CN117904376A - Hydrogen metallurgy method and system for absorbing secondary energy of steel plant and application of hydrogen metallurgy method and system - Google Patents
Hydrogen metallurgy method and system for absorbing secondary energy of steel plant and application of hydrogen metallurgy method and system Download PDFInfo
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- CN117904376A CN117904376A CN202311802928.7A CN202311802928A CN117904376A CN 117904376 A CN117904376 A CN 117904376A CN 202311802928 A CN202311802928 A CN 202311802928A CN 117904376 A CN117904376 A CN 117904376A
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 745
- 239000001257 hydrogen Substances 0.000 title claims abstract description 740
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 713
- 238000000034 method Methods 0.000 title claims abstract description 287
- 229910000831 Steel Inorganic materials 0.000 title claims abstract description 72
- 239000010959 steel Substances 0.000 title claims abstract description 72
- 238000005272 metallurgy Methods 0.000 title claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 1783
- 238000010438 heat treatment Methods 0.000 claims abstract description 205
- 238000003795 desorption Methods 0.000 claims abstract description 203
- 238000005261 decarburization Methods 0.000 claims abstract description 194
- 239000000571 coke Substances 0.000 claims abstract description 158
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 153
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 83
- 229910052742 iron Inorganic materials 0.000 claims abstract description 76
- 238000003723 Smelting Methods 0.000 claims abstract description 68
- 238000007664 blowing Methods 0.000 claims abstract description 36
- 238000005262 decarbonization Methods 0.000 claims abstract description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 26
- 230000009467 reduction Effects 0.000 claims abstract description 25
- 238000004064 recycling Methods 0.000 claims abstract description 22
- 238000002156 mixing Methods 0.000 claims abstract description 11
- 239000000428 dust Substances 0.000 claims description 188
- 239000002737 fuel gas Substances 0.000 claims description 100
- 230000008569 process Effects 0.000 claims description 80
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 36
- 229910052760 oxygen Inorganic materials 0.000 claims description 36
- 239000001301 oxygen Substances 0.000 claims description 36
- 238000009628 steelmaking Methods 0.000 claims description 30
- 238000000605 extraction Methods 0.000 claims description 28
- 150000002431 hydrogen Chemical class 0.000 claims description 28
- 238000001465 metallisation Methods 0.000 claims description 15
- 239000000110 cooling liquid Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000010521 absorption reaction Methods 0.000 description 115
- 239000000126 substance Substances 0.000 description 76
- 239000000498 cooling water Substances 0.000 description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 238000002407 reforming Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 210000001015 abdomen Anatomy 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 230000000153 supplemental effect Effects 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000005255 carburizing Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000010310 metallurgical process Methods 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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Abstract
The invention discloses a hydrogen metallurgy method and system for absorbing secondary energy of a steel plant and application thereof. The method comprises the following steps: extracting hydrogen from coke oven gas to obtain hydrogen and a first desorption gas, and blowing the first desorption gas into a blast furnace to perform low-carbon smelting; decarburizing the converter gas to obtain converter decarburization gas and a second desorption gas; decarburizing and denitrifying a part of top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas; decarburizing a portion of the blast furnace top gas to obtain a blast furnace decarburization gas and a fourth stripping gas; mixing hydrogen and recycle gas, and mixing with converter decarbonization gas and/or blast furnace decarbonization gas to be used as hydrogen-based shaft furnace reduction gas for producing sponge iron. The system comprises a coke oven gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a heating furnace, a hydrogen-based shaft furnace, a blast furnace, and further comprises a converter gas treatment unit and/or a blast furnace top gas treatment unit. The invention has important significance for absorbing secondary energy of steel mills, reducing primary energy consumption of the hydrogen-based shaft furnace and reducing carbon emission of the shaft furnace.
Description
Technical Field
The invention relates to the technical field of hydrogen metallurgy, in particular to a hydrogen metallurgy method and system for absorbing secondary energy of a steel mill and application thereof.
Background
Hydrogen metallurgy is the reduction of carbon in metallurgical processes by using hydrogen instead of carbon, thereby achieving the source carbon reduction. Hydrogen metallurgy is mainly divided into two process technologies, namely a hydrogen-rich blast furnace and a hydrogen-based shaft furnace. The hydrogen-rich blast furnace is characterized in that a blast furnace tuyere is used for blowing hydrogen-rich gas (hydrogen, coke oven gas, natural gas, synthetic gas and the like) to a hearth or a furnace body to replace partial CO reduction, so that carbon emission can be reduced. The volume fraction of hydrogen in the reducing gas of the hydrogen-based shaft furnace exceeds 55%, and the hydrogen-based shaft furnace is expected to realize full hydrogen reduction in future. The main processes of the hydrogen-based shaft furnace are MIDREX and HYL-ZR, and the direct reduced iron produced by the two processes accounts for more than 70% of the total global yield.
The reducing gas of the MIDREX process is prepared by carrying out catalytic reforming on natural gas and recycled top gas, and an additional reformer is needed as a reaction vessel. The reducing gas of the HYL-ZR process is prepared by in-situ reforming natural gas and steam under the catalytic action of hot sponge iron in the shaft furnace, and an additional reformer is not needed, but the temperature and the pressure of the entering gas are needed to be increased to improve the thermodynamic and kinetic conditions of the reaction, and higher requirements are put on equipment conditions.
Iron and steel enterprises produce a large amount of byproduct gas each year, including blast furnace gas, coke oven gas and converter gas, wherein the coke oven gas and the converter gas have higher heat values (lower heat values exceed 4000kCal/m 3 and 1500kCal/m 3). The 2022 chinese coke oven gas yield was about 1900 hundred million m 3, the converter gas yield was about 781 hundred million m 3, and more than 80% of these secondary energy sources were used as fuel or for power generation. The coke oven gas contains more than 50% of H 2 and 20% of CH 4,H2 which can be used as the reducing gas of the hydrogen-based shaft furnace, and CH 4 which can be used as the blowing gas of the hydrogen-rich blast furnace. The converter gas contains more than 50% of CO, can be used as supplementary gas for hydrogen-based shaft furnace reduction, and the CO reduction heat release can compensate the heat absorbed by H 2 reduction and can also be used as carburizing agent to increase the carbon content of sponge iron. When CH 4 is injected into the blast furnace, oxygen enrichment operation is needed to control the temperature in the furnace, meanwhile, the content of N 2 in the top gas of the blast furnace is greatly reduced, the CO proportion is greatly increased, and the oxygen enriched gas can also be used as the supplementary gas for reducing the hydrogen-based shaft furnace.
If the reducing gas in the coke oven gas, the converter gas and the hydrogen-rich blast furnace gas can be used for smelting the hydrogen-based shaft furnace, a large amount of secondary energy generated by a steel mill is consumed, the equipment investment of a conversion reforming link required for preparing the reducing gas is reduced, and the process flow of the hydrogen-based shaft furnace is simplified. In addition, if methane in the coke oven gas can be sprayed into the blast furnace for low-carbon smelting, the coke ratio of the blast furnace can be reduced, and the carbon emission can be reduced.
Therefore, it is necessary to develop a hydrogen metallurgy method and a system for absorbing secondary energy of a steel mill, which provide important technical support for recovering the secondary energy of the steel mill, reducing the primary energy consumption of a hydrogen-based shaft furnace and reducing the carbon emission of an iron-making process.
Disclosure of Invention
In view of the above-mentioned drawbacks of the prior art, the present invention aims to provide a hydrogen metallurgy method for absorbing secondary energy of a steel mill, which reduces equipment investment in a reforming process required for preparing a reducing gas, reduces carbon emissions of a hydrogen-based shaft furnace and a hydrogen-rich blast furnace, and also provides a hydrogen metallurgy system without conversion, efficient reduction and carburization.
To achieve the above and other related objects, a first aspect of the present invention provides a hydrogen metallurgy method for consuming secondary energy of a steel mill, comprising:
Carrying out hydrogen extraction treatment on coke oven gas to obtain hydrogen and a first desorption gas, and blowing the first desorption gas into a blast furnace to carry out low-carbon smelting to produce liquid molten iron;
Decarburization treatment is carried out on the converter gas to obtain converter decarburization gas and second stripping gas;
decarburizing and denitrifying a part of top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas;
Decarburizing a part of the blast furnace top gas to obtain blast furnace decarburization gas and fourth stripping gas;
mixing the hydrogen and the recycle gas, and mixing the mixture with the converter decarburization gas and/or the blast furnace decarburization gas to jointly serve as hydrogen-based shaft furnace reducing gas for producing sponge iron.
Further, the second desorption gas is conveyed to a steel mill gas pipe network.
Further, a portion of the third stripping gas is used as a fuel gas (i.e., a second fuel gas) for heating the hydrogen-based shaft furnace reducing gas.
And further, conveying the other part of the third desorption gas to a steel mill gas pipe network.
Further, the fourth stripping gas is delivered to a steelmaking plant for use in the CO 2 steelmaking.
Further, another portion of the hydrogen-based shaft furnace top gas is used as a fuel gas (i.e., a first fuel gas) for heating the hydrogen-based shaft furnace reduction gas; preferably, the other part of the hydrogen-based shaft furnace top gas used as fuel gas for heating the hydrogen-based shaft furnace reducing gas accounts for 12.0-17.1% by volume of the total hydrogen-based shaft furnace top gas.
Further, in the fuel gas, the volume fraction of the third stripping gas is less than or equal to 25% (namely the using amount of the second fuel gas), and the volume fraction of the other part of the top gas of the hydrogen-based shaft furnace is more than or equal to 75% (namely the using amount of the first fuel gas).
Further, the method further comprises: the coke oven gas is purified before being subjected to hydrogen stripping treatment.
Further, the method further comprises: the converter gas is cleaned before it is decarbonized.
Further, the method further comprises: dedusting a portion of the hydrogen-based shaft furnace top gas before it is subjected to a decarbonizing denitrification process and before another portion of the hydrogen-based shaft furnace top gas is used as a fuel gas for heating the hydrogen-based shaft furnace reducing gas; preferably, the mode of dust removal treatment of the top gas of the hydrogen-based shaft furnace comprises coarse dust removal and dry dust removal; more preferably, the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3.
Further, the method further comprises: before decarburizing a part of blast furnace top gas, carrying out dust removal treatment on the blast furnace top gas; preferably, the way of dust removal treatment of blast furnace top gas comprises coarse dust removal and wet dust removal; more preferably, the dust content of the blast furnace top gas after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the blast furnace top gas after wet dust removal is less than or equal to 5mg/Nm 3.
Further, the method further comprises: pressurizing coke oven gas before hydrogen extraction treatment; preferably, the pressure of the pressurized coke oven gas is 0.45-0.55 MPa, and the pressure of the hydrogen obtained after the hydrogen extraction treatment of the coke oven gas is 0.4-0.5 MPa.
Further, the method further comprises: pressurizing the first stripping gas before blowing the first stripping gas into a blast furnace for low-carbon smelting; preferably, the pressure of the first desorption gas after pressurization is 0.3-0.4 MPa.
Further, the method further comprises: pressurizing the converter gas before decarburizing the converter gas; preferably, the pressure of the converter gas after pressurization is 0.45-0.55 MPa, and the pressure of the converter decarburization gas obtained after decarburization treatment of the converter gas is 0.4-0.5 MPa.
Further, the method further comprises: pressurizing a portion of the top gas of the hydrogen-based shaft furnace prior to decarbonizing and denitrifying the portion; preferably, the pressure of the pressurized top gas of the hydrogen-based shaft furnace is 0.45-0.55 MPa, and the pressure of the recycled gas obtained after decarburization and denitrification treatment of a part of the top gas of the hydrogen-based shaft furnace is 0.4-0.5 MPa.
Further, the method further comprises: pressurizing a portion of the blast furnace top gas prior to decarburizing it; preferably, the pressure of the blast furnace top gas after pressurization is 0.45-0.55 MPa, and the pressure of the blast furnace decarburization gas obtained after decarburization treatment of a part of the blast furnace top gas is 0.4-0.5 MPa.
Further, the method further comprises: heat exchanging a portion of the hydrogen-based shaft furnace top gas before it is decarbonized and denitrified and before another portion of the hydrogen-based shaft furnace top gas is used as a fuel gas for heating the hydrogen-based shaft furnace reducing gas; preferably, the heat exchange treatment mode includes: reducing the temperature of the top gas of the hydrogen-based shaft furnace to below 40 ℃ by heat exchange; more preferably, the heat exchange means includes a multi-stage heat exchange including a primary heat exchange and a secondary heat exchange, the primary heat exchange means including: heat exchanging the hydrogen-based shaft furnace top gas with the recycle gas, the secondary heat exchanging comprising: heat exchanging the first-stage heat exchanged top gas of the hydrogen-based shaft furnace with a cooling liquid to reduce the temperature of the top gas of the hydrogen-based shaft furnace to 40 ℃ or below; most preferably, after heat exchange between the top gas of the hydrogen-based shaft furnace and the recycle gas, the recycle gas temperature is raised to 322-439 ℃. Wherein, the cooling liquid can adopt cooling water.
Further, the method further comprises: the hydrogen, the recycle gas, the converter decarbonization gas and the blast furnace decarbonization gas are heated before being mixed with the converter decarbonization gas and/or the blast furnace decarbonization gas and used as hydrogen-based shaft furnace reduction gas for producing sponge iron; preferably, the temperature of the hydrogen, the recycle gas, the converter decarbonizing gas and the blast furnace decarbonizing gas after heating is 950-1050 ℃.
Further, the hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55-96.5%, H 2/CO is more than or equal to 3, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the reducing gas amount of the hydrogen-based shaft furnace is 274000 ～ 317000Nm 3/H, the air pressure is 0.3-0.4 MPa, the temperature is 950-1050 ℃, the metallization rate of the sponge iron in the hydrogen-based shaft furnace is 93-95%, and the carbon content is 0.2-2.0%.
Further, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the coke oven gas is 137000 ～ 196000Nm 3 per hour, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after the hydrogen extraction treatment is carried out on the coke oven gas, the heat value of the obtained hydrogen is 60-70% of that of the coke oven gas, the gas quantity is 65000-93000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃.
Further, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the coke oven gas is 137000 ～ 196000Nm 3 per hour, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after the coke oven gas is subjected to hydrogen extraction treatment, the heat value of the obtained hydrogen is 60-70% of the heat value of the coke oven gas, the gas quantity is 65000-93000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; the heat value of the obtained first desorption gas is 1.15-1.45 times of the heat value of the coke oven gas, the gas quantity is 72000-104000 Nm 3/h, and the temperature is 20-50 ℃; the first desorption gas is blown into a blast furnace through a tuyere after being pressurized to carry out low-carbon smelting, oxygen enrichment is carried out while blowing, the oxygen enrichment rate is 28-57%, the coke ratio of the blast furnace is reduced by 45-76 kg/tHM, and the emission amount of CO 2 is reduced by 12-20%; preferably, the pressure of the first desorption gas after pressurization is 0.3-0.4 MPa.
Further, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the converter gas is 7200-100000 Nm 3/h, and the temperature is 20-50 ℃; after decarburization treatment is carried out on the converter gas, the heat value of the obtained converter decarburization gas is 1.05-1.25 times of that of the converter gas, the gas quantity is 5700-79000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; further, the heat value of the obtained second stripping gas is 35-40% of the heat value of the converter gas, the gas quantity is 1500-21200 Nm 3/h, and the temperature is 20-50 ℃.
Further, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the hydrogen content of the top gas of the hydrogen-based shaft furnace is 38-72%, the CO content is 1-13%, the gas quantity is 276000 ～ 319000Nm 3/h, the air pressure is 0.16-0.26 MPa, and the temperature is 417-534 ℃; after decarburization and denitrification treatment is carried out on a part of the top gas of the hydrogen-based shaft furnace, the heat value of the obtained recycled gas is 1.32-1.38 times that of the part of the top gas of the hydrogen-based shaft furnace, the gas quantity is 149000 ～ 181000Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; further, the heating value of the obtained third desorption gas is 70.0-88.3% of the heating value of the top gas of the part of the hydrogen-based shaft furnace, the gas quantity is 10000-60500 Nm 3/h, and the temperature is 20-50 ℃.
Further, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of a part of the top gas of the blast furnace is 8500-110000 Nm 3/h, and the temperature is 20-50 ℃; after decarburization treatment is carried out on a part of blast furnace top gas, the heat value of the obtained blast furnace decarburization gas is 1.39-1.55 times that of the part of blast furnace top gas, the gas quantity is 5700-79000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; further, the heating value of the obtained fourth desorption gas is 15-19.5% of the heating value of the part of the top gas of the blast furnace, the gas quantity is 2800-39000 Nm 3/h, and the temperature is 20-50 ℃.
It should be noted that the hour gas volumes involved in the present invention are set for 100 ten thousand tons of sponge iron per year. When the annual production of sponge iron changes, the gas quantity also needs to be correspondingly adjusted and changed.
The second aspect of the invention provides a hydrogen metallurgy system for absorbing secondary energy of a steel mill, the system comprises a coke oven gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a heating furnace, a hydrogen-based shaft furnace and a blast furnace, and the system further comprises a converter gas treatment unit and/or a blast furnace top gas treatment unit;
The coke oven gas treatment unit comprises a hydrogen extracting device, wherein the hydrogen extracting device is used for extracting hydrogen from the coke oven gas, dividing the coke oven gas into hydrogen and a first desorption gas, and is provided with a hydrogen outlet end and a first desorption gas outlet end, and the hydrogen outlet end is connected with the heating furnace;
The converter gas treatment unit comprises a first decarburization device, wherein the first decarburization device is used for decarburizing converter gas, dividing the converter gas into converter decarburization gas and second stripping gas, and is provided with a converter decarburization gas outlet end, and the converter decarburization gas outlet end is connected with the heating furnace;
The hydrogen-based shaft furnace top gas recycling unit comprises a decarburization and denitrification device, wherein the decarburization and denitrification device is used for removing CO 2 and N 2 from the hydrogen-based shaft furnace top gas, dividing the hydrogen-based shaft furnace top gas into recycle gas and third stripping gas, and is provided with a recycle gas outlet end, and the recycle gas outlet end is connected with the heating furnace;
The blast furnace top gas treatment unit comprises a second decarburization device, wherein the second decarburization device is used for decarburizing blast furnace top gas, dividing the blast furnace top gas into blast furnace decarburization gas and fourth stripping gas, and is provided with a blast furnace decarburization gas outlet end, and the blast furnace decarburization gas outlet end is connected with the heating furnace;
The heating furnace is used for heating hydrogen, converter decarburization gas, recycle gas and blast furnace decarburization gas, and the hydrogen and the recycle gas are mixed with the converter decarburization gas and/or the blast furnace decarburization gas in the heating furnace to form hydrogen-based shaft furnace reducing gas; the heating furnace is provided with a hydrogen-based shaft furnace reducing gas outlet end, the hydrogen-based shaft furnace reducing gas outlet end is connected with the hydrogen-based shaft furnace, and the hydrogen-based shaft furnace adopts the hydrogen-based shaft furnace reducing gas to produce sponge iron;
The first desorption gas outlet end is connected with the blast furnace, and the blast furnace adopts the first desorption gas to carry out low-carbon smelting to produce liquid molten iron.
Further, the system further comprises a gas pipe network, the first decarbonization device is further provided with a second desorption gas outlet end, and the second desorption gas outlet end is connected with the gas pipe network so as to send the second desorption gas into the gas pipe network.
Further, the decarbonization and denitrification device is also provided with a third desorption gas outlet end, the heating furnace is provided with a second fuel gas inlet end, and the third desorption gas outlet end is connected with the second fuel gas inlet end so as to send the third desorption gas into the heating furnace to be used as fuel gas for heating.
Further, the outlet end of the third desorption gas is also connected with a gas pipe network so as to send the third desorption gas into the gas pipe network.
Further, the system also comprises a steelmaking plant, the second decarburization device is further provided with a fourth stripping gas outlet which is connected with the steelmaking plant so as to send the fourth stripping gas into the steelmaking plant for CO 2 steelmaking.
Further, the coke oven gas treatment unit further comprises a first purifying device, wherein the first purifying device is arranged before the hydrogen extracting device and is used for purifying the coke oven gas.
Further, the converter gas treatment unit further comprises a second purifying device, wherein the second purifying device is arranged before the first decarburization device and is used for purifying the converter gas.
Further, the hydrogen-based shaft furnace top gas recycling unit further comprises a first dust removal device, wherein the first dust removal device is used for carrying out dust removal treatment on the hydrogen-based shaft furnace top gas; preferably, the first dust removal device comprises a first coarse dust remover and a dry dust remover which are sequentially connected, wherein the first coarse dust remover is used for coarsely removing dust from the top gas of the shaft furnace, and the dry dust remover is used for dry dust removal from the top gas of the shaft furnace after coarsely removing dust.
Further, the blast furnace top gas treatment unit further comprises a second dust removal device, wherein the second dust removal device is arranged before the second decarburization device and is used for carrying out dust removal treatment on the blast furnace top gas; preferably, the second dust removal device comprises a second coarse dust remover for coarse dust removal of the blast furnace top gas and a wet dust remover for wet dust removal of the blast furnace top gas.
Further, the coke oven gas treatment unit further comprises a first pressurizing machine, wherein the first pressurizing machine is used for pressurizing the coke oven gas; preferably, the first pressurizing machine is disposed between the first purifying device and the hydrogen extracting device.
Further, the coke oven gas treatment unit further comprises a fourth pressurizing machine, and the fourth pressurizing machine is arranged between the hydrogen extracting device and the blast furnace and is used for pressurizing the first desorption gas.
Further, the converter gas treatment unit further comprises a second pressurizing machine, wherein the second pressurizing machine is used for pressurizing the purified converter gas; preferably, the second press is disposed between the second purifying device and the first decarburizing device.
Further, the hydrogen-based shaft furnace top gas recycling unit further comprises a third pressurizing machine, wherein the third pressurizing machine is used for pressurizing the heat-exchanged hydrogen-based shaft furnace top gas; preferably, the third press is disposed between the first dust removing device and the decarburization and denitrification device.
Further, the blast furnace top gas treatment unit further comprises a fifth pressurizing machine, wherein the fifth pressurizing machine is used for pressurizing the blast furnace top gas after dust removal; preferably, the fifth press is disposed between the second dust removing device and the second decarburizing device.
Further, the hydrogen-based shaft furnace top gas recycling unit further comprises a heat exchange device, wherein the heat exchange device is used for carrying out heat exchange treatment on the hydrogen-based shaft furnace top gas; preferably, the heat exchange device is arranged between the first dust removal device and the third pressurizing machine, the heat exchange device comprises a multi-stage heat exchanger, the multi-stage heat exchanger comprises a primary heat exchanger and a secondary heat exchanger which are sequentially connected, the primary heat exchanger is connected with the outlet end of the recycled gas and is used for heat exchange between the recycled gas and the top gas of the hydrogen-based shaft furnace, and the secondary heat exchanger is used for heat exchange between the cooling liquid and the top gas of the hydrogen-based shaft furnace.
Further, the heating furnace is also provided with a first fuel gas inlet end, wherein the first fuel gas inlet end is an inlet for feeding hydrogen-based shaft furnace top gas into the heating furnace so as to feed the hydrogen-based shaft furnace top gas into the heating furnace as fuel gas for heating; preferably, the first fuel gas inlet end is connected to the hydrogen-based shaft furnace top gas outlet end of the heat exchange device, so that part of the heat exchanged hydrogen-based shaft furnace top gas is fed into the heating furnace as fuel gas for heating.
A third aspect of the invention provides a method according to the first aspect and/or a system according to the second aspect and uses thereof in the field of hydrogen metallurgy.
As described above, the hydrogen metallurgy method, the hydrogen metallurgy system and the application thereof for absorbing secondary energy of a steel mill have the following beneficial effects:
1) The invention extracts and utilizes H 2 in coke oven gas, CO in converter gas and CO in blast furnace top gas after rich hydrogen and oxygen as reducing gas, thereby fully utilizing the reducing capability of secondary energy of steel mill, replacing reforming reformer with mature and simple gas removal device, and reducing primary energy consumption and equipment investment of hydrogen-based shaft furnace.
2) In the method, the volume fraction of the H 2 of the hydrogen-based shaft furnace is 55-96.5%, the temperature is controlled at 950-1050 ℃, and the higher reduction capability is ensured; the CO volume fraction is 1.4-18%, and the carburization amount of 0.2-2.0% of the sponge iron can be effectively realized.
3) According to the invention, methane-rich stripping gas (namely first stripping gas) after hydrogen extraction of coke oven gas is blown into the blast furnace, and oxygen-enriched operation is performed at the same time, so that the coke ratio of the blast furnace can be reduced and the CO 2 emission of a combined steel plant can be reduced under the condition that the original blast furnace belly gas amount and theoretical combustion temperature are maintained to be basically unchanged.
In conclusion, the technology provided by the invention provides a new low-carbon and high-efficiency hydrogen metallurgy method for solving the technical problems of secondary energy consumption and high-investment reforming conversion in a steel mill, and has very important significance for simplifying the technological process of a hydrogen-based shaft furnace and reducing the carbon emission of the blast furnace.
Drawings
FIG. 1 is a schematic view showing the arrangement of a hydrogen metallurgy system for absorbing secondary energy of a steel mill according to an embodiment of the present invention in examples 1 to 8.
FIG. 2 shows a schematic layout of a hydrogen metallurgy system for absorbing secondary energy of a steel mill according to another embodiment of the present invention in examples 9 to 11.
FIG. 3 is a schematic view showing the arrangement of a hydrogen metallurgy system for absorbing secondary energy of a steel mill according to another embodiment of the present invention in example 12.
Reference numerals illustrate:
The first compressor 11, the hydrogen extracting device 12, the fourth compressor 13, the second compressor 21, the first decarburization device 22, the first coarse dust remover 31, the dry dust remover 32, the heat exchange device 33, the third compressor 34, the decarburization denitrification device 35, the second coarse dust remover 41, the wet dust remover 42, the fifth compressor 43, the second decarburization device 44, the heating furnace 50, the hydrogen-based shaft furnace 60, the blast furnace 70, the gas pipe network 80 and the steelmaking workshop 90.
Detailed Description
Other advantages and effects of the present invention will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present invention with reference to specific examples. The invention may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present invention.
The same or similar reference numbers in the drawings of embodiments of the invention correspond to the same or similar components; in the description of the present invention, it should be understood that, if there are terms such as "upper", "lower", "left", "right", "front", "rear", etc., that indicate an azimuth or a positional relationship based on the azimuth or the positional relationship shown in the drawings, it is only for convenience of describing the present invention and simplifying the description, but not for indicating or suggesting that the referred device or element must have a specific azimuth, be constructed and operated in a specific azimuth, so that the terms describing the positional relationship in the drawings are merely for exemplary illustration and should not be construed as limiting the present invention, and that the specific meaning of the above terms may be understood by those of ordinary skill in the art according to the specific circumstances.
The invention provides a hydrogen metallurgy method for absorbing secondary energy of a steel mill, which comprises the following steps of:
Carrying out hydrogen extraction treatment on coke oven gas to obtain hydrogen and a first desorption gas, and blowing the first desorption gas into a blast furnace to carry out low-carbon smelting to produce liquid molten iron;
Decarburization treatment is carried out on the converter gas to obtain converter decarburization gas and second stripping gas;
decarburizing and denitrifying a part of top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas;
Decarburizing a part of the blast furnace top gas to obtain blast furnace decarburization gas and fourth stripping gas;
mixing the hydrogen and the recycle gas, and mixing the mixture with the converter decarburization gas and/or the blast furnace decarburization gas to jointly serve as hydrogen-based shaft furnace reducing gas for producing sponge iron.
The method comprises the steps of mixing hydrogen with recycle gas, mixing the mixture with converter decarburization gas and/or blast furnace decarburization gas, and taking the mixture as hydrogen-based shaft furnace reducing gas, wherein the composition of the hydrogen-based shaft furnace reducing gas specifically comprises the following three modes:
1. The hydrogen, the recycle gas and the converter decarburization gas are mixed to form hydrogen-based shaft furnace reducing gas;
2. the hydrogen, the recycle gas and the blast furnace decarburization gas are mixed to form hydrogen-based shaft furnace reducing gas;
3. The hydrogen-based shaft furnace reducing gas is formed by mixing hydrogen, recycle gas, converter decarburization gas and blast furnace decarburization gas.
The method of the embodiment extracts and utilizes H 2 in the coke oven gas, CO in the converter gas and CO in the blast furnace top gas after rich hydrogen and oxygen enrichment as the reducing gas, thereby fully utilizing the reducing capability of secondary energy of a steel mill, using a mature and simple gas removal device to replace a reforming reformer with higher investment, and reducing the primary energy consumption and equipment investment of the hydrogen-based shaft furnace; the methane-rich stripping gas (namely the first stripping gas) after hydrogen extraction of coke oven gas is blown into the blast furnace, and simultaneously the oxygen-rich operation is carried out, so that the coke ratio of the blast furnace can be reduced and the CO 2 emission of the combined steel mill can be reduced under the condition that the original blast furnace belly gas quantity and theoretical combustion temperature are maintained to be basically unchanged.
In another embodiment of the invention, the second desorption gas is conveyed to a steel mill gas pipe network, so that full utilization of converter gas is realized.
In another embodiment of the invention, a portion of the third stripping gas is used as a fuel gas (i.e., a second fuel gas) for heating the hydrogen-based shaft furnace reduction gas.
In another embodiment of the invention, the other part of the third stripping gas is delivered to a steel mill gas pipe network.
The third stripping gas is divided into two parts for use in the embodiment, so that the full utilization of the top gas of the hydrogen-based shaft furnace is realized.
In another embodiment of the invention, the fourth stripping gas is delivered to a steelmaking plant for CO 2 steelmaking, thereby realizing the full utilization of the blast furnace top gas.
In another embodiment of the invention, another portion of the hydrogen-based shaft furnace top gas is used as a fuel gas (i.e., a first fuel gas) for heating the hydrogen-based shaft furnace reduction gas; preferably, the other part of the hydrogen-based shaft furnace top gas used as fuel gas for heating the hydrogen-based shaft furnace reducing gas accounts for 12.0-17.1% by volume of the total hydrogen-based shaft furnace top gas.
In a specific embodiment, in the fuel gas, the volume fraction of the third stripping gas is less than or equal to 25% (i.e. the amount of the second fuel gas), and the volume fraction of the other part of the top gas of the hydrogen-based shaft furnace is more than or equal to 75% (i.e. the amount of the first fuel gas).
The third stripping gas and a part of the top gas of the hydrogen-based shaft furnace are used as fuel gas for heating the reducing gas of the hydrogen-based shaft furnace, so that external fuel is not needed, and self-sufficiency is realized; it should be noted that the second fuel gas is an alternative fuel gas, or may be considered a supplemental fuel gas, and that when the first fuel gas is deficient, a portion of the third desorption gas may be selected as the supplemental fuel gas for use in heating the hydrogen-based shaft furnace reducing gas.
In another embodiment of the present invention, the method further comprises: the coke oven gas is purified before being subjected to hydrogen stripping treatment.
In another embodiment of the present invention, the method further comprises: the converter gas is cleaned before it is decarbonized.
The purification treatment in the above embodiment means desulfurization purification treatment, namely, removal of organic sulfur and inorganic sulfur from the gas. Preferably, the total sulfur content of the coke oven/converter gas after desulfurization treatment is less than or equal to 10mg/m 3.
In another embodiment of the present invention, the method further comprises: dedusting a portion of the hydrogen-based shaft furnace top gas before it is subjected to a decarbonizing denitrification process and before another portion of the hydrogen-based shaft furnace top gas is used as a fuel gas for heating the hydrogen-based shaft furnace reducing gas; preferably, the mode of dust removal treatment of the top gas of the hydrogen-based shaft furnace comprises coarse dust removal and dry dust removal; more preferably, the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3.
In another embodiment of the present invention, the method further comprises: before decarburizing a part of blast furnace top gas, carrying out dust removal treatment on the blast furnace top gas; preferably, the way of dust removal treatment of blast furnace top gas comprises coarse dust removal and wet dust removal; more preferably, the dust content of the blast furnace top gas after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the blast furnace top gas after wet dust removal is less than or equal to 5mg/Nm 3.
In another embodiment of the present invention, the method further comprises: after the coke oven gas is purified, the coke oven gas is pressurized before hydrogen extraction treatment is carried out on the coke oven gas; preferably, the pressure of the pressurized coke oven gas is 0.45-0.55 MPa, and the pressure of the hydrogen obtained after the hydrogen extraction treatment of the coke oven gas is 0.4-0.5 MPa.
In another embodiment of the present invention, the method further comprises: pressurizing the first stripping gas before blowing the first stripping gas into a blast furnace for low-carbon smelting; preferably, the pressure of the first desorption gas after pressurization is 0.3-0.4 MPa.
In another embodiment of the present invention, the method further comprises: after the converter gas is purified, pressurizing the converter gas before decarburizing the converter gas; preferably, the pressure of the converter gas after pressurization is 0.45-0.55 MPa, and the pressure of the converter decarburization gas obtained after decarburization treatment of the converter gas is 0.4-0.5 MPa.
In another embodiment of the present invention, the method further comprises: pressurizing a portion of the top gas of the hydrogen-based shaft furnace prior to decarbonizing and denitrifying the portion; preferably, the pressure of the pressurized top gas of the hydrogen-based shaft furnace is 0.45-0.55 MPa, and the pressure of the recycled gas obtained after decarburization and denitrification treatment of a part of the top gas of the hydrogen-based shaft furnace is 0.4-0.5 MPa.
In another embodiment of the present invention, the method further comprises: after dedusting a portion of the blast furnace top gas, pressurizing a portion of the blast furnace top gas before decarburizing it; preferably, the pressure of the blast furnace top gas after pressurization is 0.45-0.55 MPa, and the pressure of the blast furnace decarburization gas obtained after decarburization treatment of a part of the blast furnace top gas is 0.4-0.5 MPa.
In another embodiment of the present invention, the method further comprises: after the dust removal of the hydrogen-based shaft furnace top gas, a heat exchange treatment is performed on a part of the hydrogen-based shaft furnace top gas before it is pressurized and decarbonized and denitrified, and before another part of the hydrogen-based shaft furnace top gas is used as fuel gas for heating the hydrogen-based shaft furnace reduction gas; preferably, the heat exchange treatment mode includes: reducing the temperature of the top gas of the hydrogen-based shaft furnace to below 40 ℃ by heat exchange; more preferably, the heat exchange means includes a multi-stage heat exchange including a primary heat exchange and a secondary heat exchange, the primary heat exchange means including: heat exchanging the hydrogen-based shaft furnace top gas with the recycle gas, the secondary heat exchanging comprising: heat exchanging the first-stage heat exchanged top gas of the hydrogen-based shaft furnace with a cooling liquid to reduce the temperature of the top gas of the hydrogen-based shaft furnace to 40 ℃ or below; most preferably, after heat exchange between the top gas of the hydrogen-based shaft furnace and the recycle gas, the recycle gas temperature is raised to 322-439 ℃. Wherein, the cooling liquid can adopt cooling water.
The embodiment reduces the temperature of the top gas of the hydrogen-based shaft furnace through heat exchange so as to facilitate decarburization and denitrification treatment; the recycling gas and the top gas of the hydrogen-based shaft furnace are subjected to heat exchange, so that the waste heat of the top gas of the hydrogen-based shaft furnace is fully utilized, the temperature of the recycling gas is increased, and the requirement of a heating link on fuel gas can be reduced; in addition, in order to avoid adverse effect on decarburization and denitrification caused by excessive high temperature of the top gas of the hydrogen-based shaft furnace after heat exchange with the recycle gas, a cooling liquid can be used for carrying out secondary heat exchange so as to control the temperature of the top gas of the hydrogen-based shaft furnace after heat exchange to be 40 ℃ or below.
In another embodiment of the present invention, the method further comprises: the hydrogen, the recycle gas, the converter decarbonization gas and the blast furnace decarbonization gas are heated before being mixed with the converter decarbonization gas and/or the blast furnace decarbonization gas and used as hydrogen-based shaft furnace reduction gas for producing sponge iron; preferably, the temperature of the hydrogen, the recycle gas, the converter decarbonizing gas and the blast furnace decarbonizing gas after heating is 950-1050 ℃.
In another embodiment of the invention, the hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55-96.5%, H 2/CO is more than or equal to 3, the reducing gas amount of the hydrogen-based shaft furnace is 274000 ～ 317000Nm 3/H, the air pressure is 0.3-0.4 MPa, the temperature is 950-1050 ℃, the metallization rate of the sponge iron in the hydrogen-based shaft furnace is 93-95%, and the carbon content is 0.2-2.0% when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year.
In the embodiment, the volume fraction of the reducing gas H 2 of the hydrogen-based shaft furnace is controlled to be 55-96.5%, and the temperature is controlled to be 950-1050 ℃, so that higher reducing capability is ensured; the CO volume fraction is controlled to be 1.4-18%, so that the carburization amount of 0.2-2.0% of sponge iron can be effectively realized.
In order to achieve the technical effects, in a specific embodiment, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the coke oven gas is 137000 ～ 196000Nm 3/h, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after the coke oven gas is subjected to hydrogen extraction treatment, the heat value of the obtained hydrogen is 60-70% of the heat value of the coke oven gas, the gas quantity is 65000-93000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; the heat value of the obtained first desorption gas is 1.15-1.45 times of the heat value of the coke oven gas, the gas quantity is 72000-104000 Nm 3/h, and the temperature is 20-50 ℃; the first desorption gas is blown into a blast furnace through a tuyere after being pressurized to carry out low-carbon smelting, oxygen enrichment is carried out while blowing, the oxygen enrichment rate is 28-57%, the coke ratio of the blast furnace is reduced by 45-76 kg/tHM, and the emission amount of CO 2 is reduced by 12-20%; preferably, the pressure of the first desorption gas after pressurization is 0.3-0.4 MPa.
In a specific embodiment, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the converter gas is 7200-100000 Nm 3/h, and the temperature is 20-50 ℃; after decarburization treatment is carried out on the converter gas, the heat value of the obtained converter decarburization gas is 1.05-1.25 times of that of the converter gas, the gas quantity is 5700-79000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; the heat value of the obtained second stripping gas is 35-40% of the heat value of the converter gas, the gas quantity is 1500-21200 Nm 3/h, the temperature is 20-50 ℃, and the gas pressure is 0.02MPa.
In a specific embodiment, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the hydrogen content of the top gas of the hydrogen-based shaft furnace is 38-72%, the CO content is 1-13%, the gas amount is 276000 ～ 319000Nm 3/h, the gas pressure is 0.16-0.26 MPa, and the temperature is 417-534 ℃; after decarburization and denitrification treatment is carried out on a part of the top gas of the hydrogen-based shaft furnace, the heat value of the obtained recycled gas is 1.32-1.38 times that of the part of the top gas of the hydrogen-based shaft furnace, the gas quantity is 149000 ～ 181000Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; the calorific value of the obtained third desorption gas is 70.0-88.3% of the calorific value of the top gas of the part of hydrogen-based shaft furnace, the gas quantity is 10000-60500 Nm 3/h, the temperature is 20-50 ℃, and the gas pressure is 0.02MPa.
In a specific embodiment, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of a part of the top gas of the blast furnace is 8500-110000 Nm 3/h, and the temperature is 20-50 ℃; after decarburization treatment is carried out on a part of blast furnace top gas, the heat value of the obtained blast furnace decarburization gas is 1.39-1.55 times that of the part of blast furnace top gas, the gas quantity is 5700-79000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; the calorific value of the obtained fourth desorption gas is 15-19.5% of the calorific value of a part of blast furnace top gas, the gas quantity is 2800-39000 Nm 3/h, the temperature is 20-50 ℃, and the gas pressure is 0.02MPa.
In the above embodiment, the method of extracting hydrogen, decarbonizing and denitrifying may be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method. The above methods are all prior art, and the present invention is not described herein in detail.
It should be noted that the amount of hours involved in the above-described embodiments of the invention and in the examples that follow is set for a production of 100 ten thousand tons of sponge iron per year. When the annual production of sponge iron changes, the gas quantity also needs to be correspondingly adjusted and changed. Those skilled in the art can design and adjust the present invention according to the actual situation and needs with reference to the embodiments and examples.
Non-blast furnace smelting reduction iron making processes put into commercial production at present mainly comprise COREX, FINEX and HIsmolt processes. COREX has been successfully used in China, south Africa, india and other countries, and FINEX has been successfully used in North east Asia; the domestic introduction time of the HIsmelt process is relatively short, and at present, the HIsmelt process is in a digestion and absorption stage, and domestic ironmaking workers are also conducting intensive research on the HIsmelt process. COREX gas, FINEX gas and HIsmolt gas all contain CO and H 2, and can be used as supplementary gas for hydrogen-based shaft furnace reduction after decarburization. It should be noted, however, that COREX, FINEX and HIsmelt process are not the same in application, and there is no scenario in one factory at the same time. Therefore, any one of the COREX gas, the FINEX gas and the HIsmelt gas may be used instead of the blast furnace top gas in the above-described embodiment/example of the present invention, or any one of the COREX gas, the FINEX gas and the HIsmelt gas may be used in combination with at least one of the blast furnace top gas and the converter gas in the above-described embodiment/example of the present invention, and the decarburization treatment may be performed with reference to the same/similar method as in the above-described embodiment/example of the present invention, followed by recycling.
Referring to fig. 1 to 3, an embodiment of the present invention provides a hydrogen metallurgy system for absorbing secondary energy of a steel mill, which comprises a coke oven gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a heating furnace 50, a hydrogen-based shaft furnace 60, a blast furnace 70, and a converter gas treatment unit and/or a blast furnace top gas treatment unit;
the coke oven gas treatment unit comprises a hydrogen extracting device 12, wherein the hydrogen extracting device 12 is used for extracting hydrogen from the coke oven gas, dividing the coke oven gas into hydrogen and a first desorption gas, and is provided with a hydrogen outlet end and a first desorption gas outlet end, and the hydrogen outlet end is connected with the heating furnace 50;
The converter gas treatment unit comprises a first decarburization device 22, wherein the first decarburization device 22 is used for decarburizing the converter gas, dividing the converter gas into converter decarburization gas and second stripping gas, and is provided with a converter decarburization gas outlet end which is connected with the heating furnace 50;
The hydrogen-based shaft furnace top gas recycling unit comprises a decarbonization and denitrification device 35, wherein the decarbonization and denitrification device 35 is used for removing CO 2 and N 2 from the hydrogen-based shaft furnace top gas, dividing the hydrogen-based shaft furnace top gas into recycle gas and third stripping gas, and is provided with a recycle gas outlet end which is connected with the heating furnace 50;
The blast furnace top gas treatment unit comprises a second decarburization device 44, wherein the second decarburization device 44 is used for decarburizing blast furnace top gas, dividing the blast furnace top gas into blast furnace decarburization gas and fourth stripping gas, and is provided with a blast furnace decarburization gas outlet end which is connected with the heating furnace 50;
The heating furnace 50 is used for heating hydrogen, converter decarburization gas, recycle gas and blast furnace decarburization gas, and the hydrogen and the recycle gas are mixed with the converter decarburization gas and/or the blast furnace decarburization gas in the heating furnace 50 to form hydrogen-based shaft furnace reducing gas; the heating furnace 50 is provided with a hydrogen-based shaft furnace reducing gas outlet end, the hydrogen-based shaft furnace reducing gas outlet end is connected with a hydrogen-based shaft furnace 60, and the hydrogen-based shaft furnace 60 adopts the hydrogen-based shaft furnace reducing gas to produce sponge iron;
The outlet end of the first desorption gas is connected with a blast furnace 70, and the blast furnace 70 adopts the first desorption gas to carry out low-carbon smelting to produce liquid molten iron.
In another embodiment of the present invention, the system further comprises a gas pipe network 80, and the first decarbonization device 22 is further provided with a second stripping gas outlet connected to the gas pipe network 80 for delivering the second stripping gas into the gas pipe network 80.
In another embodiment of the present invention, the decarbonization and denitrification device 35 is further provided with a third desorption gas outlet port, the heating furnace 50 is provided with a second fuel gas inlet port, and the third desorption gas outlet port is connected to the second fuel gas inlet port to send the third desorption gas into the heating furnace 50 as the fuel gas for heating.
In another embodiment of the present invention, the third stripping gas outlet is also connected to the gas pipe network 80 to send the third stripping gas into the gas pipe network 80.
In another embodiment of the present invention, the system further comprises a steel plant 90, and the second decarbonization device 44 is further provided with a fourth stripping gas outlet connected to the steel plant 90 for feeding the fourth stripping gas into the steel plant 90 for use in the production of CO 2 steel.
In a further embodiment of the invention, the coke oven gas treatment unit further comprises a first cleaning device (not shown in the figures) arranged before the hydrogen-extracting device 12 for cleaning the coke oven gas.
In another embodiment of the invention, the converter gas treatment unit further comprises a second cleaning device (not shown in the figures) arranged before the first decarbonizing device 22 for cleaning the converter gas.
In another embodiment of the invention, the hydrogen-based shaft furnace top gas recycling unit further comprises a first dust removal device arranged between the hydrogen-based shaft furnace 60 and the heat exchange device 33 for dust removal of the hydrogen-based shaft furnace top gas; preferably, the first dust removal device comprises a first coarse dust remover 31 and a dry dust remover 32 connected in sequence, the first coarse dust remover 31 being for coarse dust removal of the top gas of the shaft furnace, the dry dust remover 32 being for dry dust removal of the top gas of the shaft furnace after coarse dust removal.
In another embodiment of the invention, the blast furnace top gas treatment unit further comprises a second dust removal device arranged before the second decarbonization device 44 for dust removal treatment of the blast furnace top gas; preferably, the second dust removing device comprises a second coarse dust remover 41 and a wet dust remover 42 connected in sequence, the second coarse dust remover 41 being used for coarse dust removal of blast furnace top gas, and the wet dust remover 42 being used for wet dust removal of blast furnace top gas.
In another embodiment of the present invention, the coke oven gas treatment unit further comprises a first pressurizing machine 11, the first pressurizing machine 11 being used for pressurizing the coke oven gas; preferably, the first pressurizing device 11 is arranged between the first purifying device and the hydrogen extracting device 12.
In another embodiment of the invention, the coke oven gas treatment unit further comprises a fourth pressurizing machine 13, the fourth pressurizing machine 13 being arranged between the hydrogen-extracting device 12 and the blast furnace 70 for pressurizing the first desorption gas.
In another embodiment of the invention, the converter gas treatment unit further comprises a second pressurizing machine 21, the second pressurizing machine 21 being used for pressurizing the purified converter gas; preferably, the second pressurizing machine 21 is arranged between the second purifying device and the second decarbonizing device 44.
In another embodiment of the invention, the hydrogen-based shaft furnace top gas recycling unit further comprises a third pressurizing machine 34, the third pressurizing machine 34 being used for pressurizing the heat exchanged hydrogen-based shaft furnace top gas; preferably, the third pressurizing machine 34 is disposed between the first dust removing device and the decarbonization and denitrification device 35.
In another embodiment of the invention, the blast furnace top gas treatment unit further comprises a fifth pressure vessel 43, the fifth pressure vessel 43 being adapted to pressurize the dedusted blast furnace top gas; preferably, the fifth pressure vessel 43 is arranged between the second dust removing device and the second decarbonizing device 44.
In another embodiment of the invention, the hydrogen-based shaft furnace top gas recycling unit further comprises a heat exchange device 33, the heat exchange device 33 being used for heat exchange treatment of the hydrogen-based shaft furnace top gas; preferably, the heat exchange device 33 is arranged between the first dust removing device and the third pressurizing device 34, the heat exchange device 33 comprises a multi-stage heat exchanger, the multi-stage heat exchanger comprises a primary heat exchanger and a secondary heat exchanger which are sequentially connected, the primary heat exchanger is connected with the outlet end of the recycled gas and is used for heat exchange between the recycled gas and the top gas of the hydrogen-based shaft furnace, and the secondary heat exchanger is used for heat exchange between the cooling liquid and the top gas of the hydrogen-based shaft furnace.
In another embodiment of the present invention, the heating furnace 50 is further provided with a first fuel gas inlet end, wherein the first fuel gas inlet end is the inlet for feeding the hydrogen-based shaft furnace top gas into the heating furnace 50, so as to feed the hydrogen-based shaft furnace top gas into the heating furnace 50 as the fuel gas for heating; preferably, the first fuel gas inlet end is connected to the hydrogen-based shaft furnace top gas outlet end of the heat exchange means 33 for feeding a portion of the heat exchanged hydrogen-based shaft furnace top gas to the heating furnace 50 as fuel gas for heating.
As shown in fig. 1, an embodiment of the present invention provides a hydrogen metallurgy system for absorbing secondary energy of a steel mill, comprising a coke oven gas treatment unit, a converter gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a heating furnace 50, a hydrogen-based shaft furnace 60, a blast furnace 70, and a gas pipe network 80;
Specifically, the coke oven gas treatment unit comprises a first purifying device, a first pressurizing machine 11, a hydrogen extracting device 12 and a fourth pressurizing machine 13 which are sequentially connected, the coke oven gas is purified by the first purifying device, the first pressurizing machine 11 is pressurized, hydrogen is extracted by the hydrogen extracting device 12 and is divided into hydrogen and first stripping gas, the hydrogen extracting device 12 is provided with a hydrogen outlet end and a first stripping gas outlet end, wherein the hydrogen outlet end is connected with the heating furnace 50, the first stripping gas outlet end and the fourth pressurizing machine 13 are sequentially connected with the blast furnace 70, and the first stripping gas is blown into the blast furnace 70 through a tuyere for low-carbon smelting after being pressurized by the fourth pressurizing machine 13;
The converter gas treatment unit comprises a second purifying device, a second pressurizing machine 21 and a first decarburization device 22 which are sequentially connected, wherein the converter gas enters the first decarburization device 22 for decarburization after being purified by the second purifying device and pressurized by the second pressurizing machine 21 and is divided into converter decarburization gas and second desorption gas, the first decarburization device 22 is provided with a converter decarburization gas outlet end and a second desorption gas outlet end, the converter decarburization gas outlet end is connected with the heating furnace 50, and the second desorption gas outlet end is connected with the gas pipe network 80 so as to send the second desorption gas into the gas pipe network 80;
The hydrogen-based shaft furnace top gas recycling unit comprises a first dust removing device, a heat exchanging device 33, a third pressurizing machine 34 and a decarburization and denitrification device 35 which are sequentially connected from a hydrogen shaft furnace top gas outlet, wherein the first dust removing device comprises a first coarse dust remover 31 and a dry dust remover 32, and after coarse dust removal and dry dust removal, the hydrogen-based shaft furnace top gas is subjected to primary heat exchange with recycle gas in the heat exchanging device 33 and then subjected to secondary heat exchange with cooling liquid; then, a part of the top gas of the hydrogen-based shaft furnace enters a third pressurizing machine 34, enters a decarburization and denitrification device 35 after being pressurized, removes CO 2 and N 2 and is divided into recycle gas and third desorption gas, wherein the decarburization and denitrification device 35 is provided with a recycle gas outlet end and a third desorption gas outlet end, the recycle gas outlet end is connected with a heating furnace 50, the third desorption gas outlet end is connected with a second fuel gas inlet end so as to send the third desorption gas into the heating furnace 50 to be used as fuel gas for heating, and the third desorption gas outlet end is also connected with a gas pipe network 80 so as to send the third desorption gas into the gas pipe network 80; the other part of the top gas of the hydrogen-based shaft furnace is directly fed into the heating furnace 50 to be used as fuel gas after heat exchange;
The heating furnace 50 is used for heating hydrogen, converter decarburization gas and recycle gas, and the hydrogen, the converter decarburization gas and the recycle gas are mixed in the heating furnace 50 to form hydrogen-based shaft furnace reducing gas; the heating furnace 50 is provided with a hydrogen-based shaft furnace reducing gas outlet end, the hydrogen-based shaft furnace reducing gas outlet end is connected with a hydrogen-based shaft furnace 60, and the hydrogen-based shaft furnace 60 adopts the hydrogen-based shaft furnace reducing gas to produce sponge iron;
the blast furnace 70 performs low-carbon smelting by using the first stripping gas to produce liquid molten iron.
As shown in fig. 2, another embodiment of the present invention provides a hydrogen metallurgy system for consuming secondary energy of a steel mill, comprising a coke oven gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a blast furnace top gas treatment unit, a heating furnace 50, a hydrogen-based shaft furnace 60, a blast furnace 70, a gas pipe network 80, and a steel-making shop 90;
Specifically, the coke oven gas treatment unit comprises a first purifying device, a first pressurizing machine 11 and a hydrogen extracting device 12 which are sequentially connected, the coke oven gas is purified by the first purifying device, the first pressurizing machine 11 is pressurized, hydrogen is extracted by the hydrogen extracting device 12 and is divided into hydrogen and first desorption gas, the hydrogen extracting device 12 is provided with a hydrogen outlet end and a first desorption gas outlet end, wherein the hydrogen outlet end is connected with the heating furnace 50, and the first desorption gas outlet end is connected with the blast furnace 70;
The hydrogen-based shaft furnace top gas recycling unit comprises a first dust removing device, a heat exchanging device 33, a third pressurizing machine 34 and a decarburization and denitrification device 35 which are sequentially connected from a hydrogen shaft furnace top gas outlet, wherein the first dust removing device comprises a first coarse dust remover 31 and a dry dust remover 32, and after coarse dust removal and dry dust removal, the hydrogen-based shaft furnace top gas is subjected to primary heat exchange with recycle gas in the heat exchanging device 33 and then subjected to secondary heat exchange with cooling liquid; then, a part of the top gas of the hydrogen-based shaft furnace enters a third pressurizing machine 34, enters a decarburization and denitrification device 35 after being pressurized, removes CO 2 and N 2 and is divided into recycle gas and third desorption gas, wherein the decarburization and denitrification device 35 is provided with a recycle gas outlet end and a third desorption gas outlet end, the recycle gas outlet end is connected with a heating furnace 50, the third desorption gas outlet end is connected with a second fuel gas inlet end so as to send the third desorption gas into the heating furnace 50 to be used as fuel gas for heating, and the third desorption gas outlet end is also connected with a gas pipe network 80 so as to send the third desorption gas into the gas pipe network 80; the other part of the top gas of the hydrogen-based shaft furnace is directly fed into the heating furnace 50 to be used as fuel gas after heat exchange;
The blast furnace top gas treatment unit comprises a second dust removing device, a fifth pressure adding machine 43 and a second decarburization device 44 which are sequentially connected from a blast furnace top gas outlet, wherein the second dust removing device comprises a first coarse dust remover 31 and a wet dust remover 42, the blast furnace top gas enters the second decarburization device 44 for decarburization after coarse dust removal, wet dust removal and pressurization, and is divided into blast furnace decarburization gas and fourth desorption gas, the second decarburization device 44 is provided with a blast furnace decarburization gas outlet end and a fourth desorption gas outlet end, the blast furnace decarburization gas outlet end is connected with the heating furnace 50, and the fourth desorption gas outlet end is connected with the steelmaking workshop 90 so as to send the fourth desorption gas into the steelmaking workshop 90 for CO 2 steelmaking;
The heating furnace 50 is used for heating hydrogen, converter decarburization gas, recycle gas and blast furnace decarburization gas, and the hydrogen and the recycle gas are mixed with the converter decarburization gas and/or the blast furnace decarburization gas in the heating furnace 50 to form hydrogen-based shaft furnace reducing gas; the heating furnace 50 is provided with a hydrogen-based shaft furnace reducing gas outlet end, the hydrogen-based shaft furnace reducing gas outlet end is connected with a hydrogen-based shaft furnace 60, and the hydrogen-based shaft furnace 60 adopts the hydrogen-based shaft furnace reducing gas to produce sponge iron;
the blast furnace 70 performs low-carbon smelting by using the first stripping gas to produce liquid molten iron.
As shown in fig. 3, another embodiment of the present invention provides a hydrogen metallurgy system for consuming secondary energy of a steel mill, comprising a coke oven gas treatment unit, a converter gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a blast furnace top gas treatment unit, a heating furnace 50, a hydrogen-based shaft furnace 60, a blast furnace 70, a gas pipe network 80, and a steelmaking plant 90;
Specifically, the coke oven gas treatment unit comprises a first purifying device, a first pressurizing machine 11 and a hydrogen extracting device 12 which are sequentially connected, the coke oven gas is purified by the first purifying device, the first pressurizing machine 11 is pressurized, hydrogen is extracted by the hydrogen extracting device 12 and is divided into hydrogen and first desorption gas, the hydrogen extracting device 12 is provided with a hydrogen outlet end and a first desorption gas outlet end, wherein the hydrogen outlet end is connected with the heating furnace 50, and the first desorption gas outlet end is connected with the blast furnace 70;
The converter gas treatment unit comprises a second purifying device, a second pressurizing machine 21 and a first decarburization device 22 which are sequentially connected, wherein the converter gas enters the first decarburization device 22 for decarburization after being purified by the second purifying device and pressurized by the second pressurizing machine 21 and is divided into converter decarburization gas and second desorption gas, the first decarburization device 22 is provided with a converter decarburization gas outlet end and a second desorption gas outlet end, the converter decarburization gas outlet end is connected with the heating furnace 50, and the second desorption gas outlet end is connected with the gas pipe network 80 so as to send the second desorption gas into the gas pipe network 80;
The hydrogen-based shaft furnace top gas recycling unit comprises a first dust removing device, a heat exchanging device 33, a third pressurizing machine 34 and a decarburization and denitrification device 35 which are sequentially connected from a hydrogen shaft furnace top gas outlet, wherein the first dust removing device comprises a first coarse dust remover 31 and a dry dust remover 32, and after coarse dust removal and dry dust removal, the hydrogen-based shaft furnace top gas is subjected to primary heat exchange with recycle gas in the heat exchanging device 33 and then subjected to secondary heat exchange with cooling liquid; then, a part of the top gas of the hydrogen-based shaft furnace enters a third pressurizing machine 34, enters a decarburization and denitrification device 35 after being pressurized, removes CO 2 and N 2 and is divided into recycle gas and third desorption gas, wherein the decarburization and denitrification device 35 is provided with a recycle gas outlet end and a third desorption gas outlet end, the recycle gas outlet end is connected with a heating furnace 50, the third desorption gas outlet end is connected with a second fuel gas inlet end so as to send the third desorption gas into the heating furnace 50 to be used as fuel gas for heating, and the third desorption gas outlet end is also connected with a gas pipe network 80 so as to send the third desorption gas into the gas pipe network 80; the other part of the top gas of the hydrogen-based shaft furnace is directly fed into the heating furnace 50 to be used as fuel gas after heat exchange;
The blast furnace top gas treatment unit comprises a second dust removing device, a fifth pressure adding machine 43 and a second decarburization device 44 which are sequentially connected from a blast furnace top gas outlet, wherein the second dust removing device comprises a second coarse dust remover 41 and a wet dust remover 42, the blast furnace top gas enters the second decarburization device 44 for decarburization after coarse dust removal, wet dust removal and pressurization, and is divided into blast furnace decarburization gas and fourth desorption gas, the second decarburization device 44 is provided with a blast furnace decarburization gas outlet end and a fourth desorption gas outlet end, the blast furnace decarburization gas outlet end is connected with the heating furnace 50, and the fourth desorption gas outlet end is connected with the steelmaking workshop 90 so as to send the fourth desorption gas into the steelmaking workshop 90 for CO 2 steelmaking;
The heating furnace 50 is used for heating hydrogen, converter decarburization gas, recycle gas and blast furnace decarburization gas, and the hydrogen and the recycle gas are mixed with the converter decarburization gas and/or the blast furnace decarburization gas in the heating furnace 50 to form hydrogen-based shaft furnace reducing gas; the heating furnace 50 is provided with a hydrogen-based shaft furnace reducing gas outlet end, the hydrogen-based shaft furnace reducing gas outlet end is connected with a hydrogen-based shaft furnace 60, and the hydrogen-based shaft furnace 60 adopts the hydrogen-based shaft furnace reducing gas to produce sponge iron;
the blast furnace 70 performs low-carbon smelting by using the first stripping gas to produce liquid molten iron.
In summary, the technology provided by the embodiment of the invention provides a new low-carbon and high-efficiency hydrogen metallurgy method for solving the technical problems of secondary energy consumption and high-investment reforming conversion in steel mills, and has great significance in reducing primary energy consumption of a hydrogen-based shaft furnace and reducing carbon emission of the shaft furnace.
The following specific exemplary examples illustrate the invention in detail. It is also to be understood that the following examples are given solely for the purpose of illustration and are not to be construed as limitations upon the scope of the invention, as many insubstantial modifications and variations are within the scope of the invention as would be apparent to those skilled in the art in light of the foregoing disclosure. The specific process parameters and the like described below are also merely examples of suitable ranges, i.e., one skilled in the art can make a suitable selection from the description herein and are not intended to be limited to the specific values described below.
Example 1
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 144647Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 60% of the heat value of the coke oven gas, the gas quantity is 68500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.45 times of that of the coke oven gas, the gas quantity is 76147Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa.
The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 32%. The coke ratio of the blast furnace is reduced by 50kg/tHM, and the emission of CO 2 is reduced by 13.3%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 93252Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas quantity is 73500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 19752Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 38.6%, a CO content of 12.2%, a gas quantity of 299064Nm 3/h, a gas pressure of 0.26MPa and a temperature of 507 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 15.4% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 412 ℃.
The heat value of the recycled gas is 1.35 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 149835Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 87.7% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 58113Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55.8%, the H 2/CO is 3.2, the gas quantity is 295824Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 2.0 percent.
Example 2
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 161540Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 76500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 85040Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while the blowing, wherein the oxygen enrichment rate is 39%. The coke ratio of the blast furnace is reduced by 60kg/tHM, and the emission of CO 2 is reduced by 16%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 67243Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas flow is 53000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 14243Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 47.3%, a CO content of 9.2%, a gas quantity of 294491Nm 3/h, a gas pressure of 0.26MPa and a temperature of 484 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 14.5% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 389 ℃.
The heat value of the recycled gas is 1.37 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 157531Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 82.3% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 44190Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 66.5%, the H 2/CO is 5.1, the gas quantity is 291505Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 1.3 percent.
Example 3
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 171043Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 81000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 90043Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 44%. The coke ratio of the blast furnace is reduced by 68kg/tHM, and the CO 2 emission is reduced by 18.1%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 51384Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas quantity is 40500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 10884Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 52.6%, a CO content of 7.3%, a gas quantity of 289212Nm 3/h, a gas pressure of 0.26MPa and a temperature of 466 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 14.2% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is raised to 371 ℃.
The heat value of the recycled gas is 1.38 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 160173Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 79.2% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 35346Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 73.2%, the H 2/CO is 7.2, the gas quantity is 286135Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 0.7 percent.
Example 4
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 186880Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 88500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 98380Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 52%. The coke ratio of the blast furnace is reduced by 73kg/tHM, and the CO 2 emission is reduced by 19.5%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 24740Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas quantity is 19500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 5240Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 63.2%, a CO content of 3.7%, a gas quantity of 287905Nm 3/h, a gas pressure of 0.26MPa and a temperature of 447 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 13.1% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 352 ℃.
The heat value of the recycled gas is 1.37 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 172011Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 74.3% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 20480Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 85.6%, the H 2/CO is 17.3, the gas quantity is 284559Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 0.3 percent.
Example 5
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon and low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 195960Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 92800Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 103160Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 57%. The coke ratio of the blast furnace is reduced by 76kg/tHM, and the CO 2 emission is reduced by 20.3%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas is 7232Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas flow is 5700Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 1532Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has hydrogen content of 71.8%, CO content of 1.1%, gas amount of 282312Nm 3/h, air pressure of 0.26MPa and temperature of 426 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 12.3% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 331 ℃.
The heat value of the recycled gas is 1.33 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 181078Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 70.3% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 10461Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 95.5%, the H 2/CO is 64.3, the gas quantity is 279736Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 0.2 percent.
Example 6
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 140424Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 66500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 73924Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 31%. The coke ratio of the blast furnace is reduced by 48kg/tHM, and the CO 2 emission is reduced by 12.8%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 93252Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas quantity is 73500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 19752Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 38.3%, a CO content of 12.1%, a gas quantity of 301836Nm 3/h, a gas pressure of 0.26MPa and a temperature of 512 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 13.7% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 417 ℃.
The heat value of the recycled gas is 1.35 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 154468Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 87.6% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 54086Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 15%, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 85%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55.2%, the H 2/CO is 3.2, the gas quantity is 299317Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 1.8 percent.
Example 7
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 137679Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 65200Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 72479Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 30%. The coke ratio of the blast furnace is reduced by 45kg/tHM, and the CO 2 emission is reduced by 12.0%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 93252Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.25 times of that of the converter gas, the gas quantity is 73500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 35% of the heat value of the converter gas, the gas quantity is 19752Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 38.2%, a CO content of 12.1%, a gas quantity of 30550Nm 3/h, a gas pressure of 0.26MPa and a temperature of 514 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 12.4% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 419 ℃.
The heat value of the recycled gas is 1.34 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 158906Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 87.5% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 51155Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 25%, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 75%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55.2%, the H 2/CO is 3.2, the gas quantity is 301185Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 1.6 percent.
Example 8
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 1, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 1, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 153094Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.45MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 72500Nm 3/h, the gas pressure is 0.4MPa, and the temperature after heating is 1050 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 80594Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.3MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 30%. The coke ratio of the blast furnace is reduced by 45kg/tHM, and the CO 2 emission is reduced by 12.0%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 100230Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.45MPa. The heat value of the converter decarburization gas is 1.05 times of that of the converter gas, the gas quantity is 79000Nm 3/h, the gas pressure is 0.4MPa, and the temperature after heating is 1050 ℃. The heat value of the second desorption gas is 40% of the heat value of the converter gas, the gas quantity is 21230Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 40.1%, a CO content of 12.7%, a gas quantity of 318767Nm 3/h, a gas pressure of 0.16MPa and a temperature of 534 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 17.1% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.45MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 439 ℃.
The heat value of the recycled gas is 1.32 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 159740Nm 3/h, the gas pressure is 0.4MPa, and the recycled gas is further heated to 1050 ℃. The third desorption gas heat value is 88.3% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 60510Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the decarbonizing gas of the converter and the recycle gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55.8%, the H 2/CO is 3.2, the gas quantity is 317686Nm 3/H, the gas pressure is 0.3MPa, and the temperature is 1050 ℃. The metallization rate of the sponge iron is more than or equal to 95 percent, and the carbon content is 1.9 percent.
Example 9
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 2, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 2, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 130922Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 62000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 68922Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 28%. The coke ratio of the blast furnace is reduced by 48kg/tHM, and the CO 2 emission is reduced by 12.8%.
(3) Blast furnace top gas treatment process
And (3) carrying out wet dust removal, pressurization and decarburization on part of blast furnace top gas to obtain blast furnace decarburization gas and fourth desorption gas, wherein the blast furnace decarburization gas is heated and then used as part of hydrogen-based shaft furnace reduction gas, and the fourth desorption gas is conveyed to a steelmaking workshop CO 2 for steelmaking. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas quantity of the blast furnace top gas is 109701Nm 3/h, the dust content after coarse dust removal is less than or equal to 6g/Nm 3, the dust content after wet dust removal is less than or equal to 5mg/Nm 3, the temperature is 40 ℃, and the pressure after pressurization is 0.55MPa. The heat value of the decarbonizing gas of the blast furnace is 1.4 times of that of the top gas of the blast furnace, the gas quantity is 73500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heating value of the fourth desorption gas is 19.4% of the heating value of the top gas of the blast furnace, the gas quantity is 36201Nm 3/h, the temperature is 40 ℃, and the air pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 42.8%, a CO content of 9.0%, a gas quantity of 299064Nm 3/h, a gas pressure of 0.26MPa and a temperature of 480 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 16% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 385 ℃.
The heat value of the recycled gas is 1.38 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 151173Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 79.3% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 47370Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the recycled gas and the blast furnace decarburization gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 61.2%, the H 2/CO is 4.8, the gas quantity is 291491Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 0.4 percent.
Example 10
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 2, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 2, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 192159Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 91000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 101159Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 56%. The coke ratio of the blast furnace is reduced by 76kg/tHM, and the CO 2 emission is reduced by 20.3%.
(3) Blast furnace top gas treatment process
And (3) carrying out wet dust removal, pressurization and decarburization on part of blast furnace top gas to obtain blast furnace decarburization gas and fourth desorption gas, wherein the blast furnace decarburization gas is heated and then used as part of hydrogen-based shaft furnace reduction gas, and the fourth desorption gas is conveyed to a steelmaking workshop CO 2 for steelmaking. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas amount of the top gas of the blast furnace is 8507Nm 3/h, the dust content after coarse dust removal is less than or equal to 6g/Nm 3, the dust content after wet dust removal is less than or equal to 5mg/Nm 3, the temperature is 40 ℃, and the pressure after pressurization is 0.55MPa. The heat value of the decarbonizing gas of the blast furnace is 1.5 times of that of the top gas of the blast furnace, the gas quantity is 5700Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heating value of the fourth desorption gas is 15% of the heating value of the top gas of the blast furnace, the gas quantity is 2807Nm 3/h, the temperature is 40 ℃, and the air pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 72.6%, a CO content of 1.0%, a gas quantity of 276087Nm 3/h, a gas pressure of 0.26MPa and a temperature of 417 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 12.4% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 322 ℃.
The heat value of the recycled gas is 1.33 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 176653Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 74% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 9128Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Hydrogen-based shaft furnace smelting process
The hydrogen, the recycled gas and the blast furnace decarburization gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 96.5%, the H 2/CO is 75, the gas quantity is 274495Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 1.2 percent.
Example 11
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 2, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 2, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 139368Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 70% of the heat value of the coke oven gas, the gas quantity is 66000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 1050 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.15 times of that of the coke oven gas, the gas quantity is 73368Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 30%. The coke ratio of the blast furnace is reduced by 45kg/tHM, and the CO 2 emission is reduced by 12%.
(3) Blast furnace top gas treatment process
And (3) carrying out wet dust removal, pressurization and decarburization on part of blast furnace top gas to obtain blast furnace decarburization gas and fourth desorption gas, wherein the blast furnace decarburization gas is heated and then used as part of hydrogen-based shaft furnace reduction gas, and the fourth desorption gas is conveyed to a steelmaking workshop CO 2 for steelmaking. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas quantity of the blast furnace top gas is 117910Nm 3/h, the dust content after coarse dust removal is less than or equal to 6g/Nm 3, the dust content after wet dust removal is less than or equal to 5mg/Nm 3, the temperature is 40 ℃, and the pressure after pressurization is 0.55MPa. The heat value of the decarbonizing gas of the blast furnace is 1.4 times of that of the top gas of the blast furnace, the gas quantity is 79000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 1050 ℃. The heating value of the fourth desorption gas is 19.5% of the heating value of the top gas of the blast furnace, the gas quantity is 38910Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 44.5%, a CO content of 9.5%, a gas quantity of 314693Nm 3/h, a gas pressure of 0.26MPa and a temperature of 504 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 17.6% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 409 ℃.
The heat value of the recycled gas is 1.35 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 162096Nm 3/h, the gas pressure is 0.5MPa, and the recycled gas is further heated to 1050 ℃. The third desorption gas heat value is 80.5% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 49769Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(5) Hydrogen-based shaft furnace smelting process
The hydrogen, the recycled gas and the blast furnace decarburization gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace was 63.8%, H 2/CO was 4.7, the gas flow was 304577Nm 3/H, the gas pressure was 0.4MPa, and the temperature was 1050 ℃. The metallization rate of the sponge iron is more than or equal to 95 percent, and the carbon content is 0.2 percent.
Example 12
The hydrogen metallurgy method for absorbing secondary energy in the steel plant adopts the system shown in fig. 3, and comprises the following specific steps:
(1) Coke oven gas treatment process
As shown in fig. 3, after pressurizing and extracting hydrogen from the purified coke oven gas, obtaining hydrogen and a first desorption gas, heating the hydrogen to be used as a part of the reducing gas of the hydrogen-based shaft furnace, and blowing the first desorption gas into the blast furnace through a tuyere after pressurizing to perform low-carbon smelting. The hydrogen extraction method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The gas amount of the coke oven gas was 139368Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the hydrogen is 65% of the heat value of the coke oven gas, the gas quantity is 66000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃.
(2) Blast furnace low-carbon smelting process
The heat value of the first desorption gas delivered to the blast furnace is 1.3 times of that of the coke oven gas, the gas quantity is 73368Nm 3/h, the temperature is 40 ℃, and the pressure after pressurization is 0.4MPa. The pressurized first desorption gas is blown into a blast furnace through a tuyere to carry out low-carbon smelting, and oxygen enrichment is carried out while blowing, wherein the oxygen enrichment rate is 28%. The coke ratio of the blast furnace is reduced by 48kg/tHM, and the CO 2 emission is reduced by 12.8%.
(3) Converter gas treatment process
Pressurizing and decarbonizing the purified converter gas to obtain converter decarbonizing gas and second desorption gas, heating the converter decarbonizing gas to serve as a part of the reducing gas of the hydrogen-based shaft furnace, and conveying the second desorption gas to a steel mill gas pipe network. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas flow of the converter gas was 50749Nm 3/h, the temperature was 40℃and the pressure after pressurization was 0.55MPa. The heat value of the converter decarburization gas is 1.17 times of that of the converter gas, the gas quantity is 40000Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heat value of the second desorption gas is 38% of the heat value of the converter gas, the gas quantity is 10749Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(4) Blast furnace top gas treatment process
And (3) carrying out wet dust removal, pressurization and decarburization on part of blast furnace top gas to obtain blast furnace decarburization gas and fourth desorption gas, wherein the blast furnace decarburization gas is heated and then used as part of hydrogen-based shaft furnace reduction gas, and the fourth desorption gas is conveyed to a steelmaking workshop CO 2 for steelmaking. The decarburization method may be any one or more of physical absorption method, chemical absorption method, and physical-chemical absorption method.
The gas quantity of the top gas of the blast furnace is 50000Nm 3/h, the dust content after coarse dust removal is less than or equal to 6g/Nm 3, the dust content after wet dust removal is less than or equal to 5mg/Nm 3, the temperature is 40 ℃, and the pressure after pressurization is 0.55MPa. The heat value of the decarbonizing gas of the blast furnace is 1.5 times of that of the top gas of the blast furnace, the gas quantity is 33500Nm 3/h, the gas pressure is 0.5MPa, and the temperature after heating is 950 ℃. The heating value of the fourth desorption gas is 15.2% of the heating value of the top gas of the blast furnace, the gas quantity is 16500Nm 3/h, the temperature is 40 ℃, and the air pressure is 0.02MPa.
(5) Top gas circulation process of hydrogen-based shaft furnace
And (3) dedusting, heat exchanging, pressurizing, decarbonizing and denitrifying the top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas, wherein the recycle gas is heated and then used as part of the reducing gas of the hydrogen-based shaft furnace, and one part of the third stripping gas is used as fuel gas for heating the reducing gas, and the other part of the third stripping gas is conveyed to a steel mill gas pipe network. The decarbonization and denitrification method can be any one or more of physical absorption method, chemical absorption method and physical-chemical absorption method.
The top gas of the hydrogen-based shaft furnace has a hydrogen content of 40%, a CO content of 10.7%, a gas quantity of 296052Nm 3/h, a gas pressure of 0.26MPa and a temperature of 417 ℃; the dust content of the top gas of the hydrogen-based shaft furnace after coarse dust removal is less than or equal to 6g/Nm 3, and the dust content of the top gas of the hydrogen-based shaft furnace after dry dust removal is less than or equal to 5mg/Nm 3; the temperature of the top gas of the hydrogen-based shaft furnace is reduced to be less than or equal to 40 ℃ after two-stage heat exchange with the recycled gas and cooling water; 15.8% of the top gas of the hydrogen-based shaft furnace after heat exchange is used as fuel gas for heating the reducing gas; pressurizing the rest part of the top gas of the hydrogen-based shaft furnace after heat exchange, and raising the air pressure to 0.55MPa; the recycled gas after decarbonizing and denitriding is subjected to primary heat exchange with the top gas of the hydrogen-based shaft furnace after dedusting, and the temperature of the recycled gas is increased to 402 ℃.
The heat value of the recycled gas is 1.37 times of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 149338Nm 3/h, the gas pressure is 0.5MPa, and the furnace is further heated to 950 ℃. The third desorption gas heat value is 84.3% of the heat value of the top gas of the hydrogen-based shaft furnace, the gas quantity is 53451Nm 3/h, the temperature is 40 ℃, and the gas pressure is 0.02MPa.
(6) Hydrogen-based shaft furnace smelting process
The hydrogen, the converter decarbonization gas, the recycle gas and the blast furnace decarbonization gas are mixed and heated to become the reducing gas of the hydrogen-based shaft furnace, and qualified sponge iron is produced. The fuel gas heated by the reducing gas is hydrogen-based shaft furnace top gas subjected to third stripping gas and heat exchange, the volume fraction of the third stripping gas is 0, and the volume fraction of the hydrogen-based shaft furnace top gas subjected to heat exchange is 100%.
The hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 58.1%, the H 2/CO is 3.6, the gas quantity is 293316Nm 3/H, the gas pressure is 0.4MPa, and the temperature is 950 ℃. The metallization rate of the sponge iron is more than or equal to 93 percent, and the carbon content is 1.8 percent.
The above embodiments are merely illustrative of the principles of the present invention and its effectiveness, and are not intended to limit the invention. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the invention. Accordingly, it is intended that all equivalent modifications and variations of the invention be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.
Claims (15)
1. A hydrogen metallurgy method for absorbing secondary energy in a steel mill, comprising:
Carrying out hydrogen extraction treatment on coke oven gas to obtain hydrogen and a first desorption gas, and blowing the first desorption gas into a blast furnace to carry out low-carbon smelting to produce liquid molten iron;
Decarburization treatment is carried out on the converter gas to obtain converter decarburization gas and second stripping gas; decarburizing and denitrifying a part of top gas of the hydrogen-based shaft furnace to obtain recycle gas and third stripping gas;
Decarburizing a part of the blast furnace top gas to obtain blast furnace decarburization gas and fourth stripping gas;
mixing the hydrogen and the recycle gas, and mixing the mixture with the converter decarburization gas and/or the blast furnace decarburization gas to jointly serve as hydrogen-based shaft furnace reducing gas for producing sponge iron.
2. The method of claim 1, further comprising at least one of the following operations ① to ④:
① Conveying the second desorption gas to a steel mill gas pipe network;
② Using a portion of the third stripping gas as a fuel gas for heating the hydrogen-based shaft furnace reducing gas;
③ Delivering the fourth stripping gas to a steelmaking plant;
④ Another portion of the hydrogen-based shaft furnace top gas is used as fuel gas for heating the hydrogen-based shaft furnace reduction gas.
3. The method of claim 2, wherein the operation ② further comprises: delivering the other part of the third desorption gas to a steel mill gas pipe network;
And/or, the operations ④ further include: the other part of the top gas of the hydrogen-based shaft furnace, which is used as the fuel gas for heating the reduction gas of the hydrogen-based shaft furnace, accounts for 12.0 to 17.1 percent of the volume of the total top gas of the hydrogen-based shaft furnace;
And/or, when the method further comprises operations ② and ④, the volume fraction of the other portion of the top gas of the hydrogen-based shaft furnace in the fuel gas is greater than or equal to 75%, and the volume fraction of the third stripping gas is greater than or equal to 25%.
4. The method of claim 1 or 2, further comprising a pretreatment comprising at least one of a purification, dust removal, pressurization, heat exchange treatment;
the purification treatment is selected from at least one of the following operations ⑤ to ⑥:
⑤ Purifying the coke oven gas before hydrogen extraction treatment;
⑥ Purifying converter gas before decarburizing the converter gas;
The dust removal treatment is selected from at least one of the following operations ⑦ to ⑧:
⑦ Dedusting a portion of the hydrogen-based shaft furnace top gas before it is subjected to a decarbonizing denitrification process and before another portion of the hydrogen-based shaft furnace top gas is used as a fuel gas for heating the hydrogen-based shaft furnace reducing gas;
⑧ Before decarburizing a part of blast furnace top gas, carrying out dust removal treatment on the blast furnace top gas;
The pressurizing treatment is selected from the following operations ⑨ to ⑨ At least one of:
⑨ Pressurizing coke oven gas before hydrogen extraction treatment;
⑩ Pressurizing the first stripping gas before blowing the first stripping gas into a blast furnace for low-carbon smelting;
Pressurizing the converter gas before decarburizing the converter gas;
pressurizing a portion of the top gas of the hydrogen-based shaft furnace prior to decarbonizing and denitrifying the portion;
pressurizing a portion of the blast furnace top gas prior to decarburizing it;
the heat exchange treatment mode comprises the following steps: a portion of the hydrogen-based shaft furnace top gas is heat exchanged prior to decarbonizing and denitrifying it and prior to using another portion of the hydrogen-based shaft furnace top gas as a fuel gas for heating the hydrogen-based shaft furnace reduction gas.
5. The method according to claim 4, wherein: the heat exchange treatment mode comprises the following steps: the temperature of the top gas of the hydrogen-based shaft furnace is reduced to 40 ℃ and below by heat exchange.
6. The method according to claim 4, wherein: the heat exchange treatment mode is heat exchange, the heat exchange mode comprises multi-stage heat exchange, the multi-stage heat exchange comprises primary heat exchange and secondary heat exchange, and the primary heat exchange mode comprises the following steps: heat exchanging the hydrogen-based shaft furnace top gas with the recycle gas, the secondary heat exchanging comprising: and carrying out heat exchange on the top gas of the hydrogen-based shaft furnace subjected to primary heat exchange and the cooling liquid.
7. The method according to claim 1, characterized in that: the method further comprises the steps of: and before the hydrogen gas and the recycle gas are mixed and are mixed with the converter decarburization gas and/or the blast furnace decarburization gas to be jointly used as the hydrogen-based shaft furnace reducing gas for producing the sponge iron, heating the hydrogen gas, the recycle gas, the converter decarburization gas and the blast furnace decarburization gas.
8. The method according to claim 1, characterized in that: the hydrogen content of the reducing gas of the hydrogen-based shaft furnace is 55-96.5%, H 2/CO is more than or equal to 3, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the reducing gas amount of the hydrogen-based shaft furnace is 274000 ～ 317000Nm 3/H, the air pressure is 0.3-0.4 MPa, the temperature is 950-1050 ℃, the metallization rate of the sponge iron in the hydrogen-based shaft furnace is 93-95%, and the carbon content is 0.2-2.0%.
9. The method according to claim 8, wherein: when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the coke oven gas is 137000 ～ 196000Nm 3 per hour, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after the coke oven gas is subjected to hydrogen extraction treatment, the heat value of the obtained hydrogen is 60-70% of the heat value of the coke oven gas, the gas quantity is 65000-93000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃;
And/or when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the converter gas is 7200-100000 Nm 3/h, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after decarburization treatment is carried out on the converter gas, the heat value of the obtained converter decarburization gas is 1.05-1.25 times of that of the converter gas, the gas quantity is 5700-79000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃;
And/or when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the hydrogen content of the top gas of the hydrogen-based shaft furnace is 38-72%, the CO content is 1-13%, the gas quantity is 276000 ～ 319000Nm 3/h, the air pressure is 0.16-0.26 MPa, and the temperature is 417-534 ℃; after decarburization and denitrification treatment is carried out on a part of the top gas of the hydrogen-based shaft furnace, the heat value of the obtained recycled gas is 1.32-1.38 times that of the part of the top gas of the hydrogen-based shaft furnace, the gas quantity is 149000 ～ 181000Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃;
And/or, when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of a part of blast furnace top gas is 8500-110000 Nm 3/h, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after decarburization treatment is carried out on a part of blast furnace top gas, the heat value of the obtained blast furnace decarburization gas is 1.39-1.55 times that of the part of blast furnace top gas, the gas quantity is 5700-79000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃.
10. The method according to claim 9, wherein: when the yield of the hydrogen-based shaft furnace is 100 ten thousand tons of sponge iron per year, the gas amount of the coke oven gas is 137000 ～ 196000Nm 3 per hour, the temperature is 20-50 ℃, and the pressure after pressurization is 0.45-0.55 MPa; after the coke oven gas is subjected to hydrogen extraction treatment, the heat value of the obtained hydrogen is 60-70% of the heat value of the coke oven gas, the gas quantity is 65000-93000 Nm 3/h, the gas pressure is 0.4-0.5 MPa, and the temperature after heating is 950-1050 ℃; the heat value of the obtained first desorption gas is 1.15-1.45 times of the heat value of the coke oven gas, the gas quantity is 72000-104000 Nm 3/h, and the temperature is 20-50 ℃; the first desorption gas is blown into a blast furnace through a tuyere after being pressurized to carry out low-carbon smelting, oxygen enrichment is carried out while blowing, the oxygen enrichment rate is 28-57%, the coke ratio of the blast furnace is reduced by 45-76 kg/tHM, and the emission amount of CO 2 is reduced by 12-20%.
11. A hydrogen metallurgy system for absorbing secondary energy of a steel mill is characterized in that: the system comprises a coke oven gas treatment unit, a hydrogen-based shaft furnace top gas recycling unit, a heating furnace, a hydrogen-based shaft furnace and a blast furnace, and further comprises a converter gas treatment unit and/or a blast furnace top gas treatment unit;
The coke oven gas treatment unit comprises a hydrogen extracting device, wherein the hydrogen extracting device is used for extracting hydrogen from the coke oven gas, dividing the coke oven gas into hydrogen and a first desorption gas, and is provided with a hydrogen outlet end and a first desorption gas outlet end, and the hydrogen outlet end is connected with the heating furnace;
The converter gas treatment unit comprises a first decarburization device, wherein the first decarburization device is used for decarburizing converter gas, dividing the converter gas into converter decarburization gas and second stripping gas, and is provided with a converter decarburization gas outlet end, and the converter decarburization gas outlet end is connected with the heating furnace;
The hydrogen-based shaft furnace top gas recycling unit comprises a decarburization and denitrification device, wherein the decarburization and denitrification device is used for removing CO 2 and N 2 from the hydrogen-based shaft furnace top gas, dividing the hydrogen-based shaft furnace top gas into recycle gas and third stripping gas, and is provided with a recycle gas outlet end, and the recycle gas outlet end is connected with the heating furnace;
The blast furnace top gas treatment unit comprises a second decarburization device, wherein the second decarburization device is used for decarburizing blast furnace top gas, dividing the blast furnace top gas into blast furnace decarburization gas and fourth stripping gas, and is provided with a blast furnace decarburization gas outlet end, and the blast furnace decarburization gas outlet end is connected with the heating furnace;
The heating furnace is used for heating hydrogen, converter decarburization gas, recycle gas and blast furnace decarburization gas, and the hydrogen and the recycle gas are mixed with the converter decarburization gas and/or the blast furnace decarburization gas in the heating furnace to form hydrogen-based shaft furnace reducing gas; the heating furnace is provided with a hydrogen-based shaft furnace reducing gas outlet end, the hydrogen-based shaft furnace reducing gas outlet end is connected with the hydrogen-based shaft furnace, and the hydrogen-based shaft furnace adopts the hydrogen-based shaft furnace reducing gas to produce sponge iron;
The first desorption gas outlet end is connected with the blast furnace, and the blast furnace adopts the first desorption gas to carry out low-carbon smelting to produce liquid molten iron.
12. The system of claim 11, further comprising at least one of the following devices: the system comprises a gas pipe network, a steelmaking workshop, a first purifying device, a second purifying device, a first dust removing device, a second dust removing device, a first pressurizing machine, a second pressurizing machine, a third pressurizing machine, a fourth pressurizing machine, a fifth pressurizing machine and a heat exchanging device;
the first decarbonization device is also provided with a second desorption gas outlet end which is connected with a gas pipe network so as to send the second desorption gas into the gas pipe network;
The decarbonization and denitrification device is also provided with a third desorption gas outlet end, the heating furnace is provided with a second fuel gas inlet end, and the third desorption gas outlet end is connected with the second fuel gas inlet end so as to send the third desorption gas into the heating furnace to be used as fuel gas for heating;
the third desorption gas outlet end is also connected with a gas pipe network so as to send the third desorption gas into the gas pipe network;
The second decarburization device is further provided with a fourth desorption gas outlet end which is connected with a steelmaking workshop so as to send the fourth desorption gas into the steelmaking workshop for CO 2 steelmaking;
the first purifying device is arranged before the hydrogen extracting device and is used for purifying the coke oven gas;
The second purifying device is arranged before the first decarburization device and is used for purifying the converter gas;
The first dust removing device is used for carrying out dust removing treatment on the top gas of the hydrogen-based shaft furnace; the second dust removing device is arranged before the second decarburization device and is used for carrying out dust removal treatment on the blast furnace top gas; the first pressurizing machine is used for pressurizing coke oven gas;
the fourth pressurizing machine is arranged between the hydrogen extracting device and the blast furnace and is used for pressurizing the first desorption gas;
The second pressurizing machine is used for pressurizing the purified converter gas; the third pressurizer is used for pressurizing the top gas of the hydrogen-based shaft furnace after heat exchange; the fifth pressurizing machine is used for pressurizing the top gas of the blast furnace after dust removal; the heat exchange device is used for carrying out heat exchange treatment on the top gas of the hydrogen-based shaft furnace.
13. The system according to claim 12, wherein: the heat exchange device comprises a multi-stage heat exchanger, the multi-stage heat exchanger comprises a primary heat exchanger and a secondary heat exchanger which are sequentially connected, the primary heat exchanger is connected with the outlet end of the recycle gas and is used for heat exchange between the recycle gas and the top gas of the hydrogen-based shaft furnace, and the secondary heat exchanger is used for heat exchange between the cooling liquid and the top gas of the hydrogen-based shaft furnace.
14. The system according to claim 11, wherein: the heating furnace is also provided with a first fuel gas inlet end, and the first fuel gas inlet end is an inlet for feeding the top gas of the hydrogen-based shaft furnace into the heating furnace so as to feed the top gas of the hydrogen-based shaft furnace into the heating furnace as fuel gas for heating.
15. Use of the method according to any one of claims 1 to 10 and/or the system according to any one of claims 11 to 14 in the field of hydrogen metallurgy.
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