WO2023173632A1 - 一种氢基竖炉生产直接还原铁的方法及装置 - Google Patents

一种氢基竖炉生产直接还原铁的方法及装置 Download PDF

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WO2023173632A1
WO2023173632A1 PCT/CN2022/104515 CN2022104515W WO2023173632A1 WO 2023173632 A1 WO2023173632 A1 WO 2023173632A1 CN 2022104515 W CN2022104515 W CN 2022104515W WO 2023173632 A1 WO2023173632 A1 WO 2023173632A1
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gas
shaft furnace
hydrogen
carbon
reduced iron
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PCT/CN2022/104515
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English (en)
French (fr)
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吴开基
何学坤
张涛
郑军
李佳楣
翟晓波
王全乐
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中冶赛迪工程技术股份有限公司
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Publication of WO2023173632A1 publication Critical patent/WO2023173632A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]

Definitions

  • the invention belongs to the technical field of metallurgical industry and relates to a method and device for producing direct reduced iron in a hydrogen-based shaft furnace.
  • the Direct Reduced Iron (DRI) process is an important link in realizing the short process of steel production, that is, the scrap steel/direct reduced iron-electric furnace process. Compared with the traditional blast furnace ironmaking process, the direct reduction ironmaking process, especially the gas-based direct reduction process, has a more significant carbon emission reduction effect.
  • the gas-based shaft furnace process generally uses natural gas reforming to produce reducing gas mainly composed of H2 and CO to achieve direct reduction of iron and top coal gas in the upper part of the shaft furnace.
  • the generated carbon oxides, such as CO and CO2 are basically mixed with methane by partially recycling CO2, and there is also a partial CO2 exhaust system.
  • the object of the present invention is to provide a method and device for producing direct reduced iron in a hydrogen-based shaft furnace to solve the problem of high carbon emissions in the prior art when producing direct reduced iron in a gas-based shaft furnace.
  • a method for producing direct reduced iron in a hydrogen-based shaft furnace including:
  • the CO2 gas is pressurized and mixed with the input H2 gas
  • the decarbonized gas and the carbon-containing hydrogen-rich gas are mixed, and the supplementary hydrocarbon gas is mixed again to obtain the shaft furnace reducing gas;
  • the shaft furnace reducing gas is input into the gas-based shaft furnace to produce direct reduced iron.
  • decarbonizing the top gas includes washing and dehydrating the top gas.
  • the mixed CO2 gas and H2 gas are subjected to a water gas reverse reaction to obtain the carbon-containing and hydrogen-rich gas.
  • the step also includes:
  • the carbon-containing and hydrogen-rich gas is heat exchanged, and the obtained waste heat is input into the water gas reverse reaction;
  • the carbon-containing hydrogen-rich gas is dehydrated.
  • hydrocarbon gas includes at least one of the following: natural gas, liquefied petroleum gas.
  • the molar fraction ratio of the input H2 gas and the CO2 gas is 1.5 to 5.0.
  • the temperature at which the mixed CO2 gas and H2 gas are subjected to the water gas reverse reaction is 200°C to 900°C.
  • the volume percentage of H2 is 40% to 55%, the volume percentage of CO is 15% to 30%, the volume percentage of H2O is 15% to 30%, and the volume percentage of CO2 is 15% to 30%. 0% to 10%.
  • a device for producing direct reduced iron in a hydrogen-based shaft furnace including:
  • a decarbonization system used to decarbonize the furnace top gas and output CO2 gas and decarbonized gas
  • the first mixing system is used to pressurize the CO2 gas and mix it with the input H2 gas;
  • a water-gas reverse reaction system for performing a water-gas reverse reaction on the mixed CO2 gas and H2 gas to obtain carbon-containing hydrogen-rich gas, where the carbon-containing hydrogen-rich gas includes H2, CO and H2O;
  • the second mixing system is used to mix the decarbonized gas and the carbon-containing hydrogen-rich gas, and mix the supplementary hydrocarbon gas again to obtain shaft furnace reducing gas;
  • An output system is used to input the shaft furnace reducing gas into the gas-based shaft furnace to produce direct reduced iron.
  • a gas purification and washing system is also provided at the output end of the gas-based shaft furnace, and the gas purification and washing system is used to wash and dehydrate the top gas.
  • the output end of the water-gas reverse reaction system is provided with a heat exchange system.
  • the heat exchange system is used to exchange heat for the carbon-containing and hydrogen-rich gas, and the waste heat obtained is input into the water-gas reverse reaction.
  • the process flow system only needs to add a small amount of hydrocarbon gas to maintain the balance of the shaft furnace DRI carburizing demand and the circulating reducing gas.
  • the process flow layout is simple and the energy consumption is low.
  • Figure 1 is a schematic flow diagram of a method for producing direct reduced iron in a hydrogen-based shaft furnace in the present invention
  • Figure 2 is a schematic structural diagram of a device for producing direct reduced iron in a hydrogen-based shaft furnace in the present invention.
  • Figure 1 shows a method for producing direct reduced iron in a hydrogen-based shaft furnace, including:
  • S4 Perform water-gas reverse reaction on the mixed CO2 gas and H2 gas to obtain carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas includes H2, CO and H2O;
  • the supplementary hydrogen is mixed with the carbon dioxide produced during the internal circulation process, and the water gas reverse reaction is used to achieve the modification and transformation of the carbon in the shaft furnace process, thereby realizing the internal recycling of carbon.
  • the furnace process is more green and low-carbon, with obvious environmental benefits; the process system only needs to add a small amount of hydrocarbon gas to maintain the balance of the shaft furnace DRI carburizing demand and circulating reducing gas.
  • the process layout is simple and the energy consumption is low. .
  • the top gas is decarbonized, which includes: washing and dehydrating the top gas.
  • the mixed CO2 gas and H2 gas are subjected to a water gas reverse reaction to obtain the carbon-containing and hydrogen-rich gas.
  • the step also includes:
  • the carbon-containing and hydrogen-rich gas is heat exchanged, and the obtained waste heat is input into the water gas reverse reaction;
  • the carbon-containing hydrogen-rich gas is dehydrated.
  • hydrocarbon gas includes at least one of the following: natural gas, liquefied petroleum gas.
  • the molar fraction ratio of the input H2 gas and the CO2 gas is 1.5 to 5.0.
  • the pressure for supplementing H2 is ⁇ 1.0MPa (gauge pressure);
  • the pressure of CO2 gas after pressurization is ⁇ 1.0MPa (gauge pressure);
  • the mixed gas passes through a water gas reverse reaction system to generate carbon-containing and hydrogen-rich gas with H2, CO and H2O as main components.
  • the main chemical reaction of the water-gas reverse reaction system is H2(g)+CO2(g) ⁇ CO(g)+H2O(g);
  • the temperature requirement of the water gas reverse reaction system is 200°C ⁇ 900°C;
  • the total conversion rate of CO2 in the water-gas reverse reaction system is >50%.
  • the temperature at which the mixed CO2 gas and H2 gas are subjected to the water gas reverse reaction is 200°C to 900°C.
  • the volume percentage of H2 is 40% to 55%, the volume percentage of CO is 15% to 30%, the volume percentage of H2O is 15% to 30%, and the volume percentage of CO2 is 15% to 30%. 0% to 10%.
  • the H2 content is 55% to 70% (volume percentage)
  • the CO content is 20% to 35%% (volume percentage)
  • the temperature is 30 to 40°C.
  • H2O is released in the form of free water and reused.
  • the carbon-containing and hydrogen-rich gas passes through the heat exchange system, it is mixed with the decarbonized gas output from the gas decarbonization system, and mixed with the pressure-regulated and pre-processed supplementary H2 and supplementary NG input from the interface end of the shaft furnace system. Finally, the shaft furnace reducing gas is formed.
  • the supplementary NG is required to be NG or LPG (liquefied petroleum gas) from which impurities have been removed;
  • the reducing gas of the shaft furnace is passed into the tubular heating furnace to be heated up. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI. After heating, the temperature of the reducing gas is 850 ⁇ 1050°C, and the pressure of the reducing gas entering the shaft furnace is 0.2MPa ⁇ 1.0Mpa (gauge pressure).
  • the by-product CO2 gas output from the top gas discharged from the top of the shaft furnace after purification, washing and gas decarbonization systems has a CO2 content of >90% (volume percentage) and a CO2 pressure range of 0.05MPa to 0.9MPa (table pressure), the temperature of CO2 is 30 ⁇ 40°C.
  • gas decarbonization system is a dry decarbonization device or a wet decarbonization device.
  • the decarbonized gas output from the gas decarbonization system has an H2 content of 70% to 90% (volume percentage), a CO content of 8% to 25% (volume percentage), and an H2O content of 0% to 1% (volume percentage). Volume percentage), the temperature is 30 ⁇ 40°C.
  • the process route is:
  • the top gas discharged from the top of the shaft furnace is purified and washed, and the by-product CO2 gas output by the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the mixed gas passes through the water gas reverse reaction system to generate H2, CO and H2O is the main component of carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas is mixed with the decarbonized gas output from the gas decarbonization system and mixed with the adjusted gas input from the interface end of the shaft furnace system.
  • a shaft furnace reducing gas is formed.
  • the shaft furnace reducing gas is passed into the tubular heating furnace to be heated. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI.
  • a device for producing direct reduced iron in a hydrogen-based shaft furnace including:
  • a decarbonization system used to decarbonize the furnace top gas and output CO2 gas and decarbonized gas
  • the first mixing system is used to pressurize the CO2 gas and mix it with the input H2 gas;
  • a water-gas reverse reaction system for performing a water-gas reverse reaction on the mixed CO2 gas and H2 gas to obtain carbon-containing hydrogen-rich gas, where the carbon-containing hydrogen-rich gas includes H2, CO and H2O;
  • the second mixing system is used to mix the decarbonized gas and the carbon-containing hydrogen-rich gas, supplement the H2, and mix the hydrocarbon gas again to obtain shaft furnace reduction gas;
  • An output system is used to heat the shaft furnace reducing gas through a tubular heating furnace and then input it into the gas-based shaft furnace to produce direct reduced iron.
  • a gas purification and washing system is also provided at the output end of the gas-based shaft furnace, and the gas purification and washing system is used to wash and dehydrate the top gas.
  • the output end of the water-gas reverse reaction system is provided with a heat exchange system.
  • the heat exchange system is used to exchange heat for the carbon-containing and hydrogen-rich gas, and the waste heat obtained is input into the water-gas reverse reaction.
  • the top gas discharged from the top of the shaft furnace is purified and washed, and the by-product CO2 gas output by the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the mixed gas passes through the water gas reverse reaction system to generate H2, CO and H2O is the main component of carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas is mixed with the decarbonized gas output from the gas decarbonization system and mixed with the adjusted gas input from the interface end of the shaft furnace system.
  • a shaft furnace reducing gas is formed.
  • the shaft furnace reducing gas is passed into the tubular heating furnace to be heated. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI.
  • the by-product CO2 gas output from the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the pressure of the CO2 gas after pressurization is 1.0 MPa (gauge pressure)
  • the mole fraction ratio of the supplemented H2 and CO2 is 3.0
  • the pressure of the supplemented H2 is 1.0 MPa (gauge pressure).
  • the mixed gas passes through the water gas reverse reaction system to generate carbon-containing and hydrogen-rich gas with H2, CO and H2O as the main components.
  • the working temperature in the water-gas reverse reaction system is 480°C.
  • the cycle conversion rate of CO2 in the system is 90.5%.
  • the components of the generated carbon-containing hydrogen-rich gas are H2: 52.6% (volume percentage), CO: 22.5% (volume percentage), H2O (g): 22.54%, residual CO2 content is 2.0%.
  • the temperature is 33°C
  • the H2 content is 67.50% (volume percentage)
  • the CO content is 28.90% (volume percentage)
  • the residual CO2 content is 3.0%.
  • the purity of the pressure-regulated and pre-treated supplementary H2 input from the interface end of the shaft furnace system is 99.9%, the pressure is 1.0MPa (gauge pressure), and the supplementary NG is liquefied petroleum gas.
  • the reducing gas of the shaft furnace is passed into the tubular heating furnace to heat up.
  • the temperature of the reduced gas after heating is 900°C, and the reducing gas pressure is 0.3MPa (gauge pressure).
  • the output by-product CO2 gas content is 99.8% (volume percentage)
  • the temperature is 33°C
  • the gauge pressure is ⁇ 0.05MPa.
  • the gas decarbonization system is a wet method. Decarbonization device.
  • the decarbonized gas output from the coal gas decarbonization system has a temperature of 33°C, an H2 content of 87.6% (volume percentage), a CO content of 9.7% (volume percentage), a CO2 content of 0.2% (volume percentage), and a H2O content of ⁇ 1% ( volume percentage).
  • the top gas discharged from the top of the shaft furnace is purified and washed, and the by-product CO2 gas output by the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the mixed gas passes through the water gas reverse reaction system to generate H2, CO and H2O is the main component of carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas is mixed with the decarbonized gas output from the gas decarbonization system and mixed with the adjusted gas input from the interface end of the shaft furnace system.
  • a shaft furnace reducing gas is formed.
  • the shaft furnace reducing gas is passed into the tubular heating furnace to be heated. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI.
  • the by-product CO2 gas output from the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the pressure of the CO2 gas after pressurization is 1.0 MPa (gauge pressure)
  • the mole fraction ratio of the supplemented H2 and CO2 is 3.0
  • the pressure of the supplemented H2 is 1.0 MPa (gauge pressure).
  • the mixed gas passes through the water gas reverse reaction system to generate carbon-containing and hydrogen-rich gas with H2, CO and H2O as the main components.
  • the working temperature in the water-gas reverse reaction system is 520°C.
  • the cycle conversion rate of CO2 in the system is 91.5%.
  • the components of the generated carbon-containing hydrogen-rich gas are H2: 54.50% (volume percentage), CO: 17.50% (volume percentage), H2O (g): 17.50%, and the residual CO2 content is 7.50%.
  • the temperature is 38°C
  • the H2 content is 69.4% (volume percentage)
  • the CO content is 21.1% (volume percentage)
  • the residual CO2 content is 9.0%.
  • the purity of the pressure-regulated and pre-treated supplementary H2 input from the interface end of the shaft furnace system is 99.9%, the pressure is 1.0MPa (gauge pressure), and the supplementary NG is NG from which impurities have been removed.
  • the reducing gas of the shaft furnace is passed into the tubular heating furnace to heat up.
  • the temperature of the reduced gas after heating is 900°C, and the reducing gas pressure is 0.3MPa (gauge pressure).
  • the output by-product CO2 gas has a content of 99.7% (volume percentage), a temperature of 36°C, a gauge pressure of ⁇ 0.05MPa, and the gas decarbonization system is a wet method. Decarbonization device.
  • the decarbonized gas output from the coal gas decarbonization system has a temperature of 36°C, an H2 content of 86.61% (volume percentage), a CO content of 12.41% (volume percentage), a CO2 content of 0.3% (volume percentage), and a H2O content of 0.7% (volume percentage). percentage).
  • the top gas discharged from the top of the shaft furnace is purified and washed, and the by-product CO2 gas output by the gas decarbonization system is mixed with H2 after pressure treatment.
  • the mixed gas passes through the water gas reverse reaction system to generate H2, CO and H2O is the main component of carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas is mixed with the decarbonized gas output from the gas decarbonization system, and then mixed with the adjusted gas input from the interface end of the shaft furnace system.
  • a shaft furnace reducing gas is formed.
  • the shaft furnace reducing gas is passed into the tubular heating furnace to be heated. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI.
  • the by-product CO2 gas output from the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the pressure of the CO2 gas after pressurization is 1.0 MPa (gauge pressure)
  • the mole fraction ratio of the supplemented H2 and CO2 is 3.0
  • the pressure of the supplemented H2 is 1.0 MPa (gauge pressure).
  • the mixed gas passes through the water gas reverse reaction system to generate carbon-containing and hydrogen-rich gas with H2, CO and H2O as the main components.
  • the working temperature in the water-gas reverse reaction system is 520°C.
  • the cycle conversion rate of CO2 in the system is 92%.
  • the components of the generated carbon-containing hydrogen-rich gas are H2: 57.57% (volume percentage), CO: 17.47% (volume percentage), H2O (g): 17.47%, residual CO2 content is 7.4%.
  • the temperature is 34°C
  • the H2 content is 69.51% (volume percentage)
  • the CO content is 21.09% (volume percentage)
  • the residual CO2 content is 8.9%.
  • the purity of the pressure-regulated and pre-treated supplementary H2 input from the interface end of the shaft furnace system is 99.9%, the pressure is 1.0MPa (gauge pressure), and the supplementary NG is NG from which impurities have been removed.
  • the reducing gas of the shaft furnace is passed into the tubular heating furnace to heat up.
  • the temperature of the reduced gas after heating is 900°C, and the reducing gas pressure is 0.3MPa (gauge pressure).
  • the output by-product CO2 gas has a content of 99.6% (volume percentage), a temperature of 35°C, a gauge pressure of ⁇ 0.05MPa, and the gas decarbonization system is a wet method. Decarbonization device.
  • the decarbonized gas output from the coal gas decarbonization system has a temperature of 35°C, an H2 content of 82.5% (volume percentage), a CO content of 16.4% (volume percentage), a CO2 content of 0.4% (volume percentage), and a H2O content of 0.7% (volume percentage). percentage).
  • the top gas discharged from the top of the shaft furnace is purified and washed, and the by-product CO2 gas output by the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the mixed gas passes through the water gas reverse reaction system to generate H2, CO and H2O is the main component of carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas is mixed with the decarbonized gas output from the gas decarbonization system and mixed with the adjusted gas input from the interface end of the shaft furnace system.
  • a shaft furnace reducing gas is formed.
  • the shaft furnace reducing gas is passed into the tubular heating furnace to be heated. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI.
  • the by-product CO2 gas output from the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the pressure of the CO2 gas after pressurization treatment is 1.0 MPa (gauge pressure)
  • the mole fraction ratio of the supplemented H2 and CO2 is 2.0
  • the pressure of the supplemented H2 is 1.0 MPa (gauge pressure).
  • the mixed gas passes through the water gas reverse reaction system to generate carbon-containing and hydrogen-rich gas with H2, CO and H2O as the main components.
  • the working temperature in the water-gas reverse reaction system is 500°C.
  • the cycle conversion rate of CO2 in the system is 90%.
  • the components of the generated carbon-containing hydrogen-rich gas are H2: 43.33% (volume percentage), CO: 23.3% (volume percentage), H2O (g): 23.3%, residual CO2 content is 10.0%.
  • the temperature is 35°C
  • the H2 content is 56.31% (volume percentage)
  • the CO content is 30.32% (volume percentage)
  • the residual CO2 content is 12.9%.
  • the purity of the pressure-regulated and pre-treated supplementary H2 input from the interface end of the shaft furnace system is 99.9%, the pressure is 1.0MPa (gauge pressure), and the supplementary NG is liquefied petroleum gas.
  • the reducing gas of the shaft furnace is passed into the tubular heating furnace to heat up.
  • the temperature of the reduced gas after heating is 900°C, and the reducing gas pressure is 0.3MPa (gauge pressure).
  • the output by-product CO2 gas has a content of 99.4% (volume percentage), a temperature of 35°C, a gauge pressure of ⁇ 0.06MPa, and the gas decarbonization system is a wet method. Decarbonization device.
  • the decarbonized gas output from the coal gas decarbonization system has a temperature of 35°C, an H2 content of 74.12% (volume percentage), a CO content of 24.57% (volume percentage), a CO2 content of 0.6% (volume percentage), and a H2O content of 0.7% (volume percentage). percentage).
  • the top gas discharged from the top of the shaft furnace is purified and washed, and the by-product CO2 gas output by the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the mixed gas passes through the water gas reverse reaction system to generate H2, CO and H2O is the main component of carbon-containing and hydrogen-rich gas.
  • the carbon-containing and hydrogen-rich gas is mixed with the decarbonized gas output from the gas decarbonization system and mixed with the adjusted gas input from the interface end of the shaft furnace system.
  • a shaft furnace reducing gas is formed.
  • the shaft furnace reducing gas is passed into the tubular heating furnace to be heated. After rising to a certain temperature, the reducing gas enters the shaft furnace to produce DRI.
  • the by-product CO2 gas output from the gas decarbonization system is mixed with supplementary H2 after pressure treatment.
  • the pressure of the CO2 gas after pressurization treatment is 1.0 MPa (gauge pressure)
  • the mole fraction ratio of the supplemented H2 and CO2 is 1.6
  • the pressure of the supplemented H2 is 1.0 MPa (gauge pressure).
  • the mixed gas passes through the water gas reverse reaction system to generate carbon-containing and hydrogen-rich gas with H2, CO and H2O as the main components.
  • the working temperature in the water-gas reverse reaction system is 500°C.
  • the cycle conversion rate of CO2 in the system is 88%.
  • the components of the generated carbon-containing hydrogen-rich gas are H2: 33.63% (volume percentage), CO: 27.3% (volume percentage), H2O (g): 27.3%, the residual CO2 content is 11.7%.
  • the temperature is 35°C
  • the H2 content is 46.10% (volume percentage)
  • the CO content is 37.47% (volume percentage)
  • the residual CO2 content is 16.06%.
  • the purity of the pressure-regulated and pre-treated supplementary H2 input from the interface end of the shaft furnace system is 99.9%, the pressure is 1.0MPa (gauge pressure), and the supplementary NG is liquefied petroleum gas.
  • the reducing gas of the shaft furnace is passed into the tubular heating furnace to heat up.
  • the temperature of the reduced gas after heating is 900°C, and the reducing gas pressure is 0.3MPa (gauge pressure).
  • the output by-product CO2 gas has a content of 99.4% (volume percentage), a temperature of 35°C, a gauge pressure of ⁇ 0.06MPa, and the gas decarbonization system is a wet method. Decarbonization device.
  • the decarbonized gas output from the coal gas decarbonization system has a temperature of 35°C, an H2 content of 74.12% (volume percentage), a CO content of 24.57% (volume percentage), a CO2 content of 0.6% (volume percentage), and a H2O content of 0.7% (volume percentage). percentage).

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Abstract

本发明涉及一种氢基竖炉生产直接还原铁的方法及装置，属于冶金工业技术领域。所述一种氢基竖炉生产直接还原铁的方法，包括：获取气基竖炉输出的炉顶煤气；将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；将所述CO2气体进行加压后与输入的H2气体进行混合；将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体，所述含碳富氢气体包括H2、CO和H2O；将所述脱碳气体和所述含碳富氢气体进行混合，补充部分碳氢气体再次进行混合，获取竖炉还原气；将所述竖炉还原气输入所述气基竖炉生产直接还原铁。将补充氢气和内循环过程产生的二氧化碳混合，通过水煤气逆反应来达到竖炉流程中碳素的改质变换，实现碳质内循环利用。

Description

一种氢基竖炉生产直接还原铁的方法及装置 技术领域
本发明属于冶金工业技术领域，涉及一种氢基竖炉生产直接还原铁的方法及装置。
背景技术
直接还原炼铁(Direct Reduced Iron，DRI)工艺是实现钢铁生产的短流程，即废钢/直接还原铁-电炉流程的重要环节。与传统的高炉炼铁工艺相比，直接还原炼铁法特别是气基直接还原工艺，其碳减排效果更加显著。
作为目前世界上最为典型应用的直接还原炼铁技术，气基竖炉工艺一般是采用天然气重整的方法来制取以H2和CO为主的还原气，实现直接还原铁，竖炉上部顶煤气产生的碳氧化物，如CO和CO2，基本上采用部分回用CO2的方式和甲烷进行混合，另有部分CO2外排系统。
发明内容
有鉴于此，本发明的目的在于提供一种氢基竖炉生产直接还原铁的方法及装置，用于解决现有技术中气基竖炉生产直接还原铁时碳排放高的问题。
为达到上述目的，本发明提供如下技术方案：
一种氢基竖炉生产直接还原铁的方法，包括：
获取气基竖炉输出的炉顶煤气；
将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；
将所述CO2气体进行加压后与输入的H2气体进行混合；
将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体，所述含碳富氢气体包括H2、CO和H2O；
将所述脱碳气体和所述含碳富氢气体进行混合，补充碳氢气体再次进行混合，获取竖炉还原气；
将所述竖炉还原气输入所述气基竖炉生产直接还原铁。
可选的，将所述炉顶煤气进行脱碳处理，之前包括：将所述炉顶煤气进行洗涤脱水。
可选的，将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体的步骤之后还包括：
对所述含碳富氢气体进行换热，获取的余热输入所述水煤气逆反应；
对所述含碳富氢气体进行脱水处理。
可选的，碳氢气体至少包括以下之一：天然气、液化石油气。
可选的，将所述CO2气体进行加压后与输入的H2气体进行混合的步骤中，输入的所述H2气体和所述CO2气体的摩尔分率比例为1.5～5.0。
可选的，将混合后的CO2气体和H2气体进行水煤气逆反应的温度为200℃～900℃。
可选的，在所述含碳富氢气中，H2的体积百分比为40％～55％，CO的体积百分比为15％～30％，H2O的体积百分比为15％～30％，CO2的体积百分比为0％～10％。
一种氢基竖炉生产直接还原铁的装置，包括：
气基竖炉，用于输出炉顶煤气；
脱碳系统，用于将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；
第一混合系统，用于将所述CO2气体进行加压后与输入的H2气体进行混合；
水煤气逆反应系统，用于将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体，所述含碳富氢气体包括H2、CO和H2O；
第二混合系统，用于将所述脱碳气体和所述含碳富氢气体进行混合，补充碳氢气体再次进行混合，获取竖炉还原气；
输出系统，用于将所述竖炉还原气输入所述气基竖炉生产直接还原铁。
可选的，在所述气基竖炉的输出端还设有煤气净化洗涤系统，所述煤气净化洗涤系统用于将所述炉顶煤气进行洗涤脱水。
可选的，所述水煤气逆反应系统的输出端设有换热系统，所述换热系统用于对所述含碳富氢气体进行换热，获取的余热输入所述水煤气逆反应。
本发明的有益效果在于：
1、将补充氢气和内循环过程产生的二氧化碳混合，通过水煤气逆反应来达到竖炉流程中碳素的改质变换，实现碳质内循环利用，过程无碳氧化物外排，相比传统的气基竖炉工艺流程更加绿色和低碳，环保效益明显。
2、工艺流程系统只需补充少量的碳氢气体来维持竖炉DRI渗碳需求量及循环还原气平衡即可，工艺流程布置简单，能耗较低。
本发明的其他优点、目标和特征在某种程度上将在随后的说明书中进行阐述，并且在某种程度上，基于对下文的考察研究对本领域技术人员而言将是显而易见的，或者可以从本发明的实践中得到教导。本发明的目标和其他优点可以通过下面的说明书来实现和获得。
附图说明
为了使本发明的目的、技术方案和优点更加清楚，下面将结合附图对本发明作优选的详细描述，其中：
图1为本发明中一种氢基竖炉生产直接还原铁的方法的流程示意图；
图2为本发明中一种氢基竖炉生产直接还原铁的装置的结构示意图。
具体实施方式
以下通过特定的具体实例说明本发明的实施方式，本领域技术人员可由本说明书所揭露的内容轻易地了解本发明的其他优点与功效。本发明还可以通过另外不同的具体实施方式加以实施或应用，本说明书中的各项细节也可以基于不同观点与应用，在没有背离本发明的精神下进行各种修饰或改变。需要说明的是，以下实施例中所提供的图示仅以示意方式说明本发明的基本构想，在不冲突的情况下，以下实施例及实施例中的特征可以相互组合。
其中，附图仅用于示例性说明，表示的仅是示意图，而非实物图，不能理解为对本发明的限制；为了更好地说明本发明的实施例，附图某些部件会有省略、放大或缩小，并不代表实际产品的尺寸；对本领域技术人员来说，附图中某些公知结构及其说明可能省略是可以理解的。
本发明实施例的附图中相同或相似的标号对应相同或相似的部件；在本发明的描述中，需要理解的是，若有术语“上”、“下”、“左”、“右”、“前”、“后”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此附图中描述位置关系的用语仅用于示例性说明，不能理解为对本发明的限制，对于本领域的普通技术人员而言，可以根据具体情况理解上述术语的具体含义。
请参阅图1，为一种氢基竖炉生产直接还原铁的方法，包括：
S1：获取气基竖炉输出的炉顶煤气；
S2：将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；
S3：将所述CO2气体进行加压后与输入的H2气体进行混合；
S4：将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体，所述含碳富氢气体包括H2、CO和H2O；
S5：将所述脱碳气体和所述含碳富氢气体进行混合，补充碳氢气体再次进行混合，获取竖炉还原气；
S6：将所述竖炉还原气输入所述气基竖炉生产直接还原铁。
将补充氢气和内循环过程产生的二氧化碳混合，通过水煤气逆反应来达到竖炉流程中碳素的改质变换，实现碳质内循环利用，过程无碳氧化物外排，相比传统的气基竖炉工艺流程更加绿色和低碳，环保效益明显；工艺流程系统只需补充少量的碳氢气体来维持竖炉DRI渗碳需求量及循环还原气平衡即可，工艺流程布置简单，能耗较低。
在一些实施过程中，将所述炉顶煤气进行脱碳处理，之前包括：将所述炉顶煤气进行洗涤脱水。
可选的，将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体的步骤之后还包括：
对所述含碳富氢气体进行换热，获取的余热输入所述水煤气逆反应；
对所述含碳富氢气体进行脱水处理。
可选的，碳氢气体至少包括以下之一：天然气、液化石油气。
可选的，将所述CO2气体进行加压后与输入的H2气体进行混合的步骤中，输入的所述H2气体和所述CO2气体的摩尔分率比例为1.5至5.0。又例如，补充H2的压力≥1.0MPa(表压)；
经加压处理后的CO2气体，压力≥1.0MPa(表压)；
进一步，所述混合后的煤气经过水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体。
水煤气逆反应系统的主要化学反应为H2(g)+CO2(g)→CO(g)+H2O(g)；
水煤气逆反应系统温度要求为200℃～900℃；
水煤气逆反应系统CO2的总转化率＞50％。
可选的，将混合后的CO2气体和H2气体进行水煤气逆反应的温度为200℃～900℃。
可选的，在所述含碳富氢气中，H2的体积百分比为40％～55％，CO的体积百分比为15％～30％，H2O的体积百分比为15％～30％，CO2的体积百分比为0％～10％。进一步，所述含碳富氢气体经换热系统后，H2的含量为55％～70％(体积百分比)，CO的含量为20％～35％％(体积百分比)，温度为30～40℃，H2O以游离水形态脱出并回用。所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理的补充H2、补充NG混合后，形成竖炉还原气。
要求补充H2的纯度＞99.9％；
要求补充NG为脱除杂质的NG或LPG(液化石油气)；
进一步，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入竖炉生产DRI。升温后还原气温度为850～1050℃，还原气进入竖炉压力为0.2MPa～1.0Mpa(表压)。
进一步，所述竖炉顶部排出的炉顶煤气经由净化洗涤、煤气脱碳系统后输出的副产CO2气体，CO2的含量＞90％(体积百分比)，CO2的压力范围0.05MPa～0.9MPa(表压)，CO2的温度为30～40℃。
进一步，所述煤气脱碳系统为干法脱碳装置或湿法脱碳装置。
进一步，所述煤气脱碳系统后输出的脱碳气，H2的含量70％～90％(体积百分比)，CO含量为8％～25％(体积百分比)，H2O含量为0％～1％(体积百分比)，温度为30～40℃。
在一些实施过程中，其工艺路线为：
竖炉顶部排出的炉顶煤气经净化洗涤、煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合，混合后的煤气经过水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体，所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理的补充H2、补充天然气混合后，形成竖炉还原气，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入竖炉生产DRI。
请参阅图2，提供一种氢基竖炉生产直接还原铁的装置，包括：
气基竖炉，用于输出炉顶煤气；
脱碳系统，用于将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；
第一混合系统，用于将所述CO2气体进行加压后与输入的H2气体进行混合；
水煤气逆反应系统，用于将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体，所述含碳富氢气体包括H2、CO和H2O；
第二混合系统，用于将所述脱碳气体和所述含碳富氢气体进行混合，补充部分H2、碳氢气体再次进行混合，获取竖炉还原气；
输出系统，用于将所述竖炉还原气经管式加热炉加热后，输入所述气基竖炉生产直接还原铁。
可选的，在所述气基竖炉的输出端还设有煤气净化洗涤系统，所述煤气净化洗涤系统用于将所述炉顶煤气进行洗涤脱水。
可选的，所述水煤气逆反应系统的输出端设有换热系统，所述换热系统用于对所述含碳富氢气体进行换热，获取的余热输入所述水煤气逆反应。
以下通过具体实施例对本发明的技术方案做进一步阐释：
实施例1：
竖炉顶部排出的炉顶煤气经净化洗涤、煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合，混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体，所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理后的补充H2、补充NG混合后，形成竖炉还原气，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入竖炉生产DRI。
煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合。经加压处理后的CO2气体的压力为1.0MPa(表压)，所述补充H2和CO2的摩尔分率比3.0，所述补充H2的压力为1.0MPa(表压)。
混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体。水煤气逆反应系统内工作温度为480℃，系统中CO2的循环转化率为90.5％，生成的含碳富氢气体的组分为H2：52.6％(体积百分比)，CO：22.5％(体积百分比)，H2O(g)：22.54％，残存CO2的含量为2.0％。
含碳富氢气体经换热系统后，温度为33℃，H2含量为67.50％(体积百分比)，CO含量为28.90％(体积百分比)，残存CO2的含量为3.0％。
竖炉系统界面端输入的经调压及预处理的补充H2纯度为99.9％，压力为1.0MPa(表压)，补充NG为液化石油气。竖炉还原气通入管式加热炉升温，升温后的还原气温度为900℃，还原气压力为0.3MPa(表压)。
竖炉顶部排出的炉顶煤气经过净化洗涤、脱碳系统后，输出的副产CO2气体的含量99.8％(体积百分比)，温度为33℃，表压～0.05MPa，煤气脱碳系统为湿法脱碳装置。
煤气脱碳系统后输出的脱碳气，温度为33℃，H2含量87.6％(体积百分比)，CO含量为9.7％(体积百分比)，CO2含量0.2％(体积百分比)，H2O含量～1％(体积百分比)。
实施例2：
竖炉顶部排出的炉顶煤气经净化洗涤、煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合，混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体，所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理后的补充H2、补充NG混合后，形成竖炉还原气，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入 竖炉生产DRI。
煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合。经加压处理后的CO2气体的压力为1.0MPa(表压)，所述补充H2和CO2的摩尔分率比3.0，所述补充H2的压力为1.0MPa(表压)。
混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体。水煤气逆反应系统内工作温度为520℃，系统中CO2的循环转化率为91.5％，生成的含碳富氢气体的组分为H2：54.50％(体积百分比)，CO：17.50％(体积百分比)，H2O(g)：17.50％，残存CO2的含量为7.50％。
含碳富氢气体经换热系统后，温度为38℃，H2含量为69.4％(体积百分比)，CO含量为21.1％(体积百分比)，残存CO2的含量为9.0％。
竖炉系统界面端输入的经调压及预处理的补充H2纯度为99.9％，压力为1.0MPa(表压)，补充NG为脱除杂质的NG。竖炉还原气通入管式加热炉升温，升温后的还原气温度为900℃，还原气压力为0.3MPa(表压)。
竖炉顶部排出的炉顶煤气经过净化洗涤、脱碳系统后，输出的副产CO2气体的含量99.7％(体积百分比)，温度为36℃，表压～0.05MPa，煤气脱碳系统为湿法脱碳装置。
煤气脱碳系统后输出的脱碳气，温度为36℃，H2含量86.61％(体积百分比)，CO含量为12.41％(体积百分比)，CO2含量0.3％(体积百分比)，H2O含量0.7％(体积百分比)。
实施例3：
竖炉顶部排出的炉顶煤气经净化洗涤、煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合，混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体，所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理后的补充H2、补充NG混合后，形成竖炉还原气，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入竖炉生产DRI。
煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合。经加压处理后的CO2气体的压力为1.0MPa(表压)，所述补充H2和CO2的摩尔分率比3.0，所述补充H2的压力为1.0MPa(表压)。
混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体。水煤气逆反应系统内工作温度为520℃，系统中CO2的循环转化率为92％，生成的含碳富氢气体的组分为H2：57.57％(体积百分比)，CO：17.47％(体积百分比)，H2O(g)：17.47％， 残存CO2的含量为7.4％。
含碳富氢气体经换热系统后，温度为34℃，H2含量为69.51％(体积百分比)，CO含量为21.09％(体积百分比)，残存CO2的含量为8.9％。
竖炉系统界面端输入的经调压及预处理的补充H2纯度为99.9％，压力为1.0MPa(表压)，补充NG为脱除杂质的NG。竖炉还原气通入管式加热炉升温，升温后的还原气温度为900℃，还原气压力为0.3MPa(表压)。
竖炉顶部排出的炉顶煤气经过净化洗涤、脱碳系统后，输出的副产CO2气体的含量99.6％(体积百分比)，温度为35℃，表压～0.05MPa，煤气脱碳系统为湿法脱碳装置。
煤气脱碳系统后输出的脱碳气，温度为35℃，H2含量82.5％(体积百分比)，CO含量为16.4％(体积百分比)，CO2含量0.4％(体积百分比)，H2O含量0.7％(体积百分比)。
实施例4：
竖炉顶部排出的炉顶煤气经净化洗涤、煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合，混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体，所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理后的补充H2、补充NG混合后，形成竖炉还原气，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入竖炉生产DRI。
煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合。经加压处理后的CO2气体的压力为1.0MPa(表压)，所述补充H2和CO2的摩尔分率比2.0，所述补充H2的压力为1.0MPa(表压)。
混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体。水煤气逆反应系统内工作温度为500℃，系统中CO2的循环转化率为90％，生成的含碳富氢气体的组分为H2：43.33％(体积百分比)，CO：23.3％(体积百分比)，H2O(g)：23.3％，残存CO2的含量为10.0％。
含碳富氢气体经换热系统后，温度为35℃，H2含量为56.31％(体积百分比)，CO含量为30.32％(体积百分比)，残存CO2的含量为12.9％。
竖炉系统界面端输入的经调压及预处理的补充H2纯度为99.9％，压力为1.0MPa(表压)，补充NG为液化石油气。竖炉还原气通入管式加热炉升温，升温后的还原气温度为900℃，还原气压力为0.3MPa(表压)。
竖炉顶部排出的炉顶煤气经过净化洗涤、脱碳系统后，输出的副产CO2气体的含量99.4％ (体积百分比)，温度为35℃，表压～0.06MPa，煤气脱碳系统为湿法脱碳装置。
煤气脱碳系统后输出的脱碳气，温度为35℃，H2含量74.12％(体积百分比)，CO含量为24.57％(体积百分比)，CO2含量0.6％(体积百分比)，H2O含量0.7％(体积百分比)。
实施例5：
竖炉顶部排出的炉顶煤气经净化洗涤、煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合，混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体，所述含碳富氢气体经换热系统后，和所述煤气脱碳系统后输出的脱碳气进行混合，与竖炉系统界面端输入的经调压及预处理后的补充H2、补充NG混合后，形成竖炉还原气，所述竖炉还原气通入管式加热炉进行升温，升至一定的温度后，还原气进入竖炉生产DRI。
煤气脱碳系统后输出的副产CO2气体，经加压处理后和补充H2进行混合。经加压处理后的CO2气体的压力为1.0MPa(表压)，所述补充H2和CO2的摩尔分率比1.6，所述补充H2的压力为1.0MPa(表压)。
混合后的煤气经水煤气逆反应系统，生成以H2、CO和H2O为主要成分的含碳富氢气体。水煤气逆反应系统内工作温度为500℃，系统中CO2的循环转化率为88％，生成的含碳富氢气体的组分为H2：33.63％(体积百分比)，CO：27.3％(体积百分比)，H2O(g)：27.3％，残存CO2的含量为11.7％。
含碳富氢气体经换热系统后，温度为35℃，H2含量为46.10％(体积百分比)，CO含量为37.47％(体积百分比)，残存CO2的含量为16.06％。
竖炉系统界面端输入的经调压及预处理的补充H2纯度为99.9％，压力为1.0MPa(表压)，补充NG为液化石油气。竖炉还原气通入管式加热炉升温，升温后的还原气温度为900℃，还原气压力为0.3MPa(表压)。
竖炉顶部排出的炉顶煤气经过净化洗涤、脱碳系统后，输出的副产CO2气体的含量99.4％(体积百分比)，温度为35℃，表压～0.06MPa，煤气脱碳系统为湿法脱碳装置。
煤气脱碳系统后输出的脱碳气，温度为35℃，H2含量74.12％(体积百分比)，CO含量为24.57％(体积百分比)，CO2含量0.6％(体积百分比)，H2O含量0.7％(体积百分比)。
最后说明的是，以上实施例仅用以说明本发明的技术方案而非限制，尽管参照较佳实施例对本发明进行了详细说明，本领域的普通技术人员应当理解，可以对本发明的技术方案进行修改或者等同替换，而不脱离本技术方案的宗旨和范围，其均应涵盖在本发明的权利要求范围当中。

Claims (10)

  1. 一种氢基竖炉生产直接还原铁的方法，其特征在于，包括：
    获取气基竖炉输出的炉顶煤气；
    将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；
    将所述CO2气体进行加压后与输入的H2气体进行混合；
    将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体，所述含碳富氢气体包括H2、CO和H2O；
    将所述脱碳气体和所述含碳富氢气体进行混合，补充碳氢气体再次进行混合，获取竖炉还原气；
    将所述竖炉还原气，，输入所述气基竖炉生产直接还原铁。
  2. 根据权利要求1所述的氢基竖炉生产直接还原铁的方法，其特征在于，将所述炉顶煤气进行脱碳处理，之前包括：将所述炉顶煤气进行洗涤脱水。
  3. 根据权利要求1所述的氢基竖炉生产直接还原铁的方法，其特征在于，将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳富氢气体的步骤之后还包括：
    对所述含碳富氢气体进行换热，获取的余热输入所述水煤气逆反应；
    对所述含碳富氢气体进行脱水处理。
  4. 根据权利要求1所述的氢基竖炉生产直接还原铁的方法，其特征在于，碳氢气体至少包括以下之一：天然气、液化石油气。
  5. 根据权利要求1所述的氢基竖炉生产直接还原铁的方法，其特征在于，将所述CO2气体进行加压后与输入的H2气体进行混合的步骤中，输入的所述H2气体和所述CO2气体的摩尔分率比例为1.5至5.0。
  6. 根据权利要求1所述的氢基竖炉生产直接还原铁的方法，其特征在于，将混合后的CO2气体和H2气体进行水煤气逆反应的温度为200℃～900℃。
  7. 根据权利要求1所述的氢基竖炉生产直接还原铁的方法，其特征在于，在所述含碳富氢气中，H2的体积百分比为40％～55％，CO的体积百分比为15％～30％，H2O的体积百分比为15％～30％，CO2的体积百分比为0％～10％。
  8. 一种氢基竖炉生产直接还原铁的装置，其特征在于，包括：
    气基竖炉，用于输出炉顶煤气；
    脱碳系统，用于将所述炉顶煤气进行脱碳处理，输出CO2气体和脱碳气体；
    第一混合系统，用于将所述CO2气体进行加压后与输入的H2气体进行混合；
    水煤气逆反应系统，用于将混合后的CO2气体和H2气体进行水煤气逆反应，获取含碳 富氢气体，所述含碳富氢气体包括H2、CO和H2O；
    第二混合系统，用于将所述脱碳气体和所述含碳富氢气体进行混合，补充碳氢气体再次进行混合，获取竖炉还原气；
    输出系统，用于将所述竖炉还原气输入所述气基竖炉生产直接还原铁。
  9. 根据权利要求8所述的氢基竖炉生产直接还原铁的装置，其特征在于，在所述气基竖炉的输出端还设有煤气净化洗涤系统，所述煤气净化洗涤系统用于将所述炉顶煤气进行洗涤脱水。
  10. 根据权利要求8所述的氢基竖炉生产直接还原铁的装置，其特征在于，所述水煤气逆反应系统的输出端设有换热系统，所述换热系统用于对所述含碳富氢气体进行换热，获取的余热输入所述水煤气逆反应。
PCT/CN2022/104515 2022-03-14 2022-07-08 一种氢基竖炉生产直接还原铁的方法及装置 WO2023173632A1 (zh)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101638702A (zh) * 2009-08-14 2010-02-03 中冶赛迪工程技术股份有限公司 一种煤气作还原气的直接还原工艺出口煤气的回用方法
CN103146866A (zh) * 2013-04-03 2013-06-12 中冶赛迪工程技术股份有限公司 利用ch4非催化转化生产海绵铁的直接还原工艺
CN106521073A (zh) * 2016-12-16 2017-03-22 江苏省冶金设计院有限公司 一种利用炉顶气制备直接还原铁的系统及方法
CN107058663A (zh) * 2017-03-14 2017-08-18 江苏省冶金设计院有限公司 一种生产直接还原铁的系统及方法
CN114574650A (zh) * 2022-03-14 2022-06-03 中冶赛迪工程技术股份有限公司 一种氢基竖炉生产直接还原铁的方法及装置

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101638702A (zh) * 2009-08-14 2010-02-03 中冶赛迪工程技术股份有限公司 一种煤气作还原气的直接还原工艺出口煤气的回用方法
CN103146866A (zh) * 2013-04-03 2013-06-12 中冶赛迪工程技术股份有限公司 利用ch4非催化转化生产海绵铁的直接还原工艺
CN106521073A (zh) * 2016-12-16 2017-03-22 江苏省冶金设计院有限公司 一种利用炉顶气制备直接还原铁的系统及方法
CN107058663A (zh) * 2017-03-14 2017-08-18 江苏省冶金设计院有限公司 一种生产直接还原铁的系统及方法
CN114574650A (zh) * 2022-03-14 2022-06-03 中冶赛迪工程技术股份有限公司 一种氢基竖炉生产直接还原铁的方法及装置

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