁物料的温度，以调控第二还原性气体的通入量或含铁物料的下料量。
具体的，二段流化装置42的操作压力为70-90kPa，优选为80kPa。
具体的，含铁物料在二段流化装置42内的反应时间在10min以内。
作为一种实施方式，该含铁物料复合喷吹系统还包括：调流调压阀、气动三通球阀球阀组及压力变送器。调流调压阀设置于第一喷吹管线613与第二喷吹管线629汇合处前方，调流调压阀用以调节管线内介质流量及进行大压差范围内的压力调节；气动三通球阀球阀组设置于管线汇合处，由气动执行机构和T型气动三通球阀组成，气动执行机构用于接收控制信号，同步驱动和控制三通球阀的动作和开闭状态，T型气动三通球阀用于控制管路中介质的合流；压力变送器设置于调流调压阀与第一喷吹管线613与第二喷吹管线629汇合处前方，压力变送器用以调控第一喷吹管线613与第二喷吹管线629内载气的喷吹压力。
通过在第一喷吹管线613和第二喷吹管线629汇合处前方设置调流调压阀，从而分别控制第一喷吹管线613和第二喷吹管线629的流量，保持恒定流量，同时可以保证第一喷吹管线613和第二喷吹管线629在汇合时压力接近，保证第一喷吹管线613中的含铁物料和第二喷吹管线629中的煤粉、熔剂能够顺利进入复合喷吹管线63进行混合。
可以理解的是，在汇合处前方，第一喷吹管线613和第二喷吹管线629分别设置有调流调压阀，具体的，第一喷吹管线613和第二喷吹管线629上的调流调压阀分别设置在距离汇合处2.5-3.5m的位置处，优选地，设置在3m处。
可以理解的是，在汇合处前方，第一喷吹管线613和第二喷吹管线629上分别设置有压力变送器，压力变送器分别设置在距离汇合处1-2m的位置处。
作为一种实施方式，复合喷吹管线63末端分离为若干支管632，分别连接至熔融还原炉7各固体喷枪64；分离处设置有分配器，用于控制各支管632的混合物料的流量；各支管632安装有补气装置，用于进行载气补充；固体喷枪64的数量至少为两个，固体喷枪64上设有防堵件，用于防止渣铁堵塞固体喷枪64。
具体的，在复合喷吹管线63末端的3-5m处，复合喷吹管线63分离为若干支管632。
具体的，复合喷吹管线63的长度为50-60m，复合喷吹管线63内混合物料的输送速度为15-25m/s，混合物料进入复合喷吹管线63到固体喷枪64的入口处的输送时间不少于3s，以保证含铁物料与煤粉、熔剂在复合喷吹管线63中充分混合。
作为一种实施方式，预处理密封罐427直接连接热矿喷吹罐611，含铁物料的输 送依靠重力，之间设有高温圆顶进料阀与旋转式排气阀，热矿喷吹罐611出料口设置旋转卸料阀。通过在预处理密封罐427和热矿喷吹罐611之间设置有高温圆顶进料阀与旋转式排气阀，使热矿喷吹罐611进料前泄压排气，防止含铁物料颗粒泄漏，保证热矿喷吹罐611的可靠密封。具体的，热矿喷吹罐611的出料口处设置有旋转卸料阀。
具体的，热矿喷吹罐611的出口处连接有两个并联的第一旋转给料机612，经二级预热预还原处理后的含铁物料经两个第一旋转给料机612输送至第一喷吹管线613；煤粉依次经过煤粉储料罐621、煤粉中间罐622及煤粉喷吹罐623后，经第二旋转给料机628输送至第二喷吹管线629，熔剂依次经过熔剂配料仓624、熔剂储料罐625、熔剂中间罐626及熔剂喷吹罐627后，经第二旋转给料机628输送至第二喷吹管线629。第一喷吹管线613中的含铁物料和第二喷吹管线629中的煤粉、熔剂在复合喷吹管线63中预混合后形成混合物料，经过预热预还原处理的含铁物料带入的显热对煤粉及熔剂进行预热，混合物料经固体喷枪64混合喷吹进入熔融还原炉7。
通过在热矿喷吹罐611设置两个并联的第一旋转给料机612，煤粉喷吹罐623和熔剂喷吹罐627后分别设置一个第二旋转给料机628，以控制各喷吹罐的给料量，并精确控制含铁物料、煤粉、熔剂之间的配比，控制喷吹精度，通过调控第一旋转给料机612与第二旋转给料机628的转速，控制煤粉的配比为含铁物料的40％-50％，熔剂的配比为含铁物料的13％-17％。
作为一种实施方式，还原废气储罐5分别与第一喷吹管线613、第二喷吹管线629和复合喷吹管线63相连通，第一喷吹管线613、第二喷吹管线629和复合喷吹管线63的喷吹载气均为一段流化装置41的第一还原废气。该设置方式可以实现第一还原废气废气的循环再利用，提高了该系统能量的利用率；且减少了预热后含铁物料的热量散失；减少了该系统中氮的入炉量，从而降低烟气中氮氧化物的生成；此外，喷吹载气中带入的CO 2易与煤粉反应生成CO，从而提高了还原性气氛，改善了熔融还原炉7的动力学条件。
进一步地，第一喷吹管线613中喷吹载气的流量为0-15000Nm 3/h；第二喷吹管线629中喷吹载气的流量为0-8000Nm 3/h；第一喷吹管线613、第二喷吹管线629和复合喷吹管线63中喷吹载气的喷吹压力均为100-500kPa。具体的，第一喷吹管线613、第二喷吹管线629和复合喷吹管线63的喷吹载气管线上均设置有流量调节阀，用于控制第一喷吹管线613、第二喷吹管线629和复合喷吹管线63的载气流量。
上述含铁物料预处理子系统固气比小，传热及传质速率快，能有效提高含铁物料的预还原度和预热温度的极限值；两级预热预处理可实现能量的分级利用，在有限的反应时间内，提高能量的利用率。含铁物料经过上述两级预热预还原处理，有利于提高了熔融还原反应的速率；同时，有利于进一步提高产能，降低煤耗，提高熔融还原技术的能耗指标。
上述复合喷吹子系统可高效利用预热后含铁物料携带的大量显热，有效减少热矿输送过程中的能量损失；有效提高煤粉温度，煤粉表面层状和孔隙结构增加，粉化发展，比表面积增加，改善熔融还原反应的动力学条件，提高熔池反应速率；提高煤粉的喷流性，有利于气力输送；促进煤粉在熔融还原炉7中熔融反应的前移， 提高煤粉在铁水熔池中的吸收率；进一步降低烟气中煤粉颗粒的带出量，降低除尘灰的含碳量；同时，有利于降低煤耗，提高熔融还原技术的能耗指标。
上述含铁物料复合喷吹系统对含铁物料的处理效率高、流程短、能源综合利用率高，可降低铁浴熔融还原工艺煤耗至850kg/t以下，热效率增加3-5％。
本申请中未述及的地方采用或借鉴已有技术即可实现。
以上，仅为本申请的具体实施方式，但本申请的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本申请揭露的技术范围内，可轻易想到其各种变化或替换，这些都应涵盖在本申请的保护范围之内。因此，本申请的保护范围应以权利要求的保护范围为准。
在本申请中，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”、“固定”等术语应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或成一体；可以是机械连接，也可以是电连接，还可以是通信；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通或两个元件的相互作用关系。对于本领域的普通技术人员而言，可以根据具体情况理解上述术语在本申请中的具体含义。
上文的公开提供了许多不同的实施方式或例子用来实现本申请的不同结构。为了简化本申请的公开，上文中对特定例子的部件和设置进行描述。当然，它们仅仅为示例，并且目的不在于限制本申请。此外，本申请可以在不同例子中重复参考数字和/或参考字母，这种重复是为了简化和清楚的目的，其本身不指示所讨论各种实施方式和/或设置之间的关系。此外，本申请提供了的各种特定的工艺和材料的例子，但是本领域普通技术人员可以意识到其他工艺的应用和/或其他材料的使用。

Claims (10)

  1. 一种含铁物料复合喷吹方法，其特征在于,所述方法包括下述步骤：
    (1)将含铁物料破碎研磨后，对所述含铁物料进行脱水干燥处理及一级预热预还原处理，所述一级预热预还原处理的第一还原性气体的温度为500-700℃，CO含量为10-20％；
    (2)将一级预热预还原处理后的含铁物料进行二级预热预还原处理，所述二级预热预还原处理的第二还原性气体为改质煤气，温度为800-1000℃，CO含量至少50％，氧化度不超过20％；
    (3)将煤粉、熔剂与二级预热预还原处理后的含铁物料在喷吹入熔融还原炉之前在喷吹管线内进行预混合，以使所述含铁物料携带的显热对煤粉和熔剂进行预热；
    (4)将预混合后的混合物料喷吹入熔融还原炉，其中，含铁物料喷吹载气、煤粉及熔剂喷吹载气、混合物料喷吹载气均为所述一级预热预还原处理的第一还原废气。
  2. 根据权利要求1所述的含铁物料复合喷吹方法，其特征在于，所述对所述含铁物料进行脱水干燥处理及一级预热预还原处理包括：
    所述含铁物料经一段流化装置下部的第一进料口进入一段流化装置，第一还原性气体经一段流化装置底部的第一进气口进入一段流化装置，所述含铁物料与所述第一还原性气体进行对流换热，所述第一还原性气体对所述含铁物料进行脱水干燥处理及一级预热预还原处理，
    所述含铁物料与所述第一还原性气体经一段流化装置上部的第一出料口排出并进入第一旋风分离器进行气固分离，得到一级预热预还原处理后的含铁物料和第一还原废气，所述第一还原废气经第一旋风分离器顶部的排气口排出并进入还原废气储罐，
    所述一级预热预还原处理后的含铁物料的预还原度为0％-20％，所述第一还原废气的温度为150℃-250℃，
    一段流化装置内发生的还原反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4。
  3. 根据权利要求1所述的含铁物料复合喷吹方法，其特征在于，所述将一级预热预还原处理后的含铁物料进行二级预热预还原处理包括：
    所述一级预热预还原处理后的含铁物料经二段流化装置下部的第二进料口进入二段流化装置，第二还原性气体经二段流化装置底部的第二进气口进入二段流化装置，所述一级预热预还原处理后的含铁物料与所述第二还原性气体进行对流换热，所述第二还原性气体对所述一级预热预还原处理后的含铁物料进行二级预热预还原处理，
    所述一级预热预还原处理后的含铁物料与所述第二还原性气体经二段流化装置上部的第二出料口排出并进入第二旋风分离器进行气固分离，得到二级预热预还原 处理后的含铁物料和第二还原废气，所述第二还原废气作为第一还原性气体循环进入一段流化装置，所述二级预热预还原处理后的含铁物料经第二旋风分离器底部出料口排出至预处理密封罐或经返料器循环回到二段流化装置，
    所述二级预热预还原处理后的含铁物料的温度为600℃-800℃，预还原度为40％-70％，
    所述二段流化装置内发生的反应有：3Fe 2O 3+CO→CO 2+2Fe 3O 4，Fe 3O 4+CO→CO 2+3FeO，FeO+CO→CO 2+Fe。
  4. 根据权利要求1所述的含铁物料复合喷吹方法，其特征在于：
    步骤(1)中所述含铁物料为铁精粉、赤铁矿粉、褐铁矿粉、菱铁矿粉、赤泥等工业固体废物、氧化铁皮中的一种或多种，所述含铁物料中铁含量不低于30％；破碎研磨后的所述含铁物料的粒度小于3mm；所述含铁物料的喷吹量为20～280t/h。
  5. 根据权利要求1所述的含铁物料复合喷吹方法，其特征在于：
    步骤(3)中所述煤粉的配加比例为所述含铁物料的40％-50％，
    所述煤粉为喷吹煤、烟煤、半焦、兰炭、泥煤中的一种或多种，所述煤粉的碳含量大于70％，粒度小于5mm；和/或
    步骤(3)中所述熔剂的配加比例为所述含铁物料的13％-17％，
    所述熔剂为碱性熔剂，所述熔剂为白云石与石灰的混合物，
    其中，所述白云石中氧化镁的含量不低于17％，所述白云石的粒度小于10mm，
    所述石灰中氧化钙的含量不低于70％，所述石灰的粒度小于3mm，
    所述白云石与所述石灰的配加比例由炉渣的二元碱度与四元碱度确定，所述石灰与所述白云石的配加比例为：
    石灰：白云石＝1：1.2(2R 4-R 2)～1:2.5(2R 4-R 2)，
    其中，R 2＝CaO/SiO 2，R 4＝(CaO+MgO)/(SiO 2+Al 2O 3)。
  6. 根据权利要求1所述的含铁物料复合喷吹方法，其特征在于：
    步骤(4)中所述含铁物料喷吹载气的载气流量为0-15000Nm 3/h，喷吹压力为100-500kPa；和/或
    步骤(4)中所述煤粉及熔剂喷吹载气的载气流量为0-8000Nm 3/h，喷吹压力为100-500kPa；和/或
    步骤(4)中所述混合物料喷吹载气的喷吹压力为100-500kPa。
  7. 一种基于如权利要求1-6任一项所述的含铁物料复合喷吹方法的含铁物料复合喷吹系统，其特征在于：
    所述系统包括含铁物料预处理子系统及复合喷吹子系统；
    所述含铁物料预处理子系统包括一段流化装置、二段流化装置、第一旋风分离器、第二旋风分离器，
    所述一段流化装置与所述二段流化装置串联设置，所述一段流化装置的第一出料口与所述二段流化装置的第二进料口之间设置有所述第一旋风分离器，所述二段流化装置的第二出料口与所述一段流化装置的第一进气口之间设置有所述第二旋风分离器，
    所述一段流化装置采用循环流化装置、鼓泡流化装置、环形流化装置其中的一种，和/或
    所述二段流化装置采用循环流化装置；
    所述复合喷吹子系统包括热矿喷吹装置、煤粉/熔剂喷吹装置、复合喷吹管线、固体喷枪，
    所述热矿喷吹装置与所述二段流化装置连接，所述热矿喷吹装置包括依次连接的热矿喷吹罐、旋转给料机、第一喷吹管线，
    所述煤粉/熔剂喷吹装置包括煤粉喷吹装置、熔剂喷吹装置、第二喷吹管线，
    所述煤粉喷吹装置与熔剂喷吹装置共同连接至所述第二喷吹管线，
    所述第二喷吹管线与所述第一喷吹管线汇合构成所述复合喷吹管线，所述复合喷吹管线与熔融还原炉的所述固体喷枪连接。
  8. 根据权利要求7所述的含铁物料复合喷吹系统，其特征在于，所述复合喷吹子系统还包括：
    调流调压阀，所述调流调压阀设置于所述第一喷吹管线与所述第二喷吹管线汇合处前方，所述调流调压阀用以调节管线内介质流量及进行大压差范围内的压力调节；
    气动三通球阀球阀组，所述气动三通球阀球阀组设置于管线汇合处，由气动执行机构和T型气动三通球阀组成，所述气动执行机构用于接收控制信号，同步驱动和控制三通球阀的动作和开闭状态，所述T型气动三通球阀用于控制管路中介质的合流；
    压力变送器，所述压力变送器设置于所述调流调压阀与所述第一喷吹管线与所述第二喷吹管线汇合处之前，所述压力变送器用以调控所述第一喷吹管线与所述第二喷吹管线内载气的喷吹压力。
  9. 根据权利要求7所述的含铁物料复合喷吹系统，其特征在于：
    所述复合喷吹管线末端分离为若干支管，分别连接至熔融还原炉各个固体喷枪；分离处设置有分配器，用于控制各支管的混合物料的流量；各支管安装有补气装置，用于进行载气补充；固体喷枪的数量至少为两个，所述固态喷枪上设有防堵件，用于防止渣铁堵塞所述固体喷枪。
  10. 根据权利要求7所述的含铁物料复合喷吹系统，其特征在于：
    所述含铁物料预处理子系统还包括：
    预处理密封罐，所述预处理密封罐与所述第二旋风分离器及所述二段流化装置连接；
    热矿喷吹罐，所述热矿喷吹罐与所述预处理密封罐连接，含铁物料依靠重力在所述预处理密封罐与所述热矿喷吹罐之间输送，所述预处理密封罐与所述热矿喷吹罐之间设有高温圆顶进料阀与旋转式排气阀，所述热矿喷吹罐出料口还设置有旋转卸料阀。
PCT/CN2022/076645 2021-04-27 2022-02-17 一种含铁物料复合喷吹方法及系统 WO2022227801A1 (zh)

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