CN115896378A - Electric energy heating hydrogen direct reduction iron-making method - Google Patents
Electric energy heating hydrogen direct reduction iron-making method Download PDFInfo
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Abstract
The invention discloses an electric energy heating hydrogen direct reduction iron making method, and belongs to the technical field of ferrous metallurgy. The invention relates to an iron making method by directly reducing hydrogen heated by electric energy, which comprises the following steps: preheating and pre-reducing iron ore powder, final reducing the pre-reduced iron ore powder, dehydrating reduction tail gas and recycling. The iron-containing raw materials are pre-reduced in the pre-reduction fluidized bed and finally reduced in the final reduction fluidized bed, the microwave heating device and the induction heating device are respectively adopted for heating, the reaction temperature of fluidized bed hydrogen iron making is maintained by heating with electric energy, the chemical energy of hydrogen can be fully utilized, the hydrogen reduction efficiency of the fluidized bed is ensured, fluidized bed full hydrogen smelting can be realized, the energy consumption of the fluidized bed hydrogen metallurgy process is effectively reduced, and the economical efficiency of the fluidized bed hydrogen metallurgy process is improved.
Description
Technical Field
The invention belongs to the technical field of ferrous metallurgy, and particularly relates to an electric energy heating method for directly reducing iron by hydrogen.
Background
At present, blast furnace ironmaking is a main process for producing molten iron, the process takes agglomerated sintered ores and pellets as main raw materials and takes coke and coal powder as main fuels, and CO is not replaceable due to the skeleton function of the coke in a blast furnace, so that CO is generated in the blast furnace ironmaking process 2 The emission amount of CO occupies the whole iron and steel industry 2 70% of the emission is the main carbon emission industry. In order to reduce carbon at the source of the ferrous metallurgy industry, development of a new green low-carbon metallurgy technology is urgently needed. The hydrogen is an excellent reducing agent and clean energy, the direct reduction iron-making process which takes hydrogen to replace carbon as the reducing agent is explored and developed, the carbon dioxide emission in the iron-making process can be reduced from the source, and the development trend of green, low-carbon and clean production in the iron and steel industry is met.
According to different types of reactors, the gas-based direct reduction iron-making process is mainly divided into a shaft furnace process and a fluidized bed process, and compared with the shaft furnace process, the fluidized direct reduction process has the advantages of directly utilizing fine ores, not needing sintering or pelletizing procedures, having small mass transfer resistance in the reaction process, having high heat transfer and reduction efficiency, realizing low-temperature reduction and the like. For the fluidized bed hydrogen iron making process, because the reduction of iron oxide by hydrogen is an endothermic reaction, not only the iron-containing material needs to be heated to the reaction temperature, but also enough heat needs to be provided to maintain the smooth proceeding of the reduction reaction in the fluidized bed, in order to meet the normal production requirement, the amount of hydrogen introduced into the fluidized bed as a heat carrier needs to be increased, which leads to that the amount of hydrogen required by heat balance is far larger than the amount of hydrogen required by the reduction reaction, which causes the serious mismatch of physical heat and chemical energy in the fluidized bed, and leads to the low utilization rate of hydrogen. Therefore, the realization of reasonable heat supply and the improvement of the utilization rate of hydrogen are technical bottlenecks which need to be broken through urgently in developing the fluidized bed hydrogen metallurgy process.
At present, the direct reduction process adopting a fluidized bed as a reactor mainly comprises a FIOR process and a Circored process, wherein the FIOR process adopts a first-stage preheating fluidized bed and a third-stage reduction fluidized bed, the first-stage preheating fluidized bed adopts natural gas or hot flue gas generated after coal gas and air are combusted to preheat mineral powder, reducing gas enters a fourth-stage fluidized bed after being preheated, and the reducing gas is connected in series to complete the reduction reaction of the iron mineral powder through the multistage fluidized beds. The Circored process uses hydrogen obtained by reforming natural gas as a single reducing agent, utilizes a fluidized bed to preheat mineral powder, carries out pre-reduction in a first-stage circulating fluidized bed, carries out final reduction in a second-stage bubbling fluidized bed, and heat required by reduction reaction is provided by heating of fine ore and circulating gas. Patent application No. CN200580017740.5 discloses an apparatus and method for direct reduction employing a two-stage fluidized bed for reduction of iron ore oxides in solid form wherein heat is generated in a first fluidized bed by reaction of a solid carbonaceous material and an oxygen-containing gas and metalliferous feed material is reduced in a second fluidized bed and heat is supplied to the second fluidized bed by a hot off-gas stream and entrained solids flowing from the first fluidized bed. The existing system adopting the fluidized bed to carry out direct reduction has the problems that the ore powder preheating effect is poor, the heat required by reduction needs to be provided by burning carbonaceous fuel, the emission of carbon dioxide is caused, the heat utilization rate is low, and the like. For the total-hydrogen iron-making process, chemical energy is converted into heat energy by burning hydrogen in a fluidized bed to maintain the progress of reduction reaction, so that the reduction of iron ore powder is easily influenced due to overhigh local oxidizing atmosphere; the hydrogen is preheated outside the fluidized bed through the hydrogen heater, a large amount of circulating hydrogen is needed to meet the requirement of reaction heat absorption, so that the energy utilization rate is low, in addition, the equipment of the hydrogen heater is relatively complex, the manufacturing cost is high, the hydrogen brittleness phenomenon easily occurs to metal under the high-temperature condition, and certain potential safety hazards exist. The direct utilization of electric energy to directly supply heat to the fluidized bed reactor is one of the important ways to realize fluidized direct reduction hydrogen metallurgy.
At present, the conventional electric heating techniques are generally microwave heating and induction heating. The microwave heating is to directly heat the material by generating dielectric dissipation in the material through a microwave field, and has the characteristics of selective heating, rapid temperature rise, uniform heating, low energy consumption, catalysis effect on chemical reaction and the like. Patent application No. CN202011060962.8 discloses a method and a device for making iron by hydrogen, in the scheme, iron-containing ore is subjected to hydrogen-rich or pure hydrogen smelting by microwave irradiation in the atmosphere of hydrogen or hydrogen-rich gas. The raw materials of the microwave heating furnace disclosed in the scheme generally contain a certain amount of coal powder with wave-absorbing capacity besides iron ore, and if wave-absorbing substances such as coal powder are not added, hydrogen is injected into the furnace, so that when iron-containing furnace burden is reduced into direct reduced iron with high metallization rate, microwave heating is difficult to continue due to the reduction of the wave-absorbing substances. Patent application No. CN202110053605.7 discloses a hydrogen shaft furnace iron-making system and method using electric energy for heating, a microwave heating section, a middle section, an induction heating section and a cooling section are arranged in a shaft furnace body, and the metallization rates of iron-containing furnace materials with different heights in the shaft furnace are controlled, so that the microwave heating and the induction heating are realized to provide required heat for reduction reaction, but the shaft furnace system cannot directly process powder ore, and the iron oxide pellets have the disadvantages of large mass transfer resistance, low heat transfer and reduction efficiency and the like in the reduction process.
In conclusion, the fluidized bed hydrogen iron making reaction temperature is maintained by utilizing electric energy for heating, the chemical energy of hydrogen is fully utilized, the fluidized bed hydrogen reduction efficiency is ensured, and the key for reducing the energy consumption of full-hydrogen direct reduction iron making and improving the economical efficiency of the hydrogen direct reduction iron making process is realized.
Disclosure of Invention
The invention aims to provide an electric energy heating method for iron making by direct reduction of hydrogen.
In order to achieve the purpose, the technical scheme provided by the invention is as follows:
an electric energy heated hydrogen direct reduction iron-making method comprises the following steps:
iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2 to exchange heat with reduction tail gas from a first cyclone separator 301, then enters the first cyclone separator 301 to exchange heat with the reduction tail gas from a pre-reduction fluidized bed cyclone separator 403, and then enters a pre-reduction fluidized bed body 401 together with powder collected by a bag-type dust collector 303 through a pre-reduction fluidized bed feeder 304, hydrogen from a main pipeline is mixed through a first gas flow regulating valve 405 and water vapor-containing hydrogen from a high-temperature dust collector 6 through a third gas flow regulating valve 601 to form reduction gas, the reduction gas enters the pre-reduction fluidized bed body 401, and the volume fraction of water vapor in the reduction gas introduced into the pre-reduction fluidized bed body 401 is controlled through the first gas flow regulating valve 405 and the third gas flow regulating valve 601; meanwhile, the microwave heating device 402 is started, the reaction temperature in the pre-reduction fluidized bed body 401 is controlled, hydrogen is fully contacted with iron ore powder and reduction reaction is carried out, and a pre-reduction product with a certain metallization rate is obtained; the pre-reduction tail gas enters a pre-reduction fluidized bed cyclone separator 403 through an upper gas outlet of a pre-reduction fluidized bed body 401, is separated, then enters a first cyclone separator 301 through a gas outlet of the pre-reduction fluidized bed cyclone separator 403, and then enters an inner tube of the gas heat exchanger 8 after powder is removed by a second cyclone separator 302 and a bag-type dust remover 303; the pre-reduction product discharged from the discharge outlet at the lower part of the pre-reduction fluidized bed body 401 and the powder obtained by the separation of the pre-reduction cyclone separator 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404;
hydrogen from a main pipeline is mixed with hydrogen from the shell of the gas heat exchanger 8 through a second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, the induction heating device 502 is started at the same time, the reaction temperature in the final reduction fluidized bed body 501 is controlled, the hydrogen is fully contacted with pre-reduced iron ore powder materials and is subjected to reduction reaction to obtain direct reduced iron, reduced tail gas enters the final reduction fluidized bed cyclone separator 503 through the upper gas outlet of the final reduction fluidized bed body 501, the reduced tail gas is separated and then enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone separator 503, the reduced tail gas after dust removal enters a tube in the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 through a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601, and dust is discharged and collected; the direct reduced iron discharged from a discharge outlet at the lower part of the final reduction fluidized bed body 501 and the powder separated by the final reduction cyclone separator 503 enter a direct reduced iron product bin 7 through a final reduction fluidized bed discharger 504;
the reduction tail gas entering the tube nest inside the gas heat exchanger 8 contains water vapor, after being further cooled by the heat exchanger, the reduction tail gas enters the hydrogen dehydration device 9 through the tube nest gas outlet for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the reduction tail gas after dehydration is hydrogen, the hydrogen enters the shell of the gas heat exchanger 8 through the gas outlet of the hydrogen dehydration device 9, and the reduction tail gas enters the final reduction fluidized bed body 501 through the gas outlet of the shell of the gas heat exchanger 8 after heat exchange of the heat exchanger for recycling as reduction gas.
Furthermore, in the step 1, the total iron mass fraction of the iron ore powder is 63-69%, and the particle size range is 0.02-0.6mm; the reduction temperature of the iron ore powder in the pre-reduction fluidized bed body 401 is 600-630 ℃, the average residence time is 30-65mm, the volume fraction of water vapor in the reduction gas is 1% -4%, the operation gas velocity is 2-2.2m/s, and the metallization rate of the pre-reduction product is 40% -45%.
Furthermore, in the step 2, the reduction temperature of the pre-reduced iron ore powder in the final reduction fluidized bed body 501 is 650-670 ℃, the average retention time is 60-90mm, the operation gas velocity is 2-2.2m/s, and the metallization rate of the directly reduced iron is 93-96.5%.
Furthermore, the microwave heating device 402 is arranged around the furnace body of the pre-reduction fluidized bed body 401, the heating frequency of the microwave heating device 402 is 2.45GHz, and the output power is 0.5-1.0MW.
Furthermore, the induction heating device 502 is arranged around the furnace body of the final reduction fluidized bed body 501, and the induction heating device 502 is a medium frequency induction heating device with a heating frequency of 150-350Hz and an output power of 0.1-1.0MW.
Further, the high temperature dust collector 6 is a metal dust collector or a ceramic dust collector.
Furthermore, the first gas flow regulating valve 405, the second gas flow regulating valve 505, the third gas flow regulating valve 601 and the fourth gas flow regulating valve 602 are all hydrogen one-way flow regulating valves.
Furthermore, the hydrogen dehydration device 9 is one or a combination of a spray tower dehydration device, a molecular sieve dehydration device and a freezing dehydration device.
Compared with the prior art, the technical scheme provided by the invention has the following remarkable advantages:
(1) The invention relates to an electric energy heated hydrogen direct reduction iron-making method, the device comprises a pre-reduction fluidized bed and a final reduction fluidized bed, the reduction degree of iron ore powder in the pre-reduction fluidized bed is lower, the content of iron oxide is high, the content of metal products is low, and a microwave heating device is adopted to heat the pre-reduction fluidized bed; the content of the metal product of the iron ore powder in the final reduction fluidized bed is high, and an induction heating device is adopted to heat the final reduction fluidized bed; according to the reduction conditions of the iron ore powder in different fluidized beds, a proper electric heating mode is selected, compared with the prior direct reduction technology that heat is provided through ore powder preheating and high-temperature reduction gas heat exchange, the direct reduction technology has the advantages of high heating speed, uniform heating, capability of realizing effective control of heating conditions, capability of improving the energy utilization rate and reduction of process energy consumption.
(2) The clean electric energy is directly utilized to continuously supply heat for the fluidized bed reactor, the reaction temperature required by reducing the iron ore powder by the hydrogen in the fluidized bed can be maintained, the heat required by the reduction reaction can be supplemented, the problem that the existing hydrogen-rich metallurgical process depends on the combustion heat supply of carbon fuels such as natural gas, coal gas or coal powder is effectively solved, the pure hydrogen reduction ironmaking is realized, the emission of carbon dioxide is reduced from the source, and the development direction of green low-carbon ironmaking is met.
(3) The tail gas of the final reduction fluidized bed is shunted after passing through a high-temperature dust remover, and a part of hydrogen containing high-temperature water vapor is mixed with fresh low-temperature hydrogen and is sent into the pre-reduction fluidized bed, so that on one hand, the direct recycling of the part of high-temperature hydrogen can be realized, on the other hand, the water vapor content of the mixed hydrogen can be reasonably regulated and controlled, the atmosphere requirement of obtaining a reduction product with a certain metallization rate by pre-reduction of iron ore powder is met, and the normal operation of a microwave heating device and an induction heating device is ensured; the other part of hydrogen containing high-temperature water vapor and the hydrogen of the pre-reduction fluidized bed tail gas after passing through the cyclone separator and the bag-type dust collector are mixed and sent to the gas heat exchanger, so that the temperature of the mixed hydrogen is further reduced, the power consumption of the hydrogen dehydration device is reduced, and the operation cost of the equipment is saved.
(4) And a hydrogen dehydration device is arranged to dehydrate the reduced water-containing hydrogen, and the treated hydrogen is directly introduced into the final reduction fluidized bed after passing through a heat exchanger, so that the full-flow cyclic utilization of the hydrogen is realized.
(5) The method for smelting iron by directly reducing hydrogen heated by electric energy has high utilization rate of reducing gas and energy, can realize fluidized bed total hydrogen smelting, can effectively reduce the energy consumption of the fluidized bed hydrogen metallurgy process, and improves the economy of the fluidized bed hydrogen metallurgy process.
Drawings
FIG. 1 is a simplified process flow diagram of an electric energy heated hydrogen direct reduction iron making process of the present invention;
FIG. 2 is a schematic structural view of an electric-energy-heated hydrogen direct-reduction iron-making apparatus according to the present invention.
Wherein: 1. an iron ore fines bin; 2. a screw feeder; 3. an iron ore powder preheater; 301. a first cyclone separator; 302. a second cyclone separator; 303. a bag-type dust collector; 304. a pre-reduction fluidized bed feeder; 4. pre-reducing the fluidized bed; 401 pre-reducing the fluidized bed body; 402. a microwave heating device; 403. a pre-reduction fluidized bed cyclone separator; 404. a pre-reduction fluidized bed discharger; 405. a first gas flow regulating valve; 5. a final reduction fluidized bed; 501. finally reducing the fluidized bed body; 502. an induction heating device; 503. a final reduction fluidized bed cyclone; 504. a final reduction fluidized bed discharger; 505. a second gas flow regulating valve; 6. a high temperature dust remover; 601. a third gas flow regulating valve; 602. a fourth gas flow regulating valve; 7. a direct reduced iron product bin; 8. a gas heat exchanger; 9. a hydrogen dehydration device.
Detailed Description
For a further understanding of the invention, reference should be made to the following detailed description taken in conjunction with the accompanying drawings and examples.
Example 1
As shown in fig. 2, the electric-energy-heated hydrogen direct-reduction iron making apparatus according to the present embodiment includes an iron ore fines bin 1, a screw feeder 2, an iron ore fines preheater 3, a pre-reduction fluidized bed 4, a final reduction fluidized bed 5, a high temperature dust collector 6, a direct-reduction iron product bin 7, a gas heat exchanger 8, and a hydrogen dehydration apparatus 9.
The iron ore powder preheater 3 comprises a first cyclone separator 301, a second cyclone separator 302, a bag-type dust collector 303 and a pre-reduction fluidized bed feeder 304;
the pre-reduction fluidized bed 4 comprises a pre-reduction fluidized bed body 401, a microwave heating device 402, a pre-reduction fluidized bed cyclone separator 403, a pre-reduction fluidized bed discharger 404 and a first gas flow regulating valve 405;
the final reduction fluidized bed 5 comprises a final reduction fluidized bed body 501, an induction heating device 502, a final reduction fluidized bed cyclone separator 503, a final reduction fluidized bed discharger 504 and a second gas flow regulating valve 505;
a tube array is arranged in the gas heat exchanger 8, a gas outlet of the high-temperature dust remover 6, a gas inlet at the bottom of the pre-reduction fluidized bed body 401 and an inlet of the tube array in the gas heat exchanger 8 are respectively provided with a pipeline which is connected with each other, and a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601 are respectively arranged on the pipelines; the high-temperature dust remover 6 is provided with a dust outlet, and the hydrogen dehydration device 9 is provided with a condensed water outlet.
The discharge hole of the iron ore fine material bin 1 is connected with the feed hole of the spiral feeder 2, the discharge hole of the spiral feeder 2 is connected with the inlet of the second cyclone separator 302, the bottom discharge hole of the second cyclone separator 302 is connected with the inlet of the first cyclone separator 301, the inlet of the first cyclone separator 301 is connected with the gas outlet of the pre-reduction cyclone separator 403, the gas outlet of the first cyclone separator 301 is connected with the inlet of the second cyclone separator 302, the gas outlet of the second cyclone separator 302 is connected with the inlet of the bag-type dust collector 303, the gas outlet of the bag-type dust collector 303 is connected with the inlet of the inner tube of the gas heat exchanger 8, and the bottom discharge hole of the first cyclone separator 301 and the bottom discharge hole of the bag-type dust collector 303 are connected with the feed hole of the pre-reduction fluidized bed feeder 304.
The discharge port of the pre-reduction fluidized bed feeder 304 is connected with the feed port of the pre-reduction fluidized bed body 401, the gas outlet of the pre-reduction fluidized bed body 401 is connected with the inlet of the pre-reduction fluidized bed cyclone separator 403, the gas inlet at the bottom of the pre-reduction fluidized bed body 401 is provided with a pipeline connected with a hydrogen main pipe, the pipeline is provided with the first gas flow regulating valve 405, the discharge port of the pre-reduction fluidized bed body 401 and the discharge port at the bottom of the pre-reduction fluidized bed cyclone separator 403 are connected with the feed port of the pre-reduction fluidized bed discharger 404, and the microwave heating device 402 is arranged around the furnace body of the pre-reduction fluidized bed body 401.
The discharge hole of the pre-reduction fluidized bed discharger 404 is connected with the feed hole of the final reduction fluidized bed body 501, the gas outlet of the final reduction fluidized bed body 501 is connected with the inlet of the final reduction fluidized bed cyclone separator 503, the gas inlet at the bottom of the final reduction fluidized bed body 501 is provided with a pipeline connected with a hydrogen header pipe, the pipeline is provided with the second gas flow regulating valve 505, the gas outlet of the final reduction fluidized bed cyclone separator 503 is connected with the inlet of the high-temperature dust collector 6, the discharge hole of the final reduction fluidized bed body 501 and the bottom discharge hole of the final reduction fluidized bed cyclone separator 503 are connected with the feed hole of the final reduction fluidized bed discharger 504, the discharge hole of the final reduction fluidized bed discharger 504 is connected with the feed hole of the direct reduced iron product bin 7, and the induction heating device 502 is arranged around the furnace body of the final reduction fluidized bed body 501.
The outlet of the tube array inside the gas heat exchanger 8 is connected with the gas inlet of the hydrogen dehydration device 9, the gas inlet of the shell of the gas heat exchanger 8 is connected with the gas outlet of the hydrogen dehydration device 9, and the gas outlet of the shell of the gas heat exchanger 8 is connected with the gas inlet at the bottom of the final reduction fluidized bed body 501.
In this embodiment, the induction heating device 502 is a medium-frequency induction heating device; the high-temperature dust remover 6 is a metal dust remover; the first gas flow regulating valve 405, the second gas flow regulating valve 505, the third gas flow regulating valve 601 and the fourth gas flow regulating valve 602 are all hydrogen one-way flow regulating valves; the hydrogen dehydration device 9 is a spray tower dehydration device.
The process flow diagram of the method for producing iron by direct reduction of hydrogen heated by electric energy according to the embodiment is shown in fig. 1, and the method comprises the following specific steps:
iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2 to exchange heat with reduction tail gas from a first cyclone separator 301, then enters the first cyclone separator 301 to exchange heat with the reduction tail gas from a pre-reduction fluidized bed cyclone separator 403, and then enters a pre-reduction fluidized bed body 401 together with powder collected by a bag-type dust collector 303 through a pre-reduction fluidized bed feeder 304, hydrogen from a main pipeline is mixed through a first gas flow regulating valve 405 and water vapor-containing hydrogen from a high-temperature dust collector 6 through a third gas flow regulating valve 601 to form reduction gas, the reduction gas enters the pre-reduction fluidized bed body 401, and the volume fraction of water vapor in the reduction gas introduced into the pre-reduction fluidized bed body 401 is regulated to be 4% through the first gas flow regulating valve 405 and the third gas flow regulating valve 601; simultaneously, a microwave heating device 402 is started, the temperature in the pre-reduction fluidized bed body 401 is controlled to be 600 ℃, hydrogen and iron ore powder are fully contacted and subjected to reduction reaction to obtain a pre-reduction product with the metallization rate of 40%, pre-reduction tail gas enters a pre-reduction fluidized bed cyclone separator 403 through an upper gas outlet of the pre-reduction fluidized bed body 401, is separated, enters a first cyclone separator 301 through a gas outlet of the pre-reduction fluidized bed cyclone separator 403, and then enters an inner tube nest of a gas heat exchanger 8 after powder is removed through a second cyclone separator 302 and a bag-type dust collector 303; the pre-reduction product discharged from the discharge port at the lower part of the pre-reduction fluidized bed body 401 and the powder separated by the pre-reduction cyclone 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The total iron mass percent of the iron ore powder used in the embodiment is 65%, the particle size range is 0.05-0.5 mm, the average retention time of the iron ore powder in the fluidized bed is 60min, and the operation gas velocity is 2m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.5MW.
hydrogen from a main pipeline is mixed with hydrogen from the shell of the gas heat exchanger 8 through a second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, the induction heating device 502 is started at the same time, the temperature in the final reduction fluidized bed body 501 is controlled to be 650 ℃, the hydrogen is fully contacted with pre-reduced iron ore powder materials and is subjected to reduction reaction, direct reduced iron with the metallization rate of 93.8% is obtained, reduced tail gas enters the final reduction fluidized bed cyclone separator 503 through the upper gas outlet of the final reduction fluidized bed body 501, is separated and then enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone separator 503, the reduced tail gas after dust removal enters a tube in the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 through a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601 respectively, and dust is discharged and collected; the direct reduced iron discharged from the discharge outlet at the lower part of the final reduction fluidized bed body 501 and the powder separated by the final reduction cyclone 503 enter the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504. In the embodiment, the average retention time of the pre-reduced material of the iron ore powder in the fluidized bed is 60min, and the operation gas velocity is 2m/s; the induction heating device is a medium-frequency induction heating device, the heating frequency of the medium-frequency induction heating device is 350Hz, and the output power of the medium-frequency induction heating device is 0.8MW.
And 3, dehydration treatment and recycling of the reduction tail gas:
the reduction tail gas entering the tube array inside the gas heat exchanger 8 contains water vapor, the reduction tail gas is further cooled by the heat exchanger and then enters the hydrogen dehydration device 9 through the tube array gas outlet for dehydration treatment, the condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the reduction tail gas after dehydration is hydrogen, the reduction tail gas after dehydration enters the shell of the gas heat exchanger 8 through the gas outlet of the hydrogen dehydration device 9, and the reduction tail gas after heat exchange by the heat exchanger enters the final reduction fluidized bed body 501 through the gas outlet of the shell of the gas heat exchanger 8 to be recycled as reduction gas.
Example 2
The structure of the electric-heating hydrogen direct reduction iron-making device is similar to that of the embodiment 1, and the difference is that the high-temperature dust remover 6 is a ceramic dust remover, and the hydrogen dehydration device 9 is a molecular sieve and freeze dehydration combined device.
The embodiment of the invention provides an iron making method by directly reducing hydrogen heated by electric energy, which comprises the following specific steps:
iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2 to exchange heat with reduction tail gas from a first cyclone separator 301, then enters the first cyclone separator 301 to exchange heat with reduction tail gas from a pre-reduction fluidized bed cyclone separator 403, and then enters a pre-reduction fluidized bed body 401 together with powder collected by a bag-type dust collector 303 through a pre-reduction fluidized bed feeder 304, hydrogen from a main pipeline is mixed through a first gas flow regulating valve 405 and water-containing steam hydrogen from a high-temperature dust collector 6 through a third gas flow regulating valve 601 to form reduction gas, the reduction gas enters the pre-reduction fluidized bed body 401 together, and the volume fraction of the water steam in the reduction gas introduced into the pre-reduction fluidized bed body 401 is regulated to be 3.5% through the first gas flow regulating valve 405 and the third gas flow regulating valve 601; simultaneously, the microwave heating device 402 is started, the temperature in the pre-reduction fluidized bed body 401 is controlled to be 620 ℃, hydrogen and iron ore powder are fully contacted and subjected to reduction reaction to obtain a pre-reduction product with the metallization rate of 41%, pre-reduction tail gas enters the pre-reduction fluidized bed cyclone separator 403 through an upper gas outlet of the pre-reduction fluidized bed body 401, is separated, enters the first cyclone separator 301 through a gas outlet of the pre-reduction fluidized bed cyclone separator 403, and then enters an inner tube nest of the gas heat exchanger 8 after powder is removed through the second cyclone separator 302 and the bag-type dust collector 303; the pre-reduction product discharged from the discharge outlet at the lower part of the pre-reduction fluidized bed body 401 and the powder separated by the pre-reduction cyclone separator 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The total iron mass percent of the iron ore powder used in the embodiment is 63.5%, the particle size range is 0.03-0.5 mm, the average retention time of the iron ore powder in the fluidized bed is 65min, and the operation gas velocity is 2.1m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.6MW.
hydrogen from a main pipeline is mixed with hydrogen from a shell of a gas heat exchanger 8 through a second gas flow regulating valve 505 to form reducing gas, the reducing gas enters a final reduction fluidized bed body 501, an induction heating device 502 is started at the same time, the temperature in the final reduction fluidized bed body 501 is controlled to be 660 ℃, the hydrogen is fully contacted with pre-reduced iron ore powder materials and subjected to reduction reaction, direct reduced iron with the metallization rate of 93% is obtained, reduced tail gas enters a final reduction fluidized bed cyclone separator 503 through an upper gas outlet of the final reduction fluidized bed body 501, is separated and then enters a high-temperature dust remover 6 through a gas outlet of the final reduction fluidized bed cyclone separator 503, the reduced tail gas after dust removal enters a tube in the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 through a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601 respectively, and dust is discharged and collected; the direct reduced iron discharged from the discharge opening at the lower part of the final reduction fluidized bed body 501 and the powder separated by the final reduction cyclone 503 enter the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504. In the embodiment, the average residence time of the iron ore powder pre-reduced material in the fluidized bed is 70min, and the operation gas velocity is 2.1m/s; the induction heating device is a medium-frequency induction heating device, the heating frequency of the medium-frequency induction heating device is 300Hz, and the output power of the medium-frequency induction heating device is 0.85MW.
And 3, dehydration treatment and recycling of the reduction tail gas:
the reduction tail gas entering the tube nest inside the gas heat exchanger 8 contains water vapor, after being further cooled by the heat exchanger, the reduction tail gas enters the hydrogen dehydration device 9 through the tube nest gas outlet for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the reduction tail gas after dehydration is hydrogen, the hydrogen enters the shell of the gas heat exchanger 8 through the gas outlet of the hydrogen dehydration device 9, and the reduction tail gas enters the final reduction fluidized bed body 501 through the gas outlet of the shell of the gas heat exchanger 8 after heat exchange of the heat exchanger for recycling as reduction gas.
Example 3
The electric energy heated hydrogen direct reduction iron making device of the embodiment is the same as the embodiment 1.
The embodiment of the invention provides an iron making method by directly reducing hydrogen heated by electric energy, which comprises the following specific steps:
iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2 to exchange heat with reduction tail gas from a first cyclone separator 301, then enters the first cyclone separator 301 to exchange heat with reduction tail gas from a pre-reduction fluidized bed cyclone separator 403, and then enters a pre-reduction fluidized bed body 401 together with powder collected by a bag-type dust collector 303 through a pre-reduction fluidized bed feeder 304, hydrogen from a main pipeline is mixed through a first gas flow regulating valve 405 and water-containing steam hydrogen from a high-temperature dust collector 6 through a third gas flow regulating valve 601 to form reduction gas, the reduction gas enters the pre-reduction fluidized bed body 401 together, and the volume fraction of the water steam in the reduction gas introduced into the pre-reduction fluidized bed body 401 is regulated to be 2% through the first gas flow regulating valve 405 and the third gas flow regulating valve 601; simultaneously, a microwave heating device 402 is started, the temperature in the pre-reduction fluidized bed body 401 is controlled to be 630 ℃, hydrogen and iron ore powder are fully contacted and subjected to reduction reaction to obtain a pre-reduction product with the metallization rate of 43%, pre-reduction tail gas enters the pre-reduction fluidized bed cyclone separator 403 through an upper gas outlet of the pre-reduction fluidized bed body 401, is separated, enters the first cyclone separator 301 through a gas outlet of the pre-reduction fluidized bed cyclone separator 403, and then enters an inner tube nest of the gas heat exchanger 8 after powder is removed through the second cyclone separator 302 and the bag-type dust collector 303; the pre-reduction product discharged from the discharge outlet at the lower part of the pre-reduction fluidized bed body 401 and the powder separated by the pre-reduction cyclone separator 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The total iron mass percent of the iron ore powder used in the embodiment is 67.2%, the particle size range is 0.05-0.6 mm, the average retention time of the iron ore powder in the fluidized bed is 40min, and the operation gas velocity is 2.2m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.7MW.
hydrogen from a main pipeline is mixed with hydrogen from a shell of a gas heat exchanger 8 through a second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, the induction heating device 502 is started at the same time, the temperature in the final reduction fluidized bed body 501 is controlled to be 670 ℃, the hydrogen is fully contacted with pre-reduced iron ore powder materials and is subjected to reduction reaction, direct reduced iron with the metallization rate of 95.3% is obtained, reduced tail gas enters a final reduction fluidized bed cyclone separator 503 through an upper gas outlet of the final reduction fluidized bed body 501, is separated and then enters a high-temperature dust remover 6 through a gas outlet of the final reduction fluidized bed cyclone separator 503, the reduced tail gas after dust removal enters a tube in the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 through a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601 respectively, and dust is discharged and collected; the direct reduced iron discharged from the discharge outlet at the lower part of the final reduction fluidized bed body 501 and the powder separated by the final reduction cyclone 503 enter the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504. In the embodiment, the average retention time of the pre-reduced material of the iron ore powder in the fluidized bed is 65min, and the operation gas velocity is 2.2m/s; the induction heating device is a medium-frequency induction heating device, the heating frequency of the medium-frequency induction heating device is 280Hz, and the output power of the medium-frequency induction heating device is 0.9MW.
And 3, dehydration treatment and recycling of the reduction tail gas:
the reduction tail gas entering the tube array inside the gas heat exchanger 8 contains water vapor, the reduction tail gas is further cooled by the heat exchanger and then enters the hydrogen dehydration device 9 through the tube array gas outlet for dehydration treatment, the condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the reduction tail gas after dehydration is hydrogen, the reduction tail gas after dehydration enters the shell of the gas heat exchanger 8 through the gas outlet of the hydrogen dehydration device 9, and the reduction tail gas after heat exchange by the heat exchanger enters the final reduction fluidized bed body 501 through the gas outlet of the shell of the gas heat exchanger 8 to be recycled as reduction gas.
Example 4
The electric energy heated hydrogen direct reduction iron making device of the embodiment is the same as the embodiment 1.
The embodiment of the invention provides an iron making method by directly reducing hydrogen heated by electric energy, which comprises the following specific steps:
iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2 to exchange heat with reduction tail gas from a first cyclone separator 301, then enters the first cyclone separator 301 to exchange heat with reduction tail gas from a pre-reduction fluidized bed cyclone separator 403, and then enters a pre-reduction fluidized bed body 401 together with powder collected by a bag-type dust collector 303 through a pre-reduction fluidized bed feeder 304, hydrogen from a main pipeline is mixed through a first gas flow regulating valve 405 and water-containing steam hydrogen from a high-temperature dust collector 6 through a third gas flow regulating valve 601 to form reduction gas, the reduction gas enters the pre-reduction fluidized bed body 401 together, and the volume fraction of the water steam in the reduction gas introduced into the pre-reduction fluidized bed body 401 is regulated to be 1% through the first gas flow regulating valve 405 and the third gas flow regulating valve 601; simultaneously, a microwave heating device 402 is started, the temperature in the pre-reduction fluidized bed body 401 is controlled to be 625 ℃, hydrogen and iron ore powder are fully contacted and subjected to reduction reaction to obtain a pre-reduction product with the metallization rate of 45%, pre-reduction tail gas enters the pre-reduction fluidized bed cyclone separator 403 through an upper gas outlet of the pre-reduction fluidized bed body 401, is separated, enters the first cyclone separator 301 through a gas outlet of the pre-reduction fluidized bed cyclone separator 403, is subjected to powder removal through the second cyclone separator 302 and the bag-type dust collector 303, and then enters an inner tube array of the gas heat exchanger 8; the pre-reduction product discharged from the discharge port at the lower part of the pre-reduction fluidized bed body 401 and the powder separated by the pre-reduction cyclone 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The total iron mass percent of the iron ore powder used in the embodiment is 69%, the particle size range is 0.02-0.55 mm, the average retention time of the iron ore powder in the fluidized bed is 30min, and the operation gas velocity is 2.2m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.68MW.
hydrogen from a main pipeline is mixed with hydrogen from a shell of a gas heat exchanger 8 through a second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, the induction heating device 502 is started at the same time, the temperature in the final reduction fluidized bed body 501 is controlled to be 670 ℃, the hydrogen is fully contacted with pre-reduced iron ore powder materials and is subjected to reduction reaction, direct reduced iron with the metallization rate of 96.5% is obtained, reduced tail gas enters a final reduction fluidized bed cyclone separator 503 through an upper gas outlet of the final reduction fluidized bed body 501, is separated and then enters a high-temperature dust remover 6 through a gas outlet of the final reduction fluidized bed cyclone separator 503, the reduced tail gas after dust removal enters a tube in the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 through a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601 respectively, and dust is discharged and collected; the direct reduced iron discharged from the discharge outlet at the lower part of the final reduction fluidized bed body 501 and the powder separated by the final reduction cyclone 503 enter the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504. In the embodiment, the average residence time of the iron ore powder pre-reduced material in the fluidized bed is 90min, and the operation gas velocity is 2.2m/s; the induction heating device is a medium-frequency induction heating device, the heating frequency of the medium-frequency induction heating device is 250Hz, and the output power of the medium-frequency induction heating device is 0.95MW.
And 3, dehydration treatment and recycling of the reduction tail gas:
the reduction tail gas entering the tube array inside the gas heat exchanger 8 contains water vapor, the reduction tail gas is further cooled by the heat exchanger and then enters the hydrogen dehydration device 9 through the tube array gas outlet for dehydration treatment, the condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the reduction tail gas after dehydration is hydrogen, the reduction tail gas after dehydration enters the shell of the gas heat exchanger 8 through the gas outlet of the hydrogen dehydration device 9, and the reduction tail gas after heat exchange by the heat exchanger enters the final reduction fluidized bed body 501 through the gas outlet of the shell of the gas heat exchanger 8 to be recycled as reduction gas.
The method can be realized by upper and lower limit values and interval values of intervals of process parameters (such as temperature, time and the like), and embodiments are not listed.
Conventional technical knowledge in the art can be used for the details which are not described in the present invention.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and are not limited. Although the present invention has been described in detail with reference to the embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (8)
1. An electric energy heated hydrogen direct reduction iron making method comprises the following specific steps:
step 1, preheating and prereducing iron ore powder:
iron ore powder enters a second cyclone separator (302) from an iron ore powder bin (1) through a screw feeder (2) to exchange heat with reduction tail gas from a first cyclone separator (301), then enters the first cyclone separator (301) to exchange heat with the reduction tail gas from a pre-reduction fluidized bed cyclone separator (403), and then enters a pre-reduction fluidized bed body (401) together with powder collected by a bag-type dust collector (303) through a pre-reduction fluidized bed feeder (304), hydrogen from a main pipeline is mixed with water vapor-containing hydrogen from a high-temperature dust collector (6) through a first gas flow regulating valve (405) to form reduction gas and enters the pre-reduction fluidized bed body (401) together through a third gas flow regulating valve (601), and the volume fraction of the water vapor in the reduction gas introduced into the pre-reduction fluidized bed body (401) is controlled through the first gas flow regulating valve (405) and the third gas flow regulating valve (601); simultaneously, starting a microwave heating device (402), controlling the reaction temperature in the pre-reduction fluidized bed body (401), and fully contacting hydrogen with iron ore powder to carry out a reduction reaction to obtain a pre-reduction product with a certain metallization rate; the pre-reduction tail gas enters a pre-reduction fluidized bed cyclone separator (403) through an upper gas outlet of a pre-reduction fluidized bed body (401), is separated and then enters a first cyclone separator (301) through a gas outlet of the pre-reduction fluidized bed cyclone separator (403), and then enters a tube array in the gas heat exchanger (8) after powder is removed by a second cyclone separator (302) and a bag-type dust collector (303); a pre-reduction product discharged from a discharge hole at the lower part of the pre-reduction fluidized bed body (401) and powder obtained by separation of the pre-reduction cyclone separator (403) enter the interior of the final reduction fluidized bed body (501) through a pre-reduction fluidized bed discharger (404);
step 2, final reduction of the pre-reduced iron ore powder:
hydrogen from a main pipeline is mixed with hydrogen from a shell of a gas heat exchanger (8) through a second gas flow regulating valve (505) to form reducing gas, the reducing gas enters a final reduction fluidized bed body (501) together, meanwhile, an induction heating device (502) is started, the reaction temperature in the final reduction fluidized bed body (501) is controlled, the hydrogen is fully contacted with pre-reduced iron ore powder materials and undergoes reduction reaction to obtain direct reduced iron, reduced tail gas enters a final reduction fluidized bed cyclone separator (503) through an upper gas outlet of the final reduction fluidized bed body (501), the reduced tail gas is separated and then enters a high-temperature dust remover (6) through a gas outlet of the final reduction fluidized bed cyclone separator (503), the reduced tail gas after dust removal enters a column pipe and the pre-reduction fluidized bed body (401) in the gas heat exchanger (8) through a fourth gas flow regulating valve (602) and a third gas flow regulating valve (601), and dust is discharged and collected; the direct reduced iron discharged from a discharge outlet at the lower part of the final reduction fluidized bed body (501) and the powder separated by the final reduction cyclone separator (503) enter a direct reduced iron product bin (7) through a final reduction fluidized bed discharger (504);
step 3, dehydration treatment and recycling of the reduction tail gas:
the reduction tail gas entering the tube nest in the gas heat exchanger (8) contains water vapor, the reduction tail gas is further cooled through the heat exchanger and then enters the hydrogen dehydration device (9) through the tube nest gas outlet for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device (9), the reduction tail gas after dehydration is hydrogen, the reduction tail gas enters the shell of the gas heat exchanger (8) through the gas outlet of the hydrogen dehydration device (9), and the reduction tail gas enters the final reduction fluidized bed body (501) through the gas outlet of the shell of the gas heat exchanger (8) after heat exchange through the heat exchanger and is recycled as reduction gas.
2. The method as claimed in claim 1, wherein in step 1, the total iron content of the iron ore powder is 63-69% by mass, and the particle size is 0.02-0.6mm; the reduction temperature of the iron ore powder in the pre-reduction fluidized bed body (401) is 600-630 ℃, the average residence time is 30-65mm, the volume fraction of water vapor in the reduction gas is 1% -4%, the operation gas velocity is 2-2.2m/s, and the metallization rate of the pre-reduction product is 40% -45%.
3. The method of making iron by direct reduction of hydrogen gas heated by electric energy as claimed in claim 1, wherein in step 2, the reduction temperature of pre-reduced iron ore powder in the final reduction fluidized bed body (501) is 650-670 ℃, the average residence time is 60-90mm, the operation gas velocity is 2-2.2m/s, and the metallization rate of direct reduced iron is 93-96.5%.
4. The method for ironmaking by direct reduction of hydrogen heated by electric energy as claimed in claim 1 or 2, characterized in that the microwave heating device (402) is arranged around the furnace body of the pre-reduction fluidized bed body (401), the heating frequency of the microwave heating device (402) is 2.45GHz, and the output power is 0.5-1.0MW.
5. The method for ironmaking by direct reduction of hydrogen heated by electric energy according to claim 1 or 3, characterized in that the induction heating device (502) is arranged around the furnace body of the final reduction fluidized bed body (501), the induction heating device (502) is a medium frequency induction heating device, the heating frequency is 150-350Hz, and the output power is 0.1-1.0MW.
6. The method of claim 1, wherein the high temperature dust collector (6) is a metal dust collector or a ceramic dust collector.
7. The method as claimed in any one of claims 1 to 6, wherein the first gas flow regulating valve (405), the second gas flow regulating valve (505), the third gas flow regulating valve (601) and the fourth gas flow regulating valve (602) are all hydrogen one-way flow regulating valves.
8. An electric energy heated hydrogen direct reduction iron making method according to any one of the claims 1-6, characterized in that the hydrogen dehydration device (9) is one or a combination of a spray tower dehydration device, a molecular sieve dehydration device and a freezing dehydration device.
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