CN109798779B - Multistage separation heating method and device for furnace burden of direct-current submerged arc furnace hot charging - Google Patents
Multistage separation heating method and device for furnace burden of direct-current submerged arc furnace hot charging Download PDFInfo
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- CN109798779B CN109798779B CN201910076886.0A CN201910076886A CN109798779B CN 109798779 B CN109798779 B CN 109798779B CN 201910076886 A CN201910076886 A CN 201910076886A CN 109798779 B CN109798779 B CN 109798779B
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- 238000000926 separation method Methods 0.000 title claims abstract description 83
- 238000010438 heat treatment Methods 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 218
- 239000003546 flue gas Substances 0.000 claims abstract description 194
- 239000000463 material Substances 0.000 claims abstract description 110
- 238000003723 Smelting Methods 0.000 claims abstract description 20
- 239000000779 smoke Substances 0.000 claims description 69
- 239000002245 particle Substances 0.000 claims description 58
- 238000003860 storage Methods 0.000 claims description 27
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 24
- 238000007599 discharging Methods 0.000 claims description 19
- 238000005303 weighing Methods 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 238000002485 combustion reaction Methods 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000010881 fly ash Substances 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims 3
- 238000004519 manufacturing process Methods 0.000 description 21
- 229910000604 Ferrochrome Inorganic materials 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 6
- 238000005245 sintering Methods 0.000 description 6
- 229910001021 Ferroalloy Inorganic materials 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- 238000005453 pelletization Methods 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 229910045601 alloy Inorganic materials 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910000640 Fe alloy Inorganic materials 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- JOPOVCBBYLSVDA-UHFFFAOYSA-N chromium(6+) Chemical compound [Cr+6] JOPOVCBBYLSVDA-UHFFFAOYSA-N 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000002500 effect on skin Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Abstract
The invention relates to a furnace burden multistage separation heating method and a furnace burden multistage separation heating device for hot charging of a direct-current submerged arc furnace, which are characterized in that: it comprises the following steps: 1) Preheating cold air; 2) Comprehensive utilization of flue gas; 3) Multistage separation heating of cold furnace burden; 4) And (5) feeding hot materials. The structure of the device is as follows: the direct-current ore-smelting furnace comprises a cold material feeding assembly and a direct-current ore-smelting furnace, and is characterized in that: the hot material feeding device comprises a direct-current ore furnace, and is characterized by further comprising a cyclone separation assembly, a hot material feeding assembly, a burner assembly, an air heating assembly and an excessive flue gas discharge assembly, wherein the cyclone separation assembly and the hot material feeding assembly are sequentially arranged between the cold material feeding assembly and the direct-current ore furnace, an inlet of the burner assembly is connected with the ore furnace, an outlet of the burner assembly is connected with the cyclone separation assembly, a flue gas inlet pipe of the air heating assembly is connected with the cyclone separation assembly, a hot air outlet of the air heating assembly is connected with the burner assembly, and an inlet of the excessive flue gas discharge assembly is connected with the direct-current ore furnace, and an outlet of the excessive flue gas discharge assembly is led to the outside.
Description
Technical Field
The invention relates to metallurgical production technology and equipment, in particular to hot charging production and equipment of a direct-current submerged arc furnace, which are a furnace burden multistage separation heating method and a furnace burden multistage separation heating device for hot charging of the direct-current submerged arc furnace.
Background
In the world ferroalloy production process, raw material supply and production cost are always in the most important position. Over time, high-quality ferrochrome mineral resources are increasingly reduced, the environmental protection consciousness is enhanced, poor-quality ferrochrome mineral resources, particularly low-grade ferrochrome mineral resources are effectively utilized, and the reduction of production cost becomes a continuously pursued goal of ferroalloy manufacturers, and the development of submerged arc furnace production technology is mainly developed around the main line.
Submerged arc furnaces are widely used in ferrous alloys, nonferrous metals or other specialized industrial fields, starting from the first submerged arc furnace available worldwide from cimac, germany. Currently, most ferrochrome is produced in conventional ac submerged arc furnaces. In order to reduce production costs, ores are often preheated in rotary kilns, ring-heated furnaces (RHFs) or preheating shaft furnaces, and preheating, particularly the use of preheating shaft furnaces, reduces the power consumption of ac submerged arc furnaces.
The process and production equipment of the finnish eutolinsect, which possess pelletization, sintering and preheating patents, are widely used in the production of ferrochrome alloys from ferrochrome ores in south africa. The process comprises grinding, mixing, pelletizing, sintering and preheating, wherein the preheated furnace burden is fed into the submerged arc furnace by self gravity. The closed alternating current submerged arc furnace effectively collects CO-rich flue gas and is used as fuel for submerged arc furnaces and sintering furnaces. In the production process, pelletization/sintering accounts for 10% of the production cost, preheating accounts for 1%, smelting accounts for 89%, and the total production cost is lower than that of an open furnace or a semi-closed furnace for lump ore and powder ore.
Problems of alternating current submerged arc furnace technology are that: all three electrodes are part of the same circuit, one electrode presents a problem, and the cross-over effect between the electrodes can lead to a reduction in power factor. The self-baking electrode has the problem of skin effect related to alternating current, and when the diameter of the electrode is more than 1.2 m-1.5 m, the problem of repeated cracking of the electrode occurs. With the increase of global resource environmental pressure, carbon-containing fuel combustion power generation becomes dislike, future power production tends to be renewable energy, solar energy and wind energy become typical renewable energy, the number of renewable energy distributed power generation units is increased, intelligent power grid regulation is needed to be matched, power utilization households such as ferroalloy submerged arc furnaces are brought into demand side management, loads of the ferroalloy submerged arc furnaces must have adjustability, and alternating current submerged arc furnaces do not have the capability. In addition, the large amount of fine ore is used, and an expensive pelletizing process is needed to meet the production process requirements of different ferrochrome alloys, so that the investment cost of equipment is high and the utilization rate is low.
Compared with the traditional submerged-arc furnace, the direct-current submerged-arc furnace solves the problems of the alternating-current submerged-arc furnace, and has the advantages of direct adoption of low-cost powder ore, high molten pool temperature, high chromium metal reduction efficiency, almost zero chromium metal content in slag, lower total production cost than the traditional submerged-arc furnace, and no need of secondary metal recovery. In view of the lack of lump ore, the traditional submerged arc furnace technology is adopted, a balling mill is also required to be added, and the investment cost is higher than that of a direct current electric furnace. However, the current direct-current submerged arc furnace can not directly utilize the flue gas rich in carbon monoxide gas to directly heat furnace charges, cold materials can not be loaded into the furnace thermally, in addition, the direct-current submerged arc furnace adopts an open arc production process, so that the power consumption is higher than that of the alternating-current submerged arc furnace, and the direct-current submerged arc furnace is seriously restricted from being widely applied to the large-scale production of ferroalloy.
The power generation efficiency by using the carbon monoxide-rich flue gas is low, which is only about 35 percent. The production process flow is optimized, the powdered furnace charge is directly heated by using the carbon monoxide-rich flue gas of the submerged arc furnace and is hot-charged into the direct-current submerged arc furnace, so that the heat loss in the production process is reduced, the pellet sintering technology is replaced, and the reduction of the power consumption of the direct-current submerged arc furnace becomes the most urgent major problem for popularizing the direct-current submerged arc furnace to produce ferrochrome in large quantities.
Disclosure of Invention
The technical problems to be solved by the invention are as follows: the method and the device for multistage separation and heating of the furnace burden for hot charging of the direct-current submerged arc furnace can utilize carbon monoxide-rich flue gas of the direct-current submerged arc furnace to directly heat powdery furnace burden and heat the powdery furnace burden to the direct-current submerged arc furnace, reduce heat loss in the production process, replace pellet sintering technology and reduce power consumption of the direct-current submerged arc furnace.
The technical scheme for solving the technical problems is as follows: a furnace burden multistage separation heating method for direct-current submerged arc furnace hot charging is characterized by comprising the following steps of: it comprises the following steps:
1) Cold air preheating
The cold air enters the air heating component for preheating, is discharged from the air heating component and enters the burner component when the preheating temperature reaches 200-250 ℃, and provides oxygen for the combustion of the burner;
2) Comprehensive utilization of flue gas
The flue gas with the temperature of 1550-1800 ℃ discharged by the direct current submerged arc furnace enters a burner assembly, is combusted and heated, is discharged out of the burner assembly and enters a cyclone separation assembly after the temperature of the flue gas is increased to 2200-2400 ℃, is subjected to heat exchange with cold furnace burden in the cyclone separation assembly to heat the cold furnace burden, is discharged out of the cyclone separation assembly and enters an air heating assembly, and is discharged to the outside after the cold air in the air heating assembly is preheated to the temperature of 200-250 ℃, the temperature of the flue gas is reduced to 120-150 ℃;
3) Multistage separation heating of cold furnace burden
Cold furnace materials enter the cyclone separation assembly from the cold material feeding assembly, are subjected to multi-stage separation by a primary cyclone separator to a quaternary cyclone separator of the cyclone separation assembly, and are heated by flue gas passing through the cyclone separation assembly to form hot furnace materials with the temperature reaching 900-1200 ℃ and enter the hot material feeding assembly;
4) Hot material feeding
The hot furnace burden entering the hot material feeding assembly is stored in a hot material storage bin, and is fed to the direct-current ore-smelting furnace through a feeder after being weighed by a weighing hopper.
The step 2) of comprehensive utilization of the flue gas comprises the following concrete steps:
(1) The flue gas which is exhausted by the direct-current submerged arc furnace and is rich in carbon monoxide enters the burner assembly under the suction of the air heating assembly, is mixed with hot air which enters the burner through the primary nozzle and has the temperature of 200-250 ℃, is combusted in an oxidizing atmosphere, is mixed with hot air which enters the burner through the secondary nozzle and has the temperature of 200-250 ℃ and is continuously combusted in the oxidizing atmosphere, carbon monoxide in the flue gas is converted into carbon dioxide, and meanwhile, the flue gas is exhausted from the burner assembly after the temperature of the flue gas is increased to 2200-2400 ℃ and enters the cyclone separation assembly;
(2) The flue gas entering the cyclone separation assembly sequentially enters a four-stage cyclone separator, a three-stage cyclone separator, a second-stage cyclone separator and a first-stage cyclone separator, and is respectively subjected to heat exchange with cold furnace burden in the first-stage cyclone separator to the four-stage cyclone separator to heat the cold furnace burden, the temperature of the flue gas is reduced to 500-600 ℃, and then the flue gas is discharged out of the cyclone separation assembly and enters an air heating assembly;
(3) The flue gas entering the air heating assembly and having the temperature of 500-600 ℃ exchanges heat with cold air entering the air heating assembly in the air preheater, the temperature of the flue gas is reduced to 120-150 ℃ after the cold air is preheated to 200-250 ℃ and enters the first flue gas purifying device to be purified, and then the flue gas is discharged to the outside;
(4) And when most of the flue gas discharged from the direct-current submerged arc furnace enters the burner assembly to be comprehensively utilized, redundant flue gas enters the redundant flue gas discharge assembly, and after being purified by the second flue gas purifying device, qualified carbon monoxide enters the carbon monoxide recovery system to be recovered, and the rest of the flue gas enters the outside.
The step 3) of multistage separation heating of the cold furnace burden comprises the following steps:
(1) Cold furnace burden enters a secondary cyclone separator of the cyclone separation assembly from the cold material feeding assembly, is heated in the secondary cyclone separator by being mixed with smoke entering the secondary cyclone separator and is separated into primary large-particle furnace burden and primary small-particle furnace burden, the primary large-particle furnace burden is discharged from the secondary cyclone separator to enter a fourth-stage cyclone separator, and the primary small-particle furnace burden enters the primary cyclone separator together with the smoke;
(2) The primary large-particle furnace burden enters a four-stage cyclone separator, is mixed with smoke entering the four-stage cyclone separator and is heated again, and is separated into secondary large-particle furnace burden and secondary small-particle furnace burden, the secondary large-particle furnace burden is discharged out of the four-stage cyclone separator and enters a hot material feeding component to feed the direct-current ore heating furnace, and the temperature of the furnace burden entering the hot material feeding component reaches between 900 ℃ and 1200 ℃ and the moisture content is 5%; the secondary small-particle furnace burden enters a tertiary cyclone separator together with the flue gas;
(3) The primary small-particle furnace burden enters a primary cyclone separator along with the flue gas, is separated into dust particle furnace burden and fly ash in the primary cyclone separator, the dust particle furnace burden is discharged out of the primary cyclone separator to enter a tertiary cyclone separator, and the flue gas and the separated fly ash are discharged out of a cyclone separation assembly and enter an air heating assembly;
(4) The secondary small-particle furnace burden enters a tertiary cyclone separator along with flue gas, is mixed with dust particle furnace burden entering the tertiary cyclone separator, is heated again, is separated into four-stage large-particle furnace burden and four-stage small-particle furnace burden, and the four-stage large-particle furnace burden is discharged out of the tertiary cyclone separator and enters a hot material feeding component to be fed by a direct-current ore heating furnace, wherein the temperature of the furnace burden entering the hot material feeding component reaches between 900 ℃ and 1200 ℃ and the moisture content reaches 5%; the four-stage small-particle furnace burden enters a secondary cyclone separator along with the flue gas;
(5) The four-stage small-particle furnace burden enters the secondary cyclone separator along with the flue gas to be mixed with the cold furnace burden, and enters the next multi-stage heating separation cycle along with the cold furnace burden while heating the cold furnace burden, so that the cold furnace burden is heated to form hot furnace burden, enters the hot material feeding assembly and is fed for the direct-current submerged arc furnace.
A device for multistage separation heating of charge materials for hot charging of a direct current submerged arc furnace, which comprises a cold charge feeding component and the direct current submerged arc furnace, and is characterized in that: still include cyclone separation subassembly, hot material feed subassembly, combustor subassembly, air heating subassembly and unnecessary flue gas discharge assembly, set gradually between cold charge feed subassembly and the direct current submerged arc furnace cyclone separation subassembly with hot material feed subassembly, the entry of combustor subassembly is connected with the direct current submerged arc furnace, the export is connected with cyclone separation subassembly, air heating subassembly's flue gas inlet pipe is connected with cyclone separation subassembly, hot air export is connected with the combustor subassembly, unnecessary flue gas discharge assembly's entry is connected with the direct current submerged arc furnace, the export leads to the external world.
The cyclone separation component has the structure that: the cyclone separator comprises a primary cyclone separator, a secondary cyclone separator, a tertiary cyclone separator and a quaternary cyclone separator, wherein a first smoke outlet is arranged on the top surface of the primary cyclone separator, a first discharge hole is arranged on the bottom surface of the primary cyclone separator, a first smoke inlet is arranged on the side surface of the primary cyclone separator, a second smoke outlet and a second feed inlet are arranged on the top surface of the secondary cyclone separator, a second discharge hole is arranged on the bottom surface of the secondary cyclone separator, a second smoke inlet is arranged on the side surface of the secondary cyclone separator, a third smoke outlet and a third feed inlet are arranged on the top surface of the tertiary cyclone separator, a third discharge hole is arranged on the bottom surface of the tertiary cyclone separator, a third smoke inlet is arranged on the side surface of the quaternary cyclone separator, a fourth smoke outlet and a fourth feed inlet are arranged on the top surface of the quaternary cyclone separator, and a fourth smoke inlet is arranged on the side surface of the quaternary cyclone separator; the first cyclone separator is arranged above the direct-current submerged arc furnace, and a first flue gas outlet of the first cyclone separator is connected with a flue gas inlet pipe of the air heating component; the second cyclone separator is arranged above the direct-current ore heating furnace and below the side of the first cyclone separator, the second flue gas outlet of the second cyclone separator is connected with the first flue gas inlet of the first cyclone separator, and the second feed inlet is communicated with the feed inlet of the cold material feed assembly; the third cyclone separator is arranged below the side of the second cyclone separator and between the direct current submerged arc furnace and the first cyclone separator, a third flue gas outlet of the third cyclone separator is connected with a second flue gas inlet of the second cyclone separator, a third feeding hole of the third cyclone separator is communicated with a first discharging hole of the first cyclone separator, and the third discharging hole of the third cyclone separator is connected with a hot material storage bin of the hot material feeding assembly through a feeding pipe; the fourth-stage cyclone separator is arranged below the side of the third-stage cyclone separator and between the direct-current submerged arc furnace and the second-stage cyclone separator, a fourth flue gas outlet of the fourth-stage cyclone separator is connected with a third flue gas inlet of the third-stage cyclone separator, a fourth feed inlet of the fourth-stage cyclone separator is communicated with a second discharge outlet of the second-stage cyclone separator, the fourth discharge outlet of the fourth-stage cyclone separator is connected with a storage bin of the hot material feeding assembly, and a fourth flue gas inlet of the fourth-stage cyclone separator is connected with an outlet of the combustor assembly.
The structure of the hot material feeding component is as follows: the hot material storage bin comprises a hot material storage bin body, a hot material bin blanking valve, a weighing hopper, a hopper blanking valve, a feeder and a feeding hose, wherein a first hot material inlet and a second hot material inlet are formed in the top surface of the hot material storage bin body, a discharge hole is formed in the bottom surface of the hot material storage bin body, the first hot material inlet of the hot material storage bin body is connected with a fourth discharge hole of a four-stage cyclone separator, the second hot material inlet is connected with a third discharge hole of the three-stage cyclone separator through the blanking pipe, the hot material bin blanking valve, the weighing hopper, the hopper blanking valve and the feeder are sequentially arranged between the discharge hole of the hot material storage bin body and the feeding hose, and an outlet of the feeding hose is connected with a hollow cathode electrode to form a hot material feeding channel.
The inlet at the bottom of the burner assembly is communicated with the direct current ore smelting furnace, the outlet at the upper part of the burner assembly is connected with the fourth flue gas inlet of the four-stage cyclone separator, the burner assembly is sequentially provided with a first air inlet and a second air inlet from bottom to top, and the first air inlet and the second air inlet are respectively connected with the hot air outlet of the air heating assembly.
The structure of the air heating component is as follows: the device comprises an air preheater, a flue gas inlet pipe, a flue gas outlet pipe, a first flue gas purifying device, a cold air inlet pipe, a hot air outlet pipe, a primary nozzle and a secondary nozzle, wherein the air preheater is connected with a first flue gas outlet of a primary cyclone separator through the flue gas inlet pipe, one end of the flue gas outlet pipe is connected with the air preheater, and the other end of the flue gas outlet pipe is connected with the first flue gas purifying device to form a flue gas discharge channel; one end of the cold air inlet pipe is connected with the air preheater, the other end of the cold air inlet pipe is communicated with the outside, one end of the hot air outlet pipe is connected with the air preheater, a first outlet and a second outlet which are used as hot air outlets are arranged at the other end of the hot air outlet pipe, the first outlet of the hot air outlet pipe is connected with a first air inlet of the burner assembly through a primary nozzle, and the second outlet of the hot air outlet pipe is connected with a second air inlet of the burner assembly through a secondary nozzle to form an air channel for providing oxygen for the combustion of the burner.
The structure of the redundant flue gas discharging component is as follows: the device comprises a second flue gas purification device and an excessive flue gas inlet pipe, wherein the second flue gas purification device is connected with a direct-current submerged arc furnace through the excessive flue gas inlet pipe serving as an inlet, and an outlet of the second flue gas purification device is communicated with the outside and is also connected with a carbon monoxide recovery system.
The bottom of the direct current submerged arc furnace is provided with a furnace bottom anode electrode, the top of the direct current submerged arc furnace is provided with a hollow cathode electrode, the top of the direct current submerged arc furnace is also provided with a first smoke outlet and a second smoke outlet, the first smoke outlet is communicated with the bottom inlet of the burner assembly, and the second smoke outlet is communicated with the redundant smoke inlet pipe of the redundant smoke exhaust assembly.
The structure of the cold material feeding component is as follows: the cyclone separator comprises a feeding port and a belt scale, wherein the feeding port is communicated with an inlet of the belt scale, and an outlet of the belt scale is communicated with a second feeding port arranged on the top surface of a secondary cyclone separator of the cyclone separation assembly.
The invention is manufactured by adopting the prior art, and the belt scale, the primary cyclone separator, the secondary cyclone separator, the burner, the weighing hopper, the feeder, the first smoke purifying device, the second smoke purifying device and the air preheater are all commercial products in the prior art.
The invention has the positive effects that:
according to the multistage separation heating method disclosed by the invention, the cold furnace burden is subjected to multistage separation heating through the cyclone separation assembly and is converted into the hot furnace burden to be fed into the direct-current ore-smelting furnace, and the consumption of electric energy and electrodes is obviously reduced when the hot furnace burden is smelted in the direct-current ore-smelting furnace. The electric energy unit consumption is close to that of an alternating-current submerged arc furnace, the smelting temperature is high, the chromium metal content in the slag is close to zero, secondary recovery treatment of the slag is not needed, and meanwhile, the slag and the wastewater do not contain harmful hexavalent chromium, so that the environmental protection is facilitated. In addition, the investment and production cost are obviously lower than those of the traditional alternating current ore furnace by using cheap ore powder raw materials; the flue gas generated by the direct current submerged arc furnace is used for heating the cold furnace burden in the cyclone separation assembly, so that the emission of harmful gas is reduced, and the environment is protected; the flue gas exhausted by the direct-current submerged arc furnace can be controlled to be carried out in a reducing atmosphere by using the burner assembly to burn and heat the flue gas, so that the reducing reaction condition in the hearth of the direct-current plasma submerged arc furnace is not influenced;
the device used in the invention can meet the production requirements of directly heating the ferrochrome ore by using the carbon monoxide-rich flue gas generated by the direct current ore-smelting furnace and hot charging the direct current ore-smelting furnace by taking the low-grade ferrochrome ore as the raw material, and solves the problem that the direct current ore-smelting furnace in the prior art can not directly heat furnace burden by using the carbon monoxide-rich flue gas generated by the direct current ore-smelting furnace; the structure that the cyclone separation component and the hot material feeding component are sequentially arranged between the cold material feeding component and the direct-current ore-smelting furnace can realize the purposes of cold material feeding and hot material charging of the direct-current ore-smelting furnace;
the cyclone separation component of the device can heat cold furnace materials with different particles in a echelon manner through the multi-stage separation of the first-stage cyclone separator and the fourth-stage cyclone separator, so that the cold furnace materials can be fully heated, and the hot charging requirement of the direct-current submerged arc furnace can be met;
4, the device used in the invention has the advantages that the hot material feeding component can store the hot furnace burden discharged by the cyclone separation component, keep the temperature of the hot furnace burden stable and uniform, and further improve the hot charging effect of the direct-current submerged arc furnace;
the device used in the invention has the advantages that the burner component can heat the smoke generated by the direct-current submerged arc furnace, the temperature of the smoke is further improved, the multi-stage separation of the cyclone separation component and the gradient heating of different granular cold furnace materials are ensured, the cold furnace materials are ensured to be fully heated, and the requirement of the direct-current submerged arc furnace on hot charging is met;
the device used in the invention has the advantages that the air heating component can preheat the air, so that the temperature of the air entering the burner is increased, the residual temperature of the flue gas is fully utilized, and the combustion efficiency of the flue gas is improved;
the device used in the invention has the advantages that the redundant smoke exhaust component can recover redundant carbon monoxide, can prevent smoke from being directly exhausted into the outside, is beneficial to environmental protection, and can realize the comprehensive utilization of the smoke together with the burner component and the cyclone separation component.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
FIG. 2 is a block diagram of a multi-stage separation heating system of the present invention.
In the figure: 1, a feeding port; 2, weighing the belt; 4, a feeding control valve; 5 feeding pipes; a first cyclone separator; a 7-stage cyclone separator; 8, blanking control valves; 9, a first blanking pipe; 10 three-stage cyclone separators; 11 furnace bottom anode electrode; a second blanking pipe 12; a four stage cyclone separator 13; 14 a first flue gas cleaning device; 15 a second flue gas purifying device; a 16 feeding pipe; 17, storing the hot materials in a storage bin; 18 a hot stock bin blanking valve; 19 weighing a hopper; a 20 hopper blanking valve; a 21 feeder; 22 feeding hoses; 23 secondary air nozzles; 24 primary air nozzles; 25 a standby valve; 26 an excess flue gas inlet duct; 27 a flue gas cleaning inlet valve; 28 direct current submerged arc furnace; a burner assembly 29; 30 flue gas inlet pipe; 31 a flue gas inlet valve; 32 an air preheater; 33 flue gas outlet duct; 34 air inlet duct; 35 an air outlet tube; 36 hollow cathode electrode.
Detailed Description
The invention will be further described with reference to the drawings and examples.
Referring to fig. 1-2, embodiment 1, a multi-stage separation heating method of burden for hot charging of a direct current submerged arc furnace, comprising the steps of:
1) Cold air preheating
The cold air enters the air heating component to be preheated, then is discharged out of the air heating component and enters the burner component 29 to supply oxygen for the combustion of the burner, and the temperature of the preheated cold air is 200-250 ℃;
2) Comprehensive utilization of flue gas
The flue gas discharged by the direct current submerged arc furnace 28 is rich in carbon monoxide flue gas, wherein the carbon monoxide gas content is 85% -90%, the hydrogen gas content is 2% -5%, the carbon dioxide gas content is 2% -5%, the methane gas content is about 1.5%, the nitrogen gas content is 2% -7%, the flue gas temperature is 1550 ℃ -1800 ℃, and the comprehensive utilization of the flue gas is specifically as follows:
(1) The flue gas which is exhausted from the direct-current submerged arc furnace 28 and rich in carbon monoxide enters the burner assembly 29 under the suction of a smoke exhaust fan of the first flue gas purifying device 14 of the air heating assembly, is mixed with hot air which enters the burner through the primary nozzle 24 and has the temperature of 200-250 ℃ in the burner assembly 29, is combusted in an oxidizing atmosphere, is then mixed with hot air which enters the burner through the secondary nozzle 23 and has the temperature of 200-250 ℃ and is continuously combusted in the oxidizing atmosphere, carbon monoxide in the flue gas is converted into carbon dioxide, and the flue gas is exhausted from the burner assembly 29 after the temperature of the flue gas is increased to 2200-2400 ℃ and enters the cyclone separation assembly;
(2) The flue gas entering the cyclone separation assembly firstly enters a four-stage cyclone separator 13 through a fourth flue gas inlet, then enters a three-stage cyclone separator 10 through a fourth flue gas outlet and a third flue gas inlet, then enters a two-stage cyclone separator 7 through a third flue gas outlet and a second flue gas inlet, then enters a first-stage cyclone separator 6 through a second flue gas outlet and a first flue gas inlet, and is respectively and thermally exchanged with cold furnace burden in the first-stage cyclone separator 6-the four-stage cyclone separator 13 to heat the cold furnace burden, and after the flue gas temperature is reduced to 500-600 ℃, the cold furnace burden is discharged out of the cyclone separation assembly through the first flue gas outlet and enters an air heating assembly;
(3) The flue gas with the temperature of 500-600 ℃ entering the air heating component exchanges heat with cold air entering the air heating component in the air preheater 32, the temperature of the flue gas is reduced to 120-150 ℃ after the cold air is preheated to 200-250 ℃ and enters the first flue gas purifying device 14 to be purified, and then the flue gas is discharged to the outside;
(4) While most of the flue gas discharged by the direct-current submerged arc furnace 28 enters the burner assembly 29 to be comprehensively utilized, redundant flue gas enters the redundant flue gas discharge assembly, and after being purified by the second flue gas purification device 15, qualified carbon monoxide enters a carbon monoxide recovery system to be recovered, and the rest of the flue gas enters the outside;
3) Multistage separation heating of cold furnace burden
The step 3) of multistage separation heating of the cold furnace burden comprises the following steps:
(1) Cold furnace burden enters a secondary cyclone separator 7 of the cyclone separation assembly from a cold material feeding assembly, the cold furnace burden is heated in the secondary cyclone separator 7 by being mixed with smoke entering the secondary cyclone separator 7 and separated into primary large-particle furnace burden and primary small-particle furnace burden, the primary large-particle furnace burden enters a four-stage cyclone separator 13 from a second discharge port of the secondary cyclone separator 7 through a fourth feed port, and the primary small-particle furnace burden enters the primary cyclone separator 6 together with the smoke through a first smoke inlet;
(2) The primary large-particle furnace burden enters a four-stage cyclone separator 13, is mixed with flue gas entering the four-stage cyclone separator 13, is heated again and is separated into a secondary large-particle furnace burden and a secondary small-particle furnace burden, the secondary large-particle furnace burden enters a hot material feeding component through a fourth discharge port of the four-stage cyclone separator 13 to feed a direct-current submerged arc furnace 28, and the temperature of the furnace burden entering the hot material feeding component reaches between 900 ℃ and 1200 ℃ and the moisture content is 5%; the secondary small-particle furnace burden enters the tertiary cyclone separator 10 along with the smoke through a third smoke inlet;
(3) The primary small particle furnace burden enters the primary cyclone separator 6 along with the flue gas through a first flue gas inlet, is separated into dust particle furnace burden and fly ash in the primary cyclone separator 6, the dust particle furnace burden enters the tertiary cyclone separator 10 through a third feed inlet from a first discharge port of the primary cyclone separator 6, and the flue gas and the separated fly ash are discharged out of the cyclone separation assembly through a first flue gas outlet and enter an air heating assembly;
(4) The secondary small-particle furnace burden enters the three-stage cyclone separator 10 along with the flue gas through a third flue gas inlet, is mixed with the dust particle furnace burden entering the three-stage cyclone separator 10, is heated again and is separated into a four-stage large-particle furnace burden and a four-stage small-particle furnace burden, the four-stage large-particle furnace burden enters a hot material feeding component through a third discharge port of the three-stage cyclone separator 10 to feed the direct-current ore-smelting furnace 28, and the temperature of the furnace burden entering the hot material feeding component reaches between 900 ℃ and 1200 ℃ and the moisture content is 5%; the four-stage small-particle furnace burden enters the secondary cyclone separator 7 along with the smoke through the second smoke inlet;
(5) The four-stage small-particle furnace burden enters the second-stage cyclone separator 7 through the second smoke inlet together with smoke to be mixed with the cold furnace burden, and enters the next multi-stage heating separation cycle together with the cold furnace burden while heating the cold furnace burden, so that the cold furnace burden is heated to form hot furnace burden, enters the hot material feeding assembly and is fed to the direct-current submerged arc furnace 28;
4) Hot material feeding
The hot charge entering the hot charge feed assembly is stored in a hot charge storage bin 17 and is then weighed by a weighing hopper 19 and fed by a feeder 21 to a direct current submerged arc furnace 28.
The device used in this embodiment includes cold charge feed subassembly, direct current ore deposit hot stove 28, cyclone separation subassembly, hot charge feed subassembly, combustor subassembly 29, air heating subassembly and unnecessary flue gas discharge subassembly, set gradually between cold charge feed subassembly and the direct current ore deposit hot stove 28 cyclone separation subassembly with hot charge feed subassembly, the entry of combustor subassembly 29 is connected with direct current ore deposit hot stove 28, the export is connected with cyclone separation subassembly, air heating subassembly's flue gas inlet pipe 30 is connected with cyclone separation subassembly, the hot air export is connected with combustor subassembly 29, unnecessary flue gas discharge subassembly's entry is connected with direct current ore deposit hot stove 28, the export leads to the external world.
The bottom of the direct current submerged arc furnace 28 is provided with a furnace bottom anode electrode 11, the top of the direct current submerged arc furnace 28 is provided with a hollow cathode electrode 36, the top of the direct current submerged arc furnace 28 is also provided with a first smoke outlet and a second smoke outlet, the first smoke outlet is communicated with the bottom inlet of the burner assembly 29, and the second smoke outlet is communicated with the redundant smoke inlet pipe 26 of the redundant smoke discharging assembly.
The structure of the cold material feeding component is as follows: the belt conveyor comprises a feeding port 1 and a belt conveyor scale 2, wherein the feeding port 1 is communicated with an inlet of the belt conveyor scale 2, and an outlet of the belt conveyor scale 2 is communicated with a second feeding port arranged on the top surface of a secondary cyclone separator 7 of the cyclone separation assembly.
The cyclone separation component has the structure that: the cyclone separator comprises a first cyclone separator 6, a second cyclone separator 7, a third cyclone separator 10 and a fourth cyclone separator 13, wherein a first smoke outlet is formed in the top surface of the first cyclone separator 6, a first discharge hole is formed in the bottom surface of the first cyclone separator, a first smoke inlet is formed in the side surface of the first cyclone separator, a second smoke outlet and a second feed inlet are formed in the top surface of the second cyclone separator 7, a second discharge hole is formed in the bottom surface of the second cyclone separator, a second smoke inlet is formed in the side surface of the second cyclone separator, a third smoke outlet and a third feed inlet are formed in the top surface of the third cyclone separator 10, a third smoke inlet is formed in the bottom surface of the third cyclone separator, a third smoke inlet is formed in the side surface of the third cyclone separator, a fourth smoke outlet and a fourth discharge hole are formed in the top surface of the fourth cyclone separator 13, and a fourth smoke inlet is formed in the side surface of the fourth cyclone separator; the primary cyclone separator 6 is arranged above the direct-current submerged arc furnace 28, and a first flue gas outlet of the primary cyclone separator is connected with a flue gas inlet pipe 30 of the air heating component; the second cyclone separator 7 is arranged above the direct-current ore-smelting furnace 28 and below the side of the first cyclone separator 6, the second flue gas outlet of the second cyclone separator is connected with the first flue gas inlet of the first cyclone separator 6, and the second feeding port is communicated with the outlet of the belt scale 2 of the cold material feeding assembly through the feeding pipe 5; the third cyclone separator 10 is arranged below the side of the second cyclone separator 7 and between the direct current ore smelting furnace 28 and the first cyclone separator 6, a third flue gas outlet of the third cyclone separator is connected with a second flue gas inlet of the second cyclone separator 7, a third feed inlet of the third cyclone separator is communicated with a first discharge opening of the first cyclone separator 6 through a first blanking pipe 9, and a third discharge opening of the third cyclone separator is connected with a hot material storage bin 17 of a hot material feeding assembly through a feed pipe 16; the fourth cyclone separator 13 is arranged below the side of the third cyclone separator 10 and between the direct current ore smelting furnace 28 and the second cyclone separator 7, a fourth smoke outlet of the fourth cyclone separator is connected with a third smoke inlet of the third cyclone separator 10, a fourth feeding hole of the fourth cyclone separator is communicated with a second discharging hole of the second cyclone separator 7 through a second discharging pipe 12, a fourth discharging hole of the fourth cyclone separator is connected with a storage bin of the hot material feeding assembly through a fourth discharging pipe, a fourth smoke inlet of the fourth cyclone separator is connected with an outlet of the burner assembly 29, a feeding control valve 4 is arranged on the feeding pipe 5, and a discharging control valve 8 is respectively arranged on the first discharging pipe 9, the second discharging pipe 12, the fourth discharging pipe and the feeding pipe 16.
The structure of the hot material feeding component is as follows: the hot material storage bin 17, the hot material bin blanking valve 18, the weighing hopper 19, the hopper blanking valve 20, the feeder 21 and the feeding hose 22 are included, a first hot material inlet and a second hot material inlet are formed in the top surface of the hot material storage bin 17, a discharge hole is formed in the bottom surface of the hot material storage bin 17, the first hot material inlet of the hot material storage bin 17 is connected with a fourth discharge hole of the four-stage cyclone separator 13, the second hot material inlet is connected with a third discharge hole of the three-stage cyclone separator 10 through the feeding pipe 16, the hot material bin blanking valve 18, the weighing hopper 19, the hopper blanking valve 20 and the feeder 21 are sequentially arranged between the discharge hole of the hot material storage bin 17 and the feeding hose 22, an outlet of the feeding hose 22 is connected with the hollow cathode 36, and a hot material feeding channel is formed, and the feeder 21 is a screw feeder.
The inlet at the bottom of the burner assembly 29 is communicated with the direct current submerged arc furnace 28, the outlet at the upper part is connected with the fourth flue gas inlet of the four-stage cyclone separator 13, a first air inlet and a second air inlet are sequentially arranged between the burner assembly 29 from bottom to top, and the first air inlet and the second air inlet are respectively connected with the hot air outlet of the air heating assembly.
The structure of the air heating component is as follows: the air preheater 32 is connected with a first smoke outlet of the primary cyclone separator 6 through the smoke inlet pipe 30, one end of the smoke outlet pipe 33 is connected with the air preheater 32, and the other end of the smoke outlet pipe 33 is connected with the first smoke purifying device 14 to form a smoke discharge channel; one end of the cold air inlet pipe 34 is connected with the air preheater 32, the other end is communicated with the outside, one end of the hot air outlet pipe 35 is connected with the air preheater 32, the other end is provided with a first outlet and a second outlet which are used as hot air outlets, the first outlet of the hot air outlet pipe 35 is connected with a first air inlet of the burner assembly 29 through the primary nozzle 24, the second outlet of the hot air outlet pipe 35 is connected with a second air inlet of the burner assembly 29 through the secondary nozzle 23, an air channel for providing oxygen for the combustion of the burner is formed, a flue gas inlet valve 31 is arranged on the flue gas inlet pipe 30, and a standby valve 25 is arranged at the end of the hot air outlet pipe 35.
The structure of the redundant flue gas discharging component is as follows: the device comprises a second flue gas purification device 15 and an excessive flue gas inlet pipe 26, wherein the second flue gas purification device 15 is connected with a direct-current submerged arc furnace 28 through the excessive flue gas inlet pipe 26 serving as an inlet, an outlet of the second flue gas purification device 15 is communicated with the outside and is also connected with a carbon monoxide recovery system, and a flue gas purification inlet valve 27 is arranged on the excessive flue gas inlet pipe 26.
The belt scale 2, the first cyclone separator 6-the fourth cyclone separator 13, the burner, the weighing hopper 19, the feeder 21, the first flue gas purifying device 14, the second flue gas purifying device 15, the air preheater 32, the feeding control valve 4, the discharging control valve 8, the hot bin discharging valve 18, the hopper discharging valve 20, the flue gas inlet valve 31, the flue gas purifying inlet valve 27 and the standby valve 25 are all commercial products in the prior art.
Claims (3)
1. A furnace burden multistage separation heating method for direct-current submerged arc furnace hot charging is characterized by comprising the following steps of: it comprises the following steps:
1) Cold air preheating
The cold air enters the air heating component for preheating, is discharged from the air heating component and enters the burner component when the preheating temperature reaches 200-250 ℃, and provides oxygen for the combustion of the burner;
2) Comprehensive utilization of flue gas
The flue gas with the temperature of 1550-1800 ℃ discharged by the direct current submerged arc furnace enters a burner assembly, is combusted and heated, is discharged out of the burner assembly and enters a cyclone separation assembly after the temperature of the flue gas is increased to 2200-2400 ℃, is subjected to heat exchange with cold furnace burden in the cyclone separation assembly to heat the cold furnace burden, is discharged out of the cyclone separation assembly and enters an air heating assembly, and is discharged to the outside after the cold air in the air heating assembly is preheated to the temperature of 200-250 ℃, the temperature of the flue gas is reduced to 120-150 ℃;
3) Multistage separation heating of cold furnace burden
Cold furnace materials enter the cyclone separation assembly from the cold material feeding assembly, are subjected to multi-stage separation by a primary cyclone separator to a quaternary cyclone separator of the cyclone separation assembly, and are heated by flue gas passing through the cyclone separation assembly to form hot furnace materials with the temperature reaching 900-1200 ℃ and enter the hot material feeding assembly;
4) Hot material feeding
The hot furnace burden entering the hot material feeding assembly is stored in a hot material storage bin, and is fed to the direct-current ore-smelting furnace through a feeder after being weighed by a weighing hopper;
the step 2) of comprehensive utilization of the flue gas comprises the following concrete steps:
(1) The flue gas which is exhausted by the direct-current submerged arc furnace and is rich in carbon monoxide enters the burner assembly under the suction of the air heating assembly, is mixed with hot air which enters the burner through the primary nozzle and has the temperature of 200-250 ℃, is combusted in an oxidizing atmosphere, is mixed with hot air which enters the burner through the secondary nozzle and has the temperature of 200-250 ℃ and is continuously combusted in the oxidizing atmosphere, carbon monoxide in the flue gas is converted into carbon dioxide, and meanwhile, the flue gas is exhausted from the burner assembly after the temperature of the flue gas is increased to 2200-2400 ℃ and enters the cyclone separation assembly;
(2) The flue gas entering the cyclone separation assembly sequentially enters a four-stage cyclone separator, a three-stage cyclone separator, a second-stage cyclone separator and a first-stage cyclone separator, and is respectively subjected to heat exchange with cold furnace burden in the first-stage cyclone separator to the four-stage cyclone separator to heat the cold furnace burden, the temperature of the flue gas is reduced to 500-600 ℃, and then the flue gas is discharged out of the cyclone separation assembly and enters an air heating assembly;
(3) The flue gas entering the air heating assembly and having the temperature of 500-600 ℃ exchanges heat with cold air entering the air heating assembly in the air preheater, the temperature of the flue gas is reduced to 120-150 ℃ after the cold air is preheated to 200-250 ℃ and enters the first flue gas purifying device to be purified, and then the flue gas is discharged to the outside;
(4) When most of the flue gas discharged from the direct-current submerged arc furnace enters the burner assembly to be comprehensively utilized, redundant flue gas enters the redundant flue gas discharge assembly, and after being purified by the second flue gas purifying device, qualified carbon monoxide enters the carbon monoxide recovery system to be recovered, and the rest of the flue gas enters the outside;
the step 3) of multistage separation heating of the cold furnace burden comprises the following steps:
(1) Cold furnace burden enters a secondary cyclone separator of the cyclone separation assembly from the cold material feeding assembly, is heated in the secondary cyclone separator by being mixed with smoke entering the secondary cyclone separator and is separated into primary large-particle furnace burden and primary small-particle furnace burden, the primary large-particle furnace burden is discharged from the secondary cyclone separator to enter a fourth-stage cyclone separator, and the primary small-particle furnace burden enters the primary cyclone separator together with the smoke;
(2) The primary large-particle furnace burden enters a four-stage cyclone separator, is mixed with smoke entering the four-stage cyclone separator and is heated again, and is separated into secondary large-particle furnace burden and secondary small-particle furnace burden, the secondary large-particle furnace burden is discharged out of the four-stage cyclone separator and enters a hot material feeding component to feed the direct-current ore heating furnace, and the temperature of the furnace burden entering the hot material feeding component reaches between 900 ℃ and 1200 ℃ and the moisture content is 5%; the secondary small-particle furnace burden enters a tertiary cyclone separator together with the flue gas;
(3) The primary small-particle furnace burden enters a primary cyclone separator along with the flue gas, is separated into dust particle furnace burden and fly ash in the primary cyclone separator, the dust particle furnace burden is discharged out of the primary cyclone separator to enter a tertiary cyclone separator, and the flue gas and the separated fly ash are discharged out of a cyclone separation assembly and enter an air heating assembly;
(4) The secondary small-particle furnace burden enters a three-stage cyclone separator together with flue gas, is mixed with dust particle furnace burden entering the three-stage cyclone separator to be heated again and separated into four-stage large-particle furnace burden and four-stage small-particle furnace burden, the four-stage large-particle furnace burden is discharged out of the three-stage cyclone separator to enter a hot material feeding component to feed a direct-current ore heating furnace, and the temperature of the furnace burden entering the hot material feeding component reaches between 900 ℃ and 1200 ℃ and moisture5The%; the four-stage small-particle furnace burden enters a secondary cyclone separator along with the flue gas;
(5) The four-stage small-particle furnace burden enters the secondary cyclone separator along with the flue gas to be mixed with the cold furnace burden, and enters the next multi-stage heating separation cycle along with the cold furnace burden while heating the cold furnace burden, so that the cold furnace burden is heated to form hot furnace burden, enters the hot material feeding assembly and is fed for the direct-current submerged arc furnace.
2. A device for multistage separation heating of charge materials for hot charging of a direct current submerged arc furnace, which comprises a cold charge feeding component and the direct current submerged arc furnace, and is characterized in that: the hot-blast furnace cooling device comprises a direct-current ore furnace, a cold-blast furnace hot-blast furnace cooling device, a cold-blast furnace cooling device, a direct-current ore furnace, a cyclone separation assembly, a hot-blast feeding assembly, a burner assembly, an air heating assembly and a redundant flue gas discharge assembly, wherein the cyclone separation assembly and the hot-blast feeding assembly are sequentially arranged between the cold-blast feeding assembly and the direct-current ore furnace;
the cyclone separation component has the structure that: the cyclone separator comprises a primary cyclone separator, a secondary cyclone separator, a tertiary cyclone separator and a quaternary cyclone separator, wherein a first smoke outlet is arranged on the top surface of the primary cyclone separator, a first discharge hole is arranged on the bottom surface of the primary cyclone separator, a first smoke inlet is arranged on the side surface of the primary cyclone separator, a second smoke outlet and a second feed inlet are arranged on the top surface of the secondary cyclone separator, a second discharge hole is arranged on the bottom surface of the secondary cyclone separator, a second smoke inlet is arranged on the side surface of the secondary cyclone separator, a third smoke outlet and a third feed inlet are arranged on the top surface of the tertiary cyclone separator, a third discharge hole is arranged on the bottom surface of the tertiary cyclone separator, a third smoke inlet is arranged on the side surface of the quaternary cyclone separator, a fourth smoke outlet and a fourth feed inlet are arranged on the top surface of the quaternary cyclone separator, and a fourth smoke inlet is arranged on the side surface of the quaternary cyclone separator; the first cyclone separator is arranged above the direct-current submerged arc furnace, and a first flue gas outlet of the first cyclone separator is connected with a flue gas inlet pipe of the air heating component; the second cyclone separator is arranged above the direct-current ore heating furnace and below the side of the first cyclone separator, the second flue gas outlet of the second cyclone separator is connected with the first flue gas inlet of the first cyclone separator, and the second feed inlet is communicated with the feed inlet of the cold material feed assembly; the third cyclone separator is arranged below the side of the second cyclone separator and between the direct current submerged arc furnace and the first cyclone separator, a third flue gas outlet of the third cyclone separator is connected with a second flue gas inlet of the second cyclone separator, a third feeding hole of the third cyclone separator is communicated with a first discharging hole of the first cyclone separator, and the third discharging hole of the third cyclone separator is connected with a hot material storage bin of the hot material feeding assembly through a feeding pipe; the fourth-stage cyclone separator is arranged below the side of the third-stage cyclone separator and between the direct-current submerged arc furnace and the second-stage cyclone separator, a fourth flue gas outlet of the fourth-stage cyclone separator is connected with a third flue gas inlet of the third-stage cyclone separator, a fourth feed inlet of the fourth-stage cyclone separator is communicated with a second discharge outlet of the second-stage cyclone separator, the fourth discharge outlet of the fourth-stage cyclone separator is connected with a storage bin of the hot material feeding assembly, and a fourth flue gas inlet of the fourth-stage cyclone separator is connected with an outlet of the combustor assembly;
the structure of the hot material feeding component is as follows: the hot material storage bin comprises a hot material storage bin, a hot material bin blanking valve, a weighing hopper, a hopper blanking valve, a feeder and a feeding hose, wherein a first hot material inlet and a second hot material inlet are formed in the top surface of the hot material storage bin, a discharge hole is formed in the bottom surface of the hot material storage bin, the first hot material inlet of the hot material storage bin is connected with a fourth discharge hole of a four-stage cyclone separator, the second hot material inlet is connected with a third discharge hole of a three-stage cyclone separator, the hot material bin blanking valve, the weighing hopper, the hopper blanking valve and the feeder are sequentially arranged between the discharge hole of the hot material storage bin and the feeding hose, and the outlet of the feeding hose is connected with a hollow cathode electrode to form a hot material feeding channel;
an inlet at the bottom of the burner assembly is communicated with the direct current ore smelting furnace, an outlet at the upper part of the burner assembly is connected with a fourth flue gas inlet of the four-stage cyclone separator, a first air inlet and a second air inlet are sequentially arranged between the burner assembly from bottom to top, and the first air inlet and the second air inlet are respectively connected with a hot air outlet of the air heating assembly;
the structure of the air heating component is as follows: the device comprises an air preheater, a flue gas inlet pipe, a flue gas outlet pipe, a first flue gas purifying device, a cold air inlet pipe, a hot air outlet pipe, a primary nozzle and a secondary nozzle, wherein the air preheater is connected with a first flue gas outlet of a primary cyclone separator through the flue gas inlet pipe, one end of the flue gas outlet pipe is connected with the air preheater, and the other end of the flue gas outlet pipe is connected with the first flue gas purifying device to form a flue gas discharge channel; one end of the cold air inlet pipe is connected with the air preheater, the other end of the cold air inlet pipe is communicated with the outside, one end of the hot air outlet pipe is connected with the air preheater, a first outlet and a second outlet which are used as hot air outlets are arranged at the other end of the hot air outlet pipe, the first outlet of the hot air outlet pipe is connected with a first air inlet of the burner assembly through a primary nozzle, and the second outlet of the hot air outlet pipe is connected with a second air inlet of the burner assembly through a secondary nozzle to form an air channel for providing oxygen for the combustion of the burner.
3. The apparatus for multistage separation and heating of charge material for hot charging of a direct current submerged arc furnace according to claim 2, characterized in that: the structure of the redundant flue gas discharging component is as follows: the device comprises a second flue gas purification device and an excessive flue gas inlet pipe, wherein the second flue gas purification device is connected with a direct-current submerged arc furnace through the excessive flue gas inlet pipe serving as an inlet, and an outlet of the second flue gas purification device is communicated with the outside and is also connected with a carbon monoxide recovery system.
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| CN108548418A (en) * | 2018-03-30 | 2018-09-18 | 沈阳鑫博工业技术股份有限公司 | A kind of single rare earth oxide suspension roasting device and its application method |
| CN208223178U (en) * | 2018-03-30 | 2018-12-11 | 沈阳鑫博工业技术股份有限公司 | A kind of single rare earth oxide suspension roasting device |
| CN209588733U (en) * | 2019-01-27 | 2019-11-05 | 中钢集团吉林机电设备有限公司 | Furnace charge multi-stage separation heating device for DC-ore-heating furnace molten charge |
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