CN115896378B - 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 electric energy heating hydrogen direct reduction ironmaking method, which comprises the following steps: preheating and prereducing iron ore powder, final reduction of prereduced iron ore powder, dewatering treatment of reduction tail gas and cyclic utilization. The pre-reduction of the iron-containing raw material in the pre-reduction fluidized bed and the final reduction in the final reduction fluidized bed are respectively heated by a microwave heating device and an induction heating device, and the reaction temperature of the fluidized bed hydrogen iron making is maintained by utilizing electric energy heating, so that the chemical energy of the hydrogen can be fully utilized, the hydrogen reduction efficiency of the fluidized bed can be ensured, the full hydrogen smelting of the fluidized bed can be realized, the energy consumption of the fluidized bed hydrogen metallurgy process can be effectively reduced, and the economy of the fluidized bed hydrogen metallurgy process can be improved.
Description
Technical Field
The invention belongs to the technical field of ferrous metallurgy, and particularly relates to an electric energy heating hydrogen direct reduction iron-making method.
Background
At present, blast furnace ironmaking is a main process for producing molten iron, the process takes agglomerated sintered ore and pellet ore as main raw materials, takes coke and coal dust as main fuels, and has irreplaceability due to the skeleton action of the coke in the blast furnace, and CO is produced in the blast furnace ironmaking process 2 The emission amount is about the CO of the whole steel industry 2 70% of the emission is the main carbon emission industry. In order to realize the source carbon reduction in the ferrous metallurgy industry, development of a new green low-carbon metallurgy technology is urgently needed. Hydrogen is an excellent reducing agent and clean energy, and the direct reduction iron-making process using the hydrogen substituted carbon as the reducing agent is explored and developed, so that 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 reactor types, 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 direct utilization of fine ore, no sintering or pelletizing process, small mass transfer resistance in the reaction process, high heat transfer and reduction efficiency, low-temperature reduction realization and the like. For the fluidized bed hydrogen iron-making process, as the hydrogen reduced iron oxide is an endothermic reaction, besides heating the iron-containing material to the reaction temperature, enough heat is needed to maintain smooth progress of the reduction reaction in the fluidized bed, and 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 the fact that the amount of hydrogen needed for heat balance is far greater than the amount of hydrogen needed for the reduction reaction, and serious mismatch of physical heat and chemical energy in the fluidized bed is caused, so that the utilization rate of hydrogen is lower. Therefore, the realization of reasonable heat supply and the improvement of the utilization rate of hydrogen are technical bottlenecks which are needed to break through in the development of the fluidized bed hydrogen metallurgy process.
The prior 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 by burning coal gas and air to preheat mineral powder, and the reduction gas enters from a fourth-stage fluidized bed after being preheated and passes through the multistage fluidized beds in series to complete the reduction reaction of the iron mineral powder. The circumored technology takes hydrogen obtained by reforming natural gas as a single reducing agent, preheats mineral powder by using a fluidized bed, prereduces the mineral powder in a first-stage circulating fluidized bed, finally reduces the mineral powder in a second-stage bubbling fluidized bed, and the heat required by the reduction reaction is provided by heating the mineral powder and circulating gas. Patent application CN200580017740.5 discloses a direct reduction apparatus and method employing a two-stage fluidized bed for reducing solid iron ore oxides, wherein heat is generated in a first fluidized bed by reacting solid carbonaceous material with an oxygen-containing gas, metalliferous feed material is reduced in a second fluidized bed, and the heat is supplied to the second fluidized bed by a hot off-gas stream and entrained solids exiting the first fluidized bed. The existing system for directly reducing by adopting the fluidized bed has the problems of poor mineral powder preheating effect, low heat utilization rate and the like because the heat required by reduction is provided by burning carbonaceous fuel, and carbon dioxide is discharged. For the full-hydrogen iron-making process, chemical energy is converted into heat energy by burning hydrogen in a fluidized bed to maintain the reduction reaction, so that the reduction of iron ore powder is easily influenced due to the fact that the local oxidizing atmosphere is too high; the hydrogen is preheated outside the fluidized bed by the hydrogen heater, so that a large amount of circulating hydrogen is needed to meet the heat absorption requirement of the reaction, the energy utilization rate is lower, in addition, the equipment of the hydrogen heater is relatively complex, the manufacturing cost is high, the hydrogen embrittlement phenomenon of metal is easy to occur under the high-temperature condition, and certain potential safety hazard exists. 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.
Currently, conventional electrical 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, has the characteristics of rapid heating, uniform heating, low energy consumption, catalysis on chemical reaction and the like, and the iron ore powder has strong microwave absorption capacity. Patent application number CN202011060962.8 discloses a method and a device for making iron by hydrogen, wherein in the scheme, iron-containing ore is subjected to microwave irradiation in hydrogen or hydrogen-rich gas atmosphere to realize hydrogen-rich or pure hydrogen smelting of the iron-containing ore. In addition to iron ore, the raw materials of the microwave heating furnace disclosed in the above proposal generally contain a certain amount of coal dust with wave absorbing capability, and if no wave absorbing material such as coal dust is added, when the iron-containing furnace burden is reduced into direct reduced iron with high metallization rate by blowing hydrogen into the furnace, the microwave heating is difficult to continue due to the reduction of the wave absorbing material. Patent application number CN202110053605.7 discloses a hydrogen shaft furnace iron making system and method using electric energy for heating, wherein 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 charges 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 treat fine ore, and the disadvantages of high mass transfer resistance, low heat transfer and reduction efficiency and the like exist in the reduction process of iron oxide pellets.
In summary, by using electric energy to heat, the reaction temperature of the fluidized bed hydrogen ironmaking is maintained, the chemical energy of the hydrogen is fully utilized, the hydrogen reduction efficiency of the fluidized bed is ensured, and the key of reducing the energy consumption of the full-hydrogen direct reduction ironmaking and improving the economy of the hydrogen direct reduction ironmaking process is realized.
Disclosure of Invention
The invention aims to provide an electric energy heating hydrogen direct reduction iron making method, by adopting the technical scheme of the invention, the electric energy of clean energy sources can be utilized to continuously supply heat for a fluidized bed reactor, the chemical energy of hydrogen is fully utilized, the fluidized bed full hydrogen smelting is realized, the energy consumption of the hydrogen direct reduction iron making process is reduced, and the economy of the hydrogen direct reduction iron making process is improved.
In order to achieve the above purpose, the technical scheme provided by the invention is as follows:
an electric energy heating hydrogen direct reduction ironmaking method comprises the following steps:
the iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2, exchanges heat with the reducing tail gas from a first cyclone separator 301, then enters the first cyclone separator 301, exchanges heat with the reducing 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 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 reducing gas, and enters the pre-reduction fluidized bed body 401 together, and the volume fraction of water vapor in the reducing 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, a microwave heating device 402 is started, the reaction temperature in the pre-reduction fluidized bed body 401 is controlled, hydrogen fully contacts with iron ore powder and undergoes a reduction reaction, 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, enters a first cyclone separator 301 through a gas outlet of the pre-reduction fluidized bed cyclone separator 403 after being separated, and enters a tube array in the gas heat exchanger 8 after powder is removed through a second cyclone separator 302 and a bag-type dust remover 303; the pre-reduction product discharged from a discharge hole at the lower part of the pre-reduction fluidized bed body 401 and the powder separated by the pre-reduction fluidized bed cyclone 403 enter the final reduction fluidized bed body 501 through a pre-reduction fluidized bed discharger 404;
the hydrogen from the main pipeline is mixed with the hydrogen from the shell of the gas heat exchanger 8 through the second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, meanwhile, the induction heating device 502 is started, the reaction temperature in the final reduction fluidized bed body 501 is controlled, the hydrogen fully contacts with the pre-reduced iron ore powder material and undergoes a reduction reaction to obtain direct reduced iron, the reducing tail gas enters the final reduction fluidized bed cyclone 503 through the upper gas outlet of the final reduction fluidized bed body 501 and enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone 503 after being separated, the reducing tail gas after dust removal enters the inner tube array of the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 respectively through the fourth gas flow regulating valve 602 and the third gas flow regulating valve 601, 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 fluidized bed cyclone 503 enter the direct reduced iron product bin 7 together through the final reduction fluidized bed discharger 504;
the reducing tail gas entering the inner tube array of the gas heat exchanger 8 contains water vapor, the water vapor is further cooled by the heat exchanger, enters the hydrogen dehydration device 9 through the air outlet of the tube array for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the dehydrated reducing tail gas is hydrogen, enters the shell of the gas heat exchanger 8 through the air outlet of the hydrogen dehydration device 9, exchanges heat by the heat exchanger, and enters the final reducing fluidized bed body 501 through the air outlet of the shell of the gas heat exchanger 8 to be recycled as reducing gas.
Further, the total iron mass fraction of the iron ore powder in the step 1 is 63% -69%, and the granularity 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 30-65min, the volume fraction of water vapor in the reduction gas is 1-4%, the operation gas speed is 2-2.2m/s, and the metallization rate of the pre-reduction product is 40-45%.
Further, the reduction temperature of the pre-reduced iron ore powder in the step 2 in the final reduction fluidized bed body 501 is 650-670 ℃, the average residence time is 60-90min, the operation air speed is 2-2.2m/s, and the metallization rate of the direct reduced iron is 93% -96.5%.
Further, the microwave heating device 402 is disposed 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.
Further, the induction heating device 502 is disposed around the furnace body of the final reduction fluidized bed body 501, the induction heating device 502 is an intermediate frequency induction heating device, the heating frequency is 150-350Hz, and the output power is 0.1-1.0MW.
Further, the high-temperature dust remover 6 is a metal dust remover or a ceramic dust remover.
Further, the first gas flow rate adjusting valve 405, the second gas flow rate adjusting valve 505, the third gas flow rate adjusting valve 601 and the fourth gas flow rate adjusting valve 602 are all hydrogen unidirectional flow rate adjusting valves.
Further, the hydrogen dehydration device 9 is one or a combination of a plurality of spray tower dehydration devices, molecular sieve dehydration devices and freeze dehydration devices.
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 heating hydrogen direct reduction iron-making method, which comprises a pre-reduction fluidized bed and a final reduction fluidized bed, wherein 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 used for heating the pre-reduction fluidized bed; the metal product content of the iron ore powder in the final reduction fluidized bed is high, and an induction heating device is used for heating 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, and compared with the prior direct reduction technology, the method has the advantages of high heating speed, uniform heating, effective control of heating conditions, energy utilization rate improvement and process energy consumption reduction, and heat is provided by preheating the ore powder and exchanging heat with high-temperature reducing gas.
(2) The clean electric energy is directly utilized to continuously supply heat for the fluidized bed reactor, the reaction temperature required by hydrogen reduction of iron ore powder in the fluidized bed can be maintained, the heat required by the reduction reaction is supplemented, the problem that the existing hydrogen-rich metallurgical process relies on combustion and heat supply of natural gas, coal gas or coal dust and other carbonaceous fuels is effectively solved, the reduction iron making of pure hydrogen is realized, the emission of carbon dioxide is reduced from the source, and the development direction of green low-carbon iron making is met.
(3) The tail gas of the final reduction fluidized bed is split after passing through a high-temperature dust remover, and part of hydrogen of high-temperature water vapor is mixed with fresh low-temperature hydrogen and sent into a 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 a reduction product with a certain metallization rate obtained 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 of 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 remover are mixed and sent into 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 running cost of equipment is saved.
(4) And a hydrogen dehydration device is arranged to carry out dehydration treatment on the reduced water-containing hydrogen, and the treated hydrogen is directly introduced into a final reduction fluidized bed after passing through a heat exchanger, so that the full-flow cyclic utilization of the hydrogen is realized.
(5) The electric energy heating hydrogen direct reduction ironmaking method has high reducing gas and energy utilization rate, can realize fluidized bed full hydrogen smelting, can effectively reduce the energy consumption of a fluidized bed hydrogen metallurgy process and improve the economy of the fluidized bed hydrogen metallurgy process.
Drawings
FIG. 1 is a schematic flow diagram of an electric energy heated hydrogen direct reduction ironmaking process of the present invention;
fig. 2 is a schematic structural diagram of an electric-energy-heated hydrogen direct reduction ironmaking apparatus according to the present invention.
Wherein: 1. iron ore powder 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; 404. a pre-reduction fluidized bed discharger; 405. a first gas flow regulating valve; 5. final reduction of the fluidized bed; 501. a final reduction 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 present invention, the present invention will be described in detail with reference to the drawings and examples.
Example 1
As shown in fig. 2, the hydrogen direct reduction iron making device heated by electric energy of the embodiment comprises an iron ore powder storage bin 1, a screw feeder 2, an iron ore powder preheater 3, a pre-reduction fluidized bed 4, a final reduction fluidized bed 5, a high-temperature dust remover 6, a direct reduction iron product storage bin 7, a gas heat exchanger 8 and a hydrogen dehydration device 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 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 503, a final reduction fluidized bed discharger 504 and a second gas flow regulating valve 505;
the inside of the gas heat exchanger 8 is provided with a tube array, the gas outlet of the high-temperature dust remover 6 and the gas inlet at the bottom of the pre-reduction fluidized bed body 401 and the inlet of the tube array inside the gas heat exchanger 8 are respectively provided with a pipeline connected with each other, and the pipeline is respectively provided with a fourth gas flow regulating valve 602 and a third gas flow regulating valve 601; 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 port of the iron ore powder bin 1 is connected with the feed port of the spiral feeder 2, the discharge port of the spiral feeder 2 is connected with the inlet of the second cyclone separator 302, the bottom discharge port 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 air outlet of the pre-reduction fluidized bed cyclone separator 403, the air outlet of the first cyclone separator 301 is connected with the inlet of the second cyclone separator 302, the air outlet of the second cyclone separator 302 is connected with the inlet of the bag dust collector 303, the air outlet of the bag dust collector 303 is connected with the inlet of the inner tube of the gas heat exchanger 8, and the bottom discharge port of the first cyclone separator 301 and the bottom discharge port of the bag dust collector 303 are connected with the feed port of the pre-reduction fluidized bed feeder 304.
The discharge gate of prereduction fluidized bed feeder 304 with prereduction fluidized bed body 401's feed inlet is connected, prereduction fluidized bed body 401's gas outlet with prereduction fluidized bed cyclone 403's entry is connected, prereduction fluidized bed body 401's bottom air inlet be equipped with the pipeline that is connected with the hydrogen house steward, the pipeline on set up first gas flow control valve 405, prereduction fluidized bed body 401's discharge gate with prereduction fluidized bed cyclone 403's bottom discharge gate with prereduction fluidized bed discharger 404's feed inlet is connected, prereduction fluidized bed body 401's furnace body is equipped with all around microwave heating device 402.
The discharge gate of pre-reduction fluidized bed discharger 404 with the feed inlet of final reduction fluidized bed body 501 is connected, the gas outlet of final reduction fluidized bed body 501 with the entry of final reduction fluidized bed cyclone 503 is connected, the bottom air inlet of final reduction fluidized bed body 501 is equipped with the pipeline that is connected with the hydrogen house steward, the pipeline on set up second gas flow control valve 505, the gas outlet of final reduction fluidized bed cyclone 503 with the entry of high temperature dust remover 6 is connected, the discharge gate of final reduction fluidized bed body 501 with the bottom discharge gate of final reduction fluidized bed cyclone 503 with the feed inlet of final reduction fluidized bed discharger 504 is connected, the discharge gate of final reduction fluidized bed discharger 504 with the feed inlet of direct reduced iron product feed bin 7 is connected, the furnace body 502 of final reduction fluidized bed body 501 is equipped with all around induction heating device.
The outlet of the inner tube array of the gas heat exchanger 8 is connected with the air inlet of the hydrogen dehydration device 9, the air inlet of the shell of the gas heat exchanger 8 is connected with the air outlet of the hydrogen dehydration device 9, and the air outlet of the shell of the gas heat exchanger 8 is connected with the air inlet at the bottom of the final reduction fluidized bed body 501.
In this embodiment, the induction heating device 502 is an intermediate 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 unidirectional flow regulating valves; the hydrogen dehydration device 9 is a spray tower dehydration device.
The process flow diagram of the electric energy heating hydrogen direct reduction ironmaking method is shown in fig. 1, and the specific steps are as follows:
the iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2, exchanges heat with the reducing tail gas from a first cyclone separator 301, then enters the first cyclone separator 301, exchanges heat with the reducing 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 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 and a third gas flow regulating valve 601 to form reducing gas, and the reducing gas enters the pre-reduction fluidized bed body 401 together, and the volume fraction of water vapor in the reducing 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 is fully contacted with iron ore powder and undergoes a reduction reaction to obtain a pre-reduction product with a metallization rate of 40%, pre-reduction tail gas enters a pre-reduction fluidized bed cyclone 403 through an air outlet at the upper part of the pre-reduction fluidized bed body 401, enters a first cyclone 301 through an air outlet of the pre-reduction fluidized bed cyclone 403 after being separated, and then enters a tube array in a gas heat exchanger 8 after powder is removed through a second cyclone 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 separated by the pre-reduction fluidized bed cyclone 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The iron ore powder used in the embodiment has the total iron mass percentage of 65%, the granularity range of 0.05-0.5 mm, the average residence time of the iron ore powder in the fluidized bed of 60min and the operation gas speed of 2m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.5MW.
the hydrogen from the main pipeline is mixed with the hydrogen from the shell of the gas heat exchanger 8 through the second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, meanwhile, the induction heating device 502 is started, the temperature in the final reduction fluidized bed body 501 is controlled to be 650 ℃, the hydrogen is fully contacted with the pre-reduction iron ore powder material and undergoes a reduction reaction to obtain direct reduced iron with the metallization rate of 93.8%, the reducing tail gas enters the final reduction fluidized bed cyclone 503 through the upper gas outlet of the final reduction fluidized bed body 501, the reducing tail gas enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone 503 after being separated, the reducing tail gas after dust removal enters the inner tube array of the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 respectively through the fourth gas flow regulating valve 602 and the third gas flow regulating valve 601, and dust is discharged and collected; the direct reduced iron discharged from the discharge port at the lower part of the final reduction fluidized bed body 501 enters the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504 together with the powder separated by the final reduction fluidized bed cyclone 503. In the embodiment, the average residence time of the iron ore powder prereduced material in the fluidized bed is 60min, and the operation gas speed is 2m/s; the induction heating device is an intermediate frequency induction heating device, the heating frequency is 350Hz, and the output power is 0.8MW.
the reducing tail gas entering the inner tube array of the gas heat exchanger 8 contains water vapor, the water vapor is further cooled by the heat exchanger, enters the hydrogen dehydration device 9 through the air outlet of the tube array for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the dehydrated reducing tail gas is hydrogen, enters the shell of the gas heat exchanger 8 through the air outlet of the hydrogen dehydration device 9, exchanges heat by the heat exchanger, and enters the final reducing fluidized bed body 501 through the air outlet of the shell of the gas heat exchanger 8 to be recycled as reducing gas.
Example 2
The structure of the electric-heating hydrogen direct reduction ironmaking 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 hydrogen direct reduction iron making method heated by electric energy in the embodiment comprises the following specific steps:
the iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2, exchanges heat with the reducing tail gas from a first cyclone separator 301, then enters the first cyclone separator 301, exchanges heat with the reducing 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 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 reducing gas, and enters the pre-reduction fluidized bed body 401 together, and the volume fraction of the water vapor in the reducing 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, a microwave heating device 402 is started, the temperature in the pre-reduction fluidized bed body 401 is controlled to be 620 ℃, hydrogen is fully contacted with iron ore powder and undergoes a reduction reaction to obtain a pre-reduction product with the metallization rate of 41 percent, pre-reduction tail gas enters a pre-reduction fluidized bed cyclone separator 403 through an air outlet at the upper part of the pre-reduction fluidized bed body 401, enters a first cyclone separator 301 through an air outlet of the pre-reduction fluidized bed cyclone separator 403 after being separated, and then enters a tube array in a gas heat exchanger 8 after powder is removed through 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 separated by the pre-reduction fluidized bed cyclone 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The iron ore powder used in the embodiment has the total iron mass percentage of 63.5%, the granularity range of 0.03-0.5 mm, the average residence time of the iron ore powder in the fluidized bed of 65min and the operation gas velocity of 2.1m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.6MW.
the hydrogen from the main pipeline is mixed with the hydrogen from the shell of the gas heat exchanger 8 through the second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, meanwhile, the induction heating device 502 is started, the temperature in the final reduction fluidized bed body 501 is controlled to be 660 ℃, the hydrogen is fully contacted with the pre-reduction iron ore powder material and undergoes a reduction reaction to obtain direct reduction iron with the metallization rate of 93%, the reduction tail gas enters the final reduction fluidized bed cyclone 503 through the upper gas outlet of the final reduction fluidized bed body 501 and enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone 503 after being separated, the reduction tail gas after dust removal enters the inner tube of the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 respectively through the fourth gas flow regulating valve 602 and the third gas flow regulating valve 601, and dust is discharged and collected; the direct reduced iron discharged from the discharge port at the lower part of the final reduction fluidized bed body 501 enters the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504 together with the powder separated by the final reduction fluidized bed cyclone 503. In the embodiment, the average residence time of the iron ore powder prereduced material in the fluidized bed is 70min, and the operation gas speed is 2.1m/s; the induction heating device is an intermediate frequency induction heating device, the heating frequency is 300Hz, and the output power is 0.85MW.
the reducing tail gas entering the inner tube array of the gas heat exchanger 8 contains water vapor, the water vapor is further cooled by the heat exchanger, enters the hydrogen dehydration device 9 through the air outlet of the tube array for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the dehydrated reducing tail gas is hydrogen, enters the shell of the gas heat exchanger 8 through the air outlet of the hydrogen dehydration device 9, exchanges heat by the heat exchanger, and enters the final reducing fluidized bed body 501 through the air outlet of the shell of the gas heat exchanger 8 to be recycled as reducing gas.
Example 3
An electric energy-heated hydrogen direct reduction iron making device of this embodiment is the same as that of embodiment 1.
The hydrogen direct reduction iron making method heated by electric energy in the embodiment comprises the following specific steps:
the iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2, exchanges heat with the reducing tail gas from a first cyclone separator 301, then enters the first cyclone separator 301, exchanges heat with the reducing 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 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 and a third gas flow regulating valve 601 to form reducing gas, and the reducing gas enters the pre-reduction fluidized bed body 401 together, wherein the volume fraction of water vapor in the reducing 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 is fully contacted with iron ore powder and undergoes a reduction reaction to obtain a pre-reduction product with the metallization rate of 43%, pre-reduction tail gas enters a pre-reduction fluidized bed cyclone separator 403 through an air outlet at the upper part of the pre-reduction fluidized bed body 401, enters a first cyclone separator 301 through an air outlet of the pre-reduction fluidized bed cyclone separator 403 after being separated, and then enters a tube array in a gas heat exchanger 8 after powder is removed through 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 separated by the pre-reduction fluidized bed cyclone 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The iron ore powder used in the embodiment has 67.2 percent of total iron by mass, the granularity range of 0.05-0.6 mm, the average residence time of the iron ore powder in the fluidized bed of 40min and the operation gas speed of 2.2m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.7MW.
the hydrogen from the main pipeline is mixed with the hydrogen from the shell of the gas heat exchanger 8 through the second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, meanwhile, the induction heating device 502 is started, the temperature in the final reduction fluidized bed body 501 is controlled to be 670 ℃, the hydrogen is fully contacted with the pre-reduction iron ore powder material and undergoes a reduction reaction to obtain direct reduced iron with the metallization rate of 95.3%, the reducing tail gas enters the final reduction fluidized bed cyclone 503 through the upper gas outlet of the final reduction fluidized bed body 501, the reducing tail gas enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone 503 after being separated, the reducing tail gas after dust removal enters the inner tube array of the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 respectively through the fourth gas flow regulating valve 602 and the third gas flow regulating valve 601, and dust is discharged and collected; the direct reduced iron discharged from the discharge port at the lower part of the final reduction fluidized bed body 501 enters the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504 together with the powder separated by the final reduction fluidized bed cyclone 503. In the embodiment, the average residence time of the iron ore powder prereduced material in the fluidized bed is 65min, and the operation gas speed is 2.2m/s; the induction heating device is an intermediate frequency induction heating device, the heating frequency is 280Hz, and the output power is 0.9MW.
the reducing tail gas entering the inner tube array of the gas heat exchanger 8 contains water vapor, the water vapor is further cooled by the heat exchanger, enters the hydrogen dehydration device 9 through the air outlet of the tube array for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the dehydrated reducing tail gas is hydrogen, enters the shell of the gas heat exchanger 8 through the air outlet of the hydrogen dehydration device 9, exchanges heat by the heat exchanger, and enters the final reducing fluidized bed body 501 through the air outlet of the shell of the gas heat exchanger 8 to be recycled as reducing gas.
Example 4
An electric energy-heated hydrogen direct reduction iron making device of this embodiment is the same as that of embodiment 1.
The hydrogen direct reduction iron making method heated by electric energy in the embodiment comprises the following specific steps:
the iron ore powder enters a second cyclone separator 302 from an iron ore powder bin 1 through a screw feeder 2, exchanges heat with reducing tail gas from a first cyclone separator 301, then enters the first cyclone separator 301, exchanges heat with reducing 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 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 and a third gas flow regulating valve 601 to form reducing gas, and the reducing gas enters the pre-reduction fluidized bed body 401 together, and the volume fraction of water vapor in the reducing 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 is fully contacted with iron ore powder and undergoes a reduction reaction to obtain a pre-reduction product with the metallization rate of 45%, pre-reduction tail gas enters a pre-reduction fluidized bed cyclone 403 through an air outlet at the upper part of the pre-reduction fluidized bed body 401, enters a first cyclone 301 through an air outlet of the pre-reduction fluidized bed cyclone 403 after being separated, and then enters an inner tube array of a gas heat exchanger 8 after powder is removed through a second cyclone 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 separated by the pre-reduction fluidized bed cyclone 403 enter the final reduction fluidized bed body 501 through the pre-reduction fluidized bed discharger 404. The iron ore powder used in the embodiment has the total iron mass percentage of 69%, the granularity range of 0.02-0.55 mm, the average residence time of the iron ore powder in the fluidized bed of 30min and the operation gas speed of 2.2m/s; the heating frequency of the microwave heating device is 2.45GHz, and the output power is 0.68MW.
the hydrogen from the main pipeline is mixed with the hydrogen from the shell of the gas heat exchanger 8 through the second gas flow regulating valve 505 to form reducing gas, the reducing gas enters the final reduction fluidized bed body 501 together, meanwhile, the induction heating device 502 is started, the temperature in the final reduction fluidized bed body 501 is controlled to be 670 ℃, the hydrogen is fully contacted with the pre-reduction iron ore powder material and undergoes a reduction reaction to obtain direct reduced iron with the metallization rate of 96.5%, the reducing tail gas enters the final reduction fluidized bed cyclone 503 through the upper gas outlet of the final reduction fluidized bed body 501, the reducing tail gas enters the high-temperature dust remover 6 through the gas outlet of the final reduction fluidized bed cyclone 503 after being separated, the reducing tail gas after dust removal enters the inner tube array of the gas heat exchanger 8 and the pre-reduction fluidized bed body 401 respectively through the fourth gas flow regulating valve 602 and the third gas flow regulating valve 601, and dust is discharged and collected; the direct reduced iron discharged from the discharge port at the lower part of the final reduction fluidized bed body 501 enters the direct reduced iron product bin 7 through the final reduction fluidized bed discharger 504 together with the powder separated by the final reduction fluidized bed cyclone 503. In the embodiment, the average residence time of the iron ore powder prereduced material in the fluidized bed is 90min, and the operation gas speed is 2.2m/s; the induction heating device is an intermediate frequency induction heating device, the heating frequency is 250Hz, and the output power is 0.95MW.
the reducing tail gas entering the inner tube array of the gas heat exchanger 8 contains water vapor, the water vapor is further cooled by the heat exchanger, enters the hydrogen dehydration device 9 through the air outlet of the tube array for dehydration treatment, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device 9, the dehydrated reducing tail gas is hydrogen, enters the shell of the gas heat exchanger 8 through the air outlet of the hydrogen dehydration device 9, exchanges heat by the heat exchanger, and enters the final reducing fluidized bed body 501 through the air outlet of the shell of the gas heat exchanger 8 to be recycled as reducing gas.
The method can be realized by the upper and lower limit values of the interval and the interval value of the process parameters (such as temperature, time and the like), and the examples are not necessarily listed here.
The invention may be practiced without these specific details, using any knowledge known in the art.
Finally, it should be noted that the above embodiments are only for illustrating the technical solution of the present invention and are not limiting. Although the present invention has been described in detail with reference to the embodiments, it should be understood by those skilled in the art that modifications and equivalents may be made thereto without departing from the spirit and scope of the present invention, which is intended to be covered by the appended claims.
Claims (8)
1. An electric energy heating hydrogen direct reduction ironmaking method comprises the following specific steps:
step 1, preheating and prereducing iron ore powder:
the iron ore powder enters a second cyclone separator (302) from an iron ore powder bin (1) through a spiral feeder (2) to exchange heat with the reducing tail gas from a first cyclone separator (301), then enters the first cyclone separator (301) to exchange heat with the reducing tail gas from a pre-reducing fluidized bed cyclone separator (403), enters a pre-reducing fluidized bed body (401) together with powder obtained by collecting the powder by a bag dust collector (303) through a pre-reducing fluidized bed feeder (304), and hydrogen from a main pipeline is mixed with steam-containing hydrogen from a high-temperature dust collector (6) through a first gas flow regulating valve (405) and a third gas flow regulating valve (601) to form reducing gas to enter the pre-reducing fluidized bed body (401), and the volume fraction of the water vapor in the reducing gas entering the pre-reducing fluidized bed body (401) is controlled 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 reaction temperature in the pre-reduction fluidized bed body (401) is controlled, hydrogen fully contacts with iron ore powder and undergoes a reduction reaction, 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 air outlet at the upper part of a pre-reduction fluidized bed body (401), enters a first cyclone separator (301) through an air outlet of the pre-reduction fluidized bed cyclone separator (403) after being separated, and then enters an inner tube array of a gas heat exchanger (8) after powder is removed through a second cyclone separator (302) and a bag-type dust remover (303); the pre-reduction product discharged from a discharge hole at the lower part of the pre-reduction fluidized bed body (401) and powder separated by a cyclone separator (403) of the pre-reduction fluidized bed enter the final reduction fluidized bed body (501) through a discharge device (404) of the pre-reduction fluidized bed;
step 2, final reduction of pre-reduced iron ore powder:
the hydrogen from the main pipeline is mixed with the 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, meanwhile, an induction heating device (502) is started to control the reaction temperature in the final reduction fluidized bed body (501), the hydrogen fully contacts with the pre-reduced iron ore powder material and undergoes a reduction reaction to obtain direct reduced iron, the reducing tail gas enters a final reduction fluidized bed cyclone (503) through an upper gas outlet of the final reduction fluidized bed body (501) and enters a high-temperature dust remover (6) through a gas outlet of the final reduction fluidized bed cyclone (503) after being separated, and the reducing tail gas after dust removal enters a tube in the gas heat exchanger (8) and the pre-reduction fluidized bed body (401) respectively through a fourth gas flow regulating valve (602) and a third gas flow regulating valve (601) and is discharged and collected; the direct reduced iron discharged from a discharge hole at the lower part of the final reduction fluidized bed body (501) and the powder separated by a final reduction fluidized bed cyclone separator (503) enter a direct reduced iron product bin (7) together through a final reduction fluidized bed discharger (504);
step 3, dehydration treatment and cyclic utilization of the reduction tail gas:
the reduction tail gas entering the inner tube array of the gas heat exchanger (8) contains water vapor, the water vapor enters the hydrogen dehydration device (9) through the tube array air outlet for dehydration after being cooled further through the heat exchanger, condensed water is discharged through the condensed water outlet of the hydrogen dehydration device (9), the dehydrated reduction tail gas is hydrogen, enters the shell of the gas heat exchanger (8) through the air outlet of the hydrogen dehydration device (9), and enters the final reduction fluidized bed body (501) through the air outlet of the shell of the gas heat exchanger (8) after heat exchange through the heat exchanger to be recycled as reduction gas.
2. The direct reduction iron making method by using hydrogen heated by electric energy according to claim 1, wherein in the step 1, the total iron mass fraction of the iron ore powder is 63% -69%, and the grain 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 30-65min, the volume fraction of water vapor in the reduction gas is 1-4%, the operation gas speed is 2-2.2m/s, and the metallization rate of the pre-reduction product is 40-45%.
3. The method for direct reduction iron making with hydrogen heated by electric energy according to claim 1, characterized in that in 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 residence time is 60-90min, the operation air speed is 2-2.2m/s, and the metallization rate of the direct reduced iron is 93% -96.5%.
4. The direct reduction ironmaking method by using electric energy for heating hydrogen according to claim 1 or 2, wherein 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. An electric energy heated direct reduction iron making method using hydrogen as described in claim 1 or 3, wherein said induction heating device (502) is disposed around the furnace body of said final reduction fluidized bed body (501), said induction heating device (502) is an intermediate frequency induction heating device, the heating frequency is 150-350Hz, and the output power is 0.1-1.0MW.
6. An electric energy heated direct reduction ironmaking method by hydrogen according to claim 1, characterized in that the high temperature dust remover (6) is a metal dust remover or a ceramic dust remover.
7. The direct reduction ironmaking method by using hydrogen heated by electric energy according to claim 1, 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 unidirectional flow regulating valves.
8. The direct reduction ironmaking method by using hydrogen heated by electric energy according to claim 1, wherein the hydrogen dehydration device (9) is one or a combination of a plurality of spray tower dehydration devices, molecular sieve dehydration devices and freeze dehydration devices.
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| CN1754966A (en) * | 2004-09-27 | 2006-04-05 | 孔凡逸 | Process for preparing reduced iron by microwave fluidized bed |
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| KR101321928B1 (en) * | 2012-05-16 | 2013-10-28 | 주식회사 포스코 | Apparatus for manufacturing molten irons and method for manufacturing molten irons using the same |
| CN103667571B (en) * | 2013-12-31 | 2015-06-03 | 中国科学院过程工程研究所 | System and method of fluidized direct reduction of iron ore concentrate powder |
| CN103725819B (en) * | 2013-12-31 | 2015-06-03 | 中国科学院过程工程研究所 | Iron ore powder fluidized reduction system and method |
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| EP3670676A1 (en) * | 2018-12-17 | 2020-06-24 | Primetals Technologies Austria GmbH | Method and device for direct reduction with electrically heated reducing gas |
| CN210215430U (en) * | 2019-06-25 | 2020-03-31 | 贺州学院 | Zero-carbon-emission steelmaking equipment |
| CN110423854B (en) * | 2019-08-30 | 2020-11-06 | 东北大学 | Electric energy full-hydrogen flash reduction direct steelmaking system and process |
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