CN220468012U - Supply device of oxygen-enriched air of blast furnace - Google Patents
Supply device of oxygen-enriched air of blast furnace Download PDFInfo
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- CN220468012U CN220468012U CN202322107750.6U CN202322107750U CN220468012U CN 220468012 U CN220468012 U CN 220468012U CN 202322107750 U CN202322107750 U CN 202322107750U CN 220468012 U CN220468012 U CN 220468012U
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 239000001301 oxygen Substances 0.000 title claims abstract description 122
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 122
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 172
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 86
- 239000007788 liquid Substances 0.000 claims abstract description 85
- 239000007789 gas Substances 0.000 claims abstract description 41
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 20
- 230000001105 regulatory effect Effects 0.000 claims description 36
- 238000004821 distillation Methods 0.000 claims description 18
- 238000009833 condensation Methods 0.000 claims description 12
- 230000005494 condensation Effects 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 12
- 238000000034 method Methods 0.000 abstract description 17
- 230000008569 process Effects 0.000 abstract description 16
- 238000000926 separation method Methods 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000002485 combustion reaction Methods 0.000 description 23
- 238000001179 sorption measurement Methods 0.000 description 14
- 239000002994 raw material Substances 0.000 description 11
- 239000000446 fuel Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 4
- 230000007547 defect Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000012856 packing Methods 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 230000002950 deficient Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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Abstract
The utility model relates to a supply device of blast furnace oxygen-enriched air, which comprises a first air conveying main pipe and a main rectifying tower, wherein the main rectifying tower comprises a main rectifying upper tower, a main condensing evaporator and a main rectifying lower tower, one side of the main rectifying tower is provided with an auxiliary tower, the auxiliary tower comprises an auxiliary rectifying tower and a heat exchanger, the heat exchanger is communicated with the first air conveying main pipe through a first air conveying branch pipe, the heat exchanger is communicated with the main rectifying lower tower through a liquefied air pipe, the main rectifying lower tower is communicated with the auxiliary rectifying tower through a first liquid nitrogen conveying pipe, the first liquid nitrogen conveying pipe is provided with a first oxygen-enriched gas conveying pipe through a first liquid oxygen conveying pipe, the first oxygen-enriched gas conveying pipe is provided with a first online chromatograph, and the heat exchanger is provided with a second liquid oxygen conveying pipe. The energy consumption required by the large-scale air separation system for producing oxygen is reduced, and the intermittent supply can be realized by meeting the process requirement of a blast furnace. The utility model is convenient to adjust and use and has wide market prospect.
Description
Technical Field
The utility model relates to the field of supply equipment of oxygen-enriched air of a blast furnace, in particular to a supply device of oxygen-enriched air of the blast furnace.
Background
The fuel combustion is a severe oxidation reaction of fuel and combustion improver which generates heat and light under certain conditions. The common fuel combustion uses air as combustion improver, the oxygen content in the air participating in the combustion reaction is only 21%, the nitrogen content not participating in the combustion reaction is as high as 79%, and the nitrogen absorbs a large amount of combustion reaction heat and is finally discharged into the atmosphere along with the flue gas, so that great energy waste is caused. The oxygen-enriched combustion is the combustion of fuel with oxygen content greater than 21% in the combustion improver. The combustion mode improves the content of useful oxygen in the combustion improver, reduces the content of useless component nitrogen in the combustion improver, and has positive significance for stabilizing the combustion process, improving the combustion efficiency and improving the heat transfer in the furnace.
According to the basic theoretical knowledge of fuel combustion, basic characteristics of combustion such as combustion reaction speed, air consumption coefficient, combustion product generation amount, theoretical combustion temperature and the like when the oxygen content in combustion air is increased by using blast furnace gas as fuel are explained; the prior art is realized by mixing oxygen with air with high concentration to form oxygen-enriched air, and then delivering the oxygen-enriched air into a blast furnace for supporting combustion. According to the running condition of the blast furnace, the blast furnace is heated intermittently, and two modes of intermittent supply of high-concentration oxygen are adopted, wherein the first mode is from oxygen produced by pressure swing adsorption; second oxygen produced by a large-scale rectification air separation system; the first oxygen produced by pressure swing adsorption depends on the corresponding adsorption packing, the adsorption capacity of the corresponding adsorption packing gradually decreases along with the adsorption and desorption times, and when the adsorption capacity of the corresponding adsorption packing decreases to a preset value, the adsorption capacity of the corresponding adsorption packing needs to be replaced, and although pressure swing adsorption can realize intermittent supply along with the operation of a blast furnace process, the pressure swing adsorption is basically higher in production cost of high-concentration oxygen per unit volume compared with a large-scale rectification air separation system and is not applicable to large enterprises; however, for small enterprises, the pressure swing adsorption process for producing high-concentration oxygen is simpler, and the maintenance is convenient and relatively more applicable.
The oxygen produced by the large-scale rectification air separation system has lower production cost per unit volume relative to pressure swing adsorption, but the process is continuous due to the limited process of the large-scale rectification air separation system; the process of blast furnace production is intermittent, oxygen supply is continuously carried out no matter whether the blast furnace works or not, the waste is avoided, and the oxygen content of the oxygen-enriched air serving as the auxiliary fuel gas is only required to be more than 21% according to the oxygen-enriched combustion theory; the oxygen produced by the large-scale rectification air separation system meets the requirement of GB/T3863-2008 industrial oxygen, the raw materials for producing oxygen by rectification are compressed air after cooling and purifying, the normal air separation process is particularly used as a lower tower in a high-pressure environment to form two raw materials which are supplied to an upper tower, namely oxygen-enriched liquid air, and the liquid nitrogen is supplied to the upper tower through a heat source channel of a main condensing heat exchanger of the lower tower to form high pressure of the oxygen-enriched liquid air, so that the supply pressure of the compressed air is not less than the pressure of the lower tower, and the pressure of the compressed air is high, thereby leading to high energy consumption of the whole large-scale rectification air separation system.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model provides a supply device of blast furnace oxygen-enriched air, which can reduce the energy consumption required by the production of oxygen by a large-scale air separation system and can meet the process requirements of a blast furnace for intermittent supply, and is used for overcoming the defects in the prior art.
The utility model adopts the technical scheme that: the utility model provides a blast furnace oxygen-enriched air's supply arrangement, includes first air delivery main pipe and main rectifying column, main rectifying column from last to including main rectifying upper tower, main condensation evaporator and main rectifying lower tower down in proper order, one side of main rectifying column be provided with the auxiliary column, the auxiliary column from last to including the auxiliary rectifying column in proper order and the cold source passageway of the heat exchanger that is linked together with auxiliary rectifying column bottom, the heat source passageway of heat exchanger is linked together through first air delivery branch pipe with first air delivery main pipe, the heat source passageway of heat exchanger is linked together through the liquefied air pipe with main rectifying lower tower, main rectifying lower tower is linked together through first liquid nitrogen conveyer pipe with auxiliary rectifying tower, auxiliary rectifying column and main condensation evaporator below the first liquid nitrogen conveyer pipe are linked together through first liquid oxygen conveyer pipe, be provided with first oxygen-enriched gas conveyer pipe on the auxiliary rectifying column, be provided with first online chromatograph on the first oxygen-enriched gas conveyer pipe, be provided with the second liquid oxygen conveyer pipe on the heat exchanger cold source passageway.
Preferably, the bottom of the main distillation upper tower is communicated with the main distillation lower tower through an oxygen-enriched liquid air conveying pipe, a second regulating valve is arranged on the oxygen-enriched liquid air conveying pipe, a heat source channel of the main condensation evaporator is communicated with the main distillation upper tower through a second liquid nitrogen conveying pipe, a third regulating valve is arranged on the second liquid nitrogen conveying pipe, a second liquid nitrogen conveying pipe between the third regulating valve and the main condensation evaporator is communicated with the main distillation lower tower through a fourth liquid nitrogen conveying pipe, and a fourth regulating valve is arranged on the fourth liquid nitrogen conveying pipe.
Preferably, the device further comprises a gas mixer, the gas mixer comprises a tank body, a second oxygen-enriched gas conveying pipe, a gas guide cone and mixing blades, wherein the second oxygen-enriched gas conveying pipe, the gas guide cone and the mixing blades are sequentially arranged from the inlet end of the tank body to the outlet end of the tank body, the mixing blades are in a plurality, the inlet end of the tank body is communicated with a second air conveying main pipe, the first oxygen-enriched gas conveying pipe is communicated with the second oxygen-enriched gas conveying pipe, a fifth regulating valve is arranged on the first oxygen-enriched gas conveying pipe, and a third air conveying main pipe is arranged on the outlet end of the tank body.
Preferably, the first liquid nitrogen conveying pipe and the first liquid nitrogen conveying pipe are respectively and sequentially provided with a sixth regulating valve and a liquid flow sensor along the direction from the auxiliary rectifying tower to the auxiliary rectifying tower.
Preferably, the first air conveying main pipe is communicated with the main rectifying upper tower through a second air conveying branch pipe, the first air conveying main pipe is communicated with the main rectifying lower tower through a third air conveying branch pipe, seventh regulating valves are respectively arranged on the second air conveying branch pipe and the third air conveying branch pipe, and a turbine expander is arranged on the second air conveying branch pipe between the seventh regulating valve arranged on the second air conveying branch pipe and the main rectifying upper tower.
Preferably, the main rectifying upper tower is provided with a first dirty nitrogen conveying pipe, the oxygen-enriched liquid air conveying pipe and the second liquid nitrogen conveying pipe are provided with a subcooler, and the first dirty nitrogen conveying pipe and the auxiliary rectifying tower are communicated with each other through the second dirty nitrogen conveying pipe between the subcooler and the main rectifying upper tower.
Preferably, the second air conveying main pipe is provided with an air filter and a ninth regulating valve in sequence along the direction from the tank body to the tank body, and the third air conveying main pipe is provided with a gas flow sensor, a fan and a second online chromatograph.
The utility model has the beneficial effects that: firstly, the utility model realizes the reduction of the pressure of the compressed air used as the rectifying raw material through the product, thereby realizing the reduction of the energy of the compressed air in a proper pressure range and saving energy; the product overcomes the defect that the large-scale rectifying equipment in the prior art is generally used for continuously supplying oxygen, and can realize intermittent oxygen supply according to the requirement of the blast furnace for supplying air; when the blast furnace does not need to supply air, liquid oxygen is supplied to the outside through the second liquid oxygen delivery pipe as an oxygen component product, and the normal rectification air separation process is not influenced.
And secondly, the air filter and the ninth regulating valve are sequentially arranged on the second air conveying main pipe along the direction from the tank body to the tank body, and the air filter is arranged to facilitate the filtration of particulate matters carried by air entering the second air conveying main pipe.
Finally, the bottom of the heat exchanger cold source channel and the bottom of the main rectifying lower tower are respectively provided with liquid level sensors; the liquid level sensor is arranged to facilitate feedback of the liquid level.
The utility model has the advantages of simple structure, convenient operation, ingenious design, great improvement of working efficiency, good social and economic benefits and easy popularization and use.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
Fig. 2 is an enlarged partial schematic view of detail a of fig. 1.
Fig. 3 is an enlarged partial schematic view of detail B of fig. 1.
Fig. 4 is a schematic cross-sectional structure of the can body.
Detailed Description
As shown in fig. 1 to 4, a supply device of oxygen-enriched air of a blast furnace comprises a first air conveying main pipe 1, a main rectifying tower and a main heat exchanger 2 for gas heat exchange, wherein the main rectifying tower sequentially comprises a main rectifying upper tower 3, a main condensing evaporator 4 and a main rectifying lower tower 5 from top to bottom, a second nitrogen conveying pipe 45 is arranged on the main rectifying lower tower 5, and the second nitrogen conveying pipe 45 is used for conveying pure nitrogen; one side of the main rectifying tower is provided with an auxiliary tower, the auxiliary tower sequentially comprises an auxiliary rectifying tower 6 and a cold source channel of a heat exchanger 7 communicated with the bottom of the auxiliary rectifying tower 6 from top to bottom, a heat source channel of the heat exchanger 7 is communicated with a first air conveying main pipe 1 through a first air conveying branch pipe 8, a heat source channel of the heat exchanger 7 is communicated with a main rectifying lower tower 5 through a liquefied air pipe 9, the main rectifying lower tower 5 is communicated with the auxiliary rectifying tower 6 through a first liquid nitrogen conveying pipe 10, the auxiliary rectifying tower 6 below the first liquid nitrogen conveying pipe 10 and a main condensing evaporator 4 are communicated through a first liquid oxygen conveying pipe 11, a first oxygen-enriched gas conveying pipe 12 is arranged on the auxiliary rectifying tower 6, a first online chromatograph 13 is arranged on the first oxygen-enriched gas conveying pipe 12, a second liquid oxygen conveying pipe 14 is arranged on the heat exchanger 7 cold source channel, and a first liquefied air pipe 9, a first oxygen-enriched gas conveying pipe 12 and a second liquid oxygen conveying pipe 14 are respectively provided with a first regulating valve 15. The bottom of the main distillation upper tower 3 is communicated with the main distillation lower tower 5 through an oxygen-enriched liquid air conveying pipe 16, a second regulating valve 17 is arranged on the oxygen-enriched liquid air conveying pipe 16, a heat source channel of the main condensation evaporator 4 is communicated with the main distillation upper tower 3 through a second liquid nitrogen conveying pipe 18, a third regulating valve 19 is arranged on the second liquid nitrogen conveying pipe 18, the second liquid nitrogen conveying pipe 18 between the third regulating valve 19 and the main condensation evaporator 4 is communicated with the main distillation lower tower 5 through a fourth liquid nitrogen conveying pipe 20, and a fourth regulating valve 21 is arranged on the fourth liquid nitrogen conveying pipe 20. The main rectifying upper tower 3 is provided with a first dirty nitrogen conveying pipe 38, the oxygen-enriched liquid air conveying pipe 16 and the second liquid nitrogen conveying pipe 18 are provided with a subcooler 39, and the first dirty nitrogen conveying pipe 38 and the auxiliary rectifying tower 6 between the subcooler 39 and the main rectifying upper tower 3 are communicated through a second dirty nitrogen conveying pipe 40. The oxygen-enriched liquid air conveyed by the oxygen-enriched liquid air conveying pipe 16 and the high-purity liquid nitrogen conveyed by the second liquid nitrogen conveying pipe 18 are further refrigerated by using the polluted nitrogen conveyed by the first polluted nitrogen conveying pipe 38 as a cold source, so that the polluted nitrogen is used as a cold source of the main rectifying upper tower 3.
The first nitrogen delivery pipe 36 is arranged between the main condensation evaporator 4 and the main rectification lower tower 5, and an eighth regulating valve 37 is arranged on the first nitrogen delivery pipe 36. The first air conveying main pipe 1 is communicated with the main rectifying upper tower 3 through a second air conveying branch pipe 32, the first air conveying main pipe 1 is communicated with the main rectifying lower tower 5 through a third air conveying branch pipe 33, seventh regulating valves 34 are respectively arranged on the second air conveying branch pipe 32 and the third air conveying branch pipe 33, and a turbine expander 35 is arranged on the second air conveying branch pipe 32 between the seventh regulating valve 34 arranged on the second air conveying branch pipe 32 and the main rectifying upper tower 3.
In addition, the product also comprises a gas mixer, the gas mixer comprises a tank body 22 and a second oxygen-enriched gas conveying pipe 23, an air guide cone 24 and mixing blades 25, wherein the second oxygen-enriched gas conveying pipe 23, the air guide cone 24 and the mixing blades 25 are sequentially arranged from the air inlet end of the tank body 22 to the air outlet end of the tank body 22, the mixing blades 25 are uniformly distributed in the inner cavity of the tank body 22 outside the central axis of the tank body 22 in a star shape, the air inlet end of the tank body 22 is communicated with a second air conveying main pipe 26, the first oxygen-enriched gas conveying pipe 12 is communicated with the second oxygen-enriched gas conveying pipe 23, a fifth regulating valve 27 is arranged on the first oxygen-enriched gas conveying pipe 12, and a third air conveying main pipe 28 is arranged on the air outlet end of the tank body 22. The compressed air which is conveyed into the tank body 22 by the second air conveying main pipe 26 is mixed by utilizing the oxygen which is provided by the first oxygen-enriched air conveying pipe 12, and the oxygen which is provided by the compressed air and the first oxygen-enriched air conveying pipe 12 is fully mixed by the guiding of the air guide cone 24 and the guiding of the mixing blades 25 to form oxygen-enriched air which is conveyed to the third air conveying main pipe 28 and then conveyed to the blast furnace.
Further, the second air delivery main pipe 26 is provided with an air filter 41 and a ninth regulating valve 42 in sequence along the direction from the tank 22 to the tank 22, and the third air delivery main pipe 28 is provided with a gas flow sensor 46, a fan 43 and a second online chromatograph 44. The third air delivery main 28 is provided with a gas flow sensor 46 to facilitate feedback of flow parameters of the gas delivered through the third air delivery main 28; the second in-line chromatograph 44 mounted on the third main air delivery conduit 28 facilitates feedback of the component parameters of the gas delivered through the third main air delivery conduit 28.
The heat exchanger 7 cold source channel and the bottom of the main rectification lower tower 5 are respectively provided with a liquid level sensor 29. The level sensor 29 is installed to facilitate feedback of the level height.
The first liquid nitrogen delivery pipe 10 and the first liquid nitrogen delivery pipe 10 are respectively and sequentially provided with a sixth regulating valve 30 and a liquid flow sensor 31 along the direction from the auxiliary rectifying tower 6 to the direction away from the auxiliary rectifying tower 6. The liquid flow sensor 31 is installed to facilitate feedback of the liquid flow.
The application method of the product is as follows: as shown in fig. 1 to 4, the compressed air subjected to the cooling process and the purifying process enters the first air delivery main 1 and is then divided into three parts: a first portion of compressed air enters the heat source channels of the heat exchanger 7 through the first air delivery manifold 8; the second part of compressed air enters the main rectifying upper tower 3 through the second air conveying branch pipe 32 to serve as a rectifying raw material of the main rectifying upper tower 3, and the temperature of the second part of compressed air entering the main rectifying upper tower 3 is reduced by expansion and cooling of the turbine expander 35 during the period; the third part of the compressed air is fed into the main rectifying lower column 5 through the third air conveying branch pipe 33 as the rectifying raw material of the main rectifying lower column 5.
The third part of compressed air enters the main distillation lower tower 5, and liquid nitrogen cooling oxygen components returned by a heat source channel of the main condensation evaporator 4 gradually fall to the bottom of the main distillation lower tower 5 to form an oxygen-enriched liquid air in a gradually ascending period, and the oxygen-enriched liquid air is sent to the main distillation upper tower 3 through an oxygen-enriched liquid air conveying pipe 16 to serve as a rectification raw material and serve as a cold source; the boiling point of the nitrogen component is lower, the nitrogen content in the gas in the main rectifying lower tower 5 gradually rises along with the rising of the height of the main rectifying lower tower 5, the high-content nitrogen at the top of the main rectifying lower tower 5 enters a heat source channel of the main condensing evaporator 4 and a medium in a cold source channel of the main condensing evaporator 4 for heat exchange, liquid nitrogen is formed after passing through the heat source channel of the main condensing evaporator 4 and is divided into two parts, and the first part of liquid nitrogen is used as reflux cooling liquid of the main rectifying lower tower 5 and flows back to the main rectifying lower tower 5 through a fourth liquid nitrogen conveying pipe 20; the second part of liquid nitrogen is sent to the main rectifying upper tower 3 through a second liquid nitrogen conveying pipe 18 and is used as one of cold source mediums of the main rectifying upper tower 3, part of oxygen-deficient liquid nitrogen extracted from the middle upper part of the main rectifying lower tower 5 is sent to the auxiliary rectifying tower 6 through a first liquid nitrogen conveying pipe 10, and the oxygen-deficient liquid nitrogen contains high-content nitrogen components and low-content oxygen components.
The second part of compressed air enters the main rectification upper tower 3 to rise gradually, and in the rising process, the second part of compressed air sequentially performs countercurrent heat exchange with the oxygen-enriched liquid air entering the main rectification upper tower 3 and performs countercurrent heat exchange with the liquid nitrogen entering the main rectification upper tower 3; as the height of the main upper rectifying tower 3 increases, the nitrogen content in the main upper rectifying tower 3 gradually increases, and the oxygen component in the main upper rectifying tower 3 gradually decreases, pure nitrogen is formed at the top of the main upper rectifying tower 3, and the medium forms first liquid oxygen after entering a cold source channel of the main condensing evaporator 4 through the bottom of the main upper rectifying tower 3; the first liquid oxygen enters the auxiliary rectifying tower 6 through the first liquid oxygen conveying pipe 11, impurity gas in the rectifying process of the main rectifying upper tower 3 forms first polluted nitrogen along with high-purity nitrogen, the first polluted nitrogen is conveyed outwards through the first polluted nitrogen conveying pipe 38, and the first polluted nitrogen is used as a cold source of the subcooler 39, is subjected to countercurrent heat exchange with oxygen-enriched liquid air serving as a first heat source of the subcooler 39 and liquid nitrogen serving as a second heat source of the subcooler 39, and then is continuously conveyed outwards along the first polluted nitrogen conveying pipe 38.
The first part of compressed air enters the heat source channel of the heat exchanger 7 and continuously exchanges heat with the medium continuously entering the cold source channel of the heat exchanger 7, and when the first part of compressed air passes through the heat source channel of the heat exchanger 7, liquid air is formed and is sent back to the main rectifying lower tower 5 through the liquefied air pipe 9, and the first part of compressed air is mixed with the continuously falling liquid medium to gradually fall and form oxygen-enriched liquid air in the main rectifying lower tower 5. The medium in the cold source channel of the heat exchanger 7 is continuously vaporized, and the liquid medium continuously ascends along the auxiliary rectifying tower 6 and sequentially exchanges heat with the first liquid oxygen entering the auxiliary rectifying tower 6 and exchanges heat with the oxygen-deficient liquid nitrogen entering the auxiliary rectifying tower 6 in a countercurrent manner; when the auxiliary rectifying tower 6 is started to a preset time, the nitrogen component in the auxiliary rectifying tower 6 gradually rises along with the increase of the height of the auxiliary rectifying tower 6, the oxygen component gradually descends along with the rise of the auxiliary rectifying tower 6 to finally form second liquid oxygen in a cold source channel of the heat exchanger 7 communicated with the bottom of the auxiliary rectifying tower 6, and second polluted nitrogen is formed at the bottom of the auxiliary rectifying tower 6 and conveyed to the first polluted nitrogen conveying pipe 38 through the second polluted nitrogen conveying pipe 40 to be combined with the first polluted nitrogen and then conveyed outwards along with the first polluted nitrogen. Oxygen with the oxygen content of the auxiliary rectifying tower 6 is conveyed outwards through the first oxygen-enriched gas conveying pipe 12, the time of the oxygen conveyed outwards through the first oxygen-enriched gas conveying pipe 12 is determined according to the requirement of a blast furnace gas supply process, when the first oxygen-enriched gas conveying pipe 12 is not required to convey oxygen outwards, the oxygen component produced by rectification of the auxiliary rectifying tower 6 is conveyed outwards along the second liquid oxygen conveying pipe 14 by taking second liquid oxygen formed in a cold source channel of the heat exchanger 7 as a final oxygen product, and when the first oxygen-enriched gas conveying pipe 12 conveys oxygen outwards, the amount of liquid conveyed outwards through the second liquid oxygen conveying pipe 14 can be reduced so as to meet the process requirement of conveying oxygen outwards through the first oxygen-enriched gas conveying pipe 12.
When oxygen-enriched air is required to be supplied according to the process requirement of the blast furnace, firstly, the blower 43 is opened, the opening degrees of the fifth regulating valve 27 and the ninth regulating valve 42 are regulated, the auxiliary rectifying tower 6 sequentially conveys oxygen to the tank body 22 through the first oxygen-enriched air conveying pipe 12 and the second oxygen-enriched air conveying pipe 23, meanwhile, as the blower 43 is opened, the opening degrees of the fifth regulating valve 27 and the ninth regulating valve 42 are regulated, external air is filtered through the air filter 41 and enters the second air conveying main pipe 26 to convey compressed air with normal oxygen content for supplying the blast furnace to the tank body 22, and the compressed air and the oxygen are fully mixed to form oxygen-enriched compressed air after the tank body 22 sequentially passes through the air guide cone 24 and the mixing blades 25, and are conveyed into the third air conveying main pipe 28 to be supplied to the blast furnace. During the process, the fan needs to compensate the temperature rise of the passing gas acting by the low-temperature oxygen, so that the heat loss required by the rewarming of the formed oxygen-enriched compressed gas is reduced.
Compared with the prior art, the product uses the raw material air which sequentially passes through the first air conveying main pipe 1 and the first air conveying branch pipe 8 and enters the heat exchanger 7 as a heat source of the heat exchanger 7, and exchanges heat with a medium entering a cold source channel of the heat exchanger 7 to form liquid air, the liquid air has lower energy required for acquiring the oxygen-enriched liquid air, and the generated liquid air is used as the raw material of the oxygen-enriched liquid air and nitrogen which are conveyed outwards by the main rectifying lower tower 5. The energy required by liquefaction is completely acquired in the rectification process of the auxiliary tower, so that the main rectification lower tower 5 can acquire liquid rectification raw materials, the pressure of the main rectification lower tower 5 is reduced, the pressure of raw material air supply is reduced, and the energy of compressed air in a proper pressure range is reduced.
According to the embodiment, the reduction of the pressure of the compressed air serving as the rectification raw material is realized through the product, so that the reduction of the energy of the compressed air in a proper pressure range is realized, and the energy saving is realized; the product overcomes the defect that the large-scale rectifying equipment in the prior art is generally used for continuously supplying oxygen, and can realize intermittent oxygen supply according to the requirement of the blast furnace for supplying air; when the blast furnace does not need to supply air, liquid oxygen is supplied to the outside through the second liquid oxygen delivery pipe 14 as an oxygen component product, and the normal rectification air separation process is not affected.
The above-described embodiments are merely preferred embodiments of the present utility model and are not intended to limit the scope of the present utility model, so that all equivalent changes or modifications of the structure, characteristics and principles described in the claims should be included in the scope of the present utility model.
Claims (7)
1. The utility model provides a blast furnace oxygen-enriched air's supply arrangement, includes first air delivery main pipe (1) and main rectifying column, main rectifying column from last tower (3), main condensation evaporator (4) and main rectifying lower column (5) of rectifying down of including in proper order, its characterized in that: one side of main rectifying column be provided with vice tower, vice tower from last to including vice rectifying column (6) and the cold source passageway of heat exchanger (7) that are linked together with vice rectifying column (6) bottom in proper order, the heat source passageway of heat exchanger (7) is linked together through first air conveying branch pipe (8) with first air conveying main pipe (1), the heat source passageway of heat exchanger (7) is linked together through liquefied air pipe (9) with main rectifying lower column (5), main rectifying lower column (5) are linked together through first liquid nitrogen conveyer pipe (10) with vice rectifying column (6), vice rectifying column (6) and main condensation evaporator (4) of first liquid nitrogen conveyer pipe (10) below are linked together through first liquid oxygen conveyer pipe (11).
2. The supply device of blast furnace oxygen-enriched air according to claim 1, wherein: the bottom of the main distillation upper tower (3) is communicated with the main distillation lower tower (5) through an oxygen-enriched liquid air conveying pipe (16), a second regulating valve (17) is arranged on the oxygen-enriched liquid air conveying pipe (16), a heat source channel of the main condensation evaporator (4) is communicated with the main distillation upper tower (3) through a second liquid nitrogen conveying pipe (18), a third regulating valve (19) is arranged on the second liquid nitrogen conveying pipe (18), the second liquid nitrogen conveying pipe (18) between the third regulating valve (19) and the main condensation evaporator (4) is communicated with the main distillation lower tower (5) through a fourth liquid nitrogen conveying pipe (20), and a fourth regulating valve (21) is arranged on the fourth liquid nitrogen conveying pipe (20).
3. The supply device of blast furnace oxygen-enriched air according to claim 1, wherein: the oxygen-enriched air mixing device comprises a tank body (22) and a plurality of mixing blades (25), wherein the tank body (22) comprises a tank body (22), a second oxygen-enriched air conveying pipe (23), an air guide cone (24) and the mixing blades (25) are sequentially arranged from the air inlet end of the tank body (22) to the air outlet end of the tank body (22), the air inlet end of the tank body (22) is communicated with a second air conveying main pipe (26), the first oxygen-enriched air conveying pipe (12) is communicated with the second oxygen-enriched air conveying pipe (23), a fifth regulating valve (27) is arranged on the first oxygen-enriched air conveying pipe (12), and a third air conveying main pipe (28) is arranged on the air outlet end of the tank body (22).
4. The supply device of blast furnace oxygen-enriched air according to claim 1, wherein: the first liquid nitrogen conveying pipe (10) and the first liquid nitrogen conveying pipe (10) are respectively and sequentially provided with a sixth regulating valve (30) and a liquid flow sensor (31) along the direction from the auxiliary rectifying tower (6) to the direction away from the auxiliary rectifying tower (6).
5. The supply device of blast furnace oxygen-enriched air according to claim 1, wherein: the first air conveying main pipe (1) is communicated with the main rectifying upper tower (3) through a second air conveying branch pipe (32), the first air conveying main pipe (1) is communicated with the main rectifying lower tower (5) through a third air conveying branch pipe (33), seventh regulating valves (34) are respectively arranged on the second air conveying branch pipe (32) and the third air conveying branch pipe (33), and a turbine expander (35) is arranged on the seventh regulating valve (34) arranged on the second air conveying branch pipe (32) and the second air conveying branch pipe (32) between the main rectifying upper tower (3).
6. The supply device of blast furnace oxygen-enriched air according to claim 2, wherein: the main distillation upper tower (3) is provided with a first dirty nitrogen conveying pipe (38), the oxygen-enriched liquid air conveying pipe (16) and the second liquid nitrogen conveying pipe (18) are provided with a subcooler (39), and the first dirty nitrogen conveying pipe (38) and the auxiliary distillation tower (6) are communicated with each other through a second dirty nitrogen conveying pipe (40) between the subcooler (39) and the main distillation upper tower (3).
7. A supply device of blast furnace oxygen-enriched air according to claim 3, characterized in that: the second air conveying main pipe (26) is provided with an air filter (41) and a ninth regulating valve (42) in sequence along the direction from the tank body (22) to the direction close to the tank body (22), and the third air conveying main pipe (28) is provided with a gas flow sensor (46), a fan (43) and a second online chromatograph (44).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322107750.6U CN220468012U (en) | 2023-08-07 | 2023-08-07 | Supply device of oxygen-enriched air of blast furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322107750.6U CN220468012U (en) | 2023-08-07 | 2023-08-07 | Supply device of oxygen-enriched air of blast furnace |
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| Publication Number | Publication Date |
|---|---|
| CN220468012U true CN220468012U (en) | 2024-02-09 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322107750.6U Active CN220468012U (en) | 2023-08-07 | 2023-08-07 | Supply device of oxygen-enriched air of blast furnace |
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| Country | Link |
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| CN (1) | CN220468012U (en) |
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