CN100398668C - Technological process and apparatus for heating high concentration CO and other reducing gas - Google Patents
Technological process and apparatus for heating high concentration CO and other reducing gas Download PDFInfo
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- CN100398668C CN100398668C CNB2005100273989A CN200510027398A CN100398668C CN 100398668 C CN100398668 C CN 100398668C CN B2005100273989 A CNB2005100273989 A CN B2005100273989A CN 200510027398 A CN200510027398 A CN 200510027398A CN 100398668 C CN100398668 C CN 100398668C
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- 238000000034 method Methods 0.000 title claims abstract description 48
- 238000010438 heat treatment Methods 0.000 title claims abstract description 40
- 239000007789 gas Substances 0.000 claims abstract description 136
- 238000002485 combustion reaction Methods 0.000 claims abstract description 36
- 239000003517 fume Substances 0.000 claims abstract description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 41
- 239000003546 flue gas Substances 0.000 claims description 33
- 238000005516 engineering process Methods 0.000 claims description 16
- 238000005338 heat storage Methods 0.000 claims description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000003034 coal gas Substances 0.000 claims description 9
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 6
- 229910052593 corundum Inorganic materials 0.000 claims description 6
- 239000010431 corundum Substances 0.000 claims description 6
- 230000006698 induction Effects 0.000 claims description 6
- 229910052573 porcelain Inorganic materials 0.000 claims description 6
- 238000010792 warming Methods 0.000 claims description 6
- 229910001051 Magnalium Inorganic materials 0.000 claims description 5
- 239000000919 ceramic Substances 0.000 claims description 5
- 238000004880 explosion Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000002912 waste gas Substances 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 15
- 229910052799 carbon Inorganic materials 0.000 abstract description 15
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 230000007774 longterm Effects 0.000 abstract description 2
- 239000008188 pellet Substances 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 13
- 239000000428 dust Substances 0.000 description 10
- 229910002091 carbon monoxide Inorganic materials 0.000 description 8
- 238000011946 reduction process Methods 0.000 description 8
- 239000004575 stone Substances 0.000 description 8
- 238000003723 Smelting Methods 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 238000009825 accumulation Methods 0.000 description 6
- 239000000567 combustion gas Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 238000004458 analytical method Methods 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 5
- 238000003672 processing method Methods 0.000 description 4
- 208000011580 syndromic disease Diseases 0.000 description 4
- 238000009827 uniform distribution Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
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- 230000002950 deficient Effects 0.000 description 1
- 238000006253 efflorescence Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 206010037844 rash Diseases 0.000 description 1
- 229910001067 superalloy steel Inorganic materials 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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Abstract
The technological process of heating high concentration CO and other reducing gas includes the following steps: 1. pre-heating the combustion supporting air and burnt gas to 130-150 deg.c with the hot blast stove fume before heat accumulating operation of the said gas; and 2. pre-heating the cold reducing gas to 130-150 deg.c with the hot blast stove fume through heat exchange in the heat pipe heat exchanger, and the further heat exchange between the pre-heated reducing gas and the heat accumulating pellet bed inside the ball type hot blast stove to raise the temperature of the reducing gas to 850-950 deg.c. Or, the cold reducing gas may be heat exchanged for the second time to raise the temperature to 400 deg.c before the heat exchange inside the ball type hot blast stove. The present invention can overcome the carbon separating reaction of the reducing gas during being heated so as to realize the long term stable heating of the reducing gas.
Description
Technical field
The present invention relates to non-blast furnace ironmaking and promptly directly reduce and the melting and reducing field, relate to a kind of heating process and device thereof that contains reducing gass such as high-concentration carbon monoxide and hydrogen.The purpose of the reducing gas of heating high concentration CO and hydrogen is to be used for shaft furnace to produce direct-reduced iron, perhaps uses the reducing gas of blast furnace blowing high density.
Background technology
The heating process of high-concentration carbon monoxide gas and method all are one of critical technological points in various direct reduction and smelting reduction process.The professional person is known, and in existing various smelting reduction process technology, ironmaking technique of fusion and reduction all produces big reducing gas flow, that contain higher concentration carbon monoxide and hydrogen, and custom is referred to as melting and reducing furnace exhaust gas or residual gas.For example the tail gas amount of COREX smelting reduction process generation is about 1600～1800NM./ t, the tail gas amount that the Hismelt smelting reduction process produces is about 2000～2400N_M./t。How to utilize the residual gas of smelting reduction process, will directly have influence on the reasonableness and the competitive power of ironmaking technique of fusion and reduction technology.Numerous utilizing in the scheme, utilizing the residual gas production direct-reduced iron or the sponge iron of smelting reduction process is exactly one of them scheme.
The residual gas that utilizes smelting reduction process is that reducing gas is produced direct-reduced iron or sponge iron, and after the reducing gas purifying treatment, it is reducing gas to be heated to certain temperature that one important operation arranged.Reducing gas heating process method has indirect heating method or snead process.A kind of typical indirect heating method is that reducing gas is passed through at metallic conduit, with the outer thermal medium heat exchange of metallic conduit, thereby promotes temperature.The advantage of this kind heating means is that the concentration of the quality of reducing gas or carbon monoxide and hydrogen does not change in heat-processed, easily analyses carbon but the shortcoming of this kind method is a reducing gas at certain warm area.
The reaction that all cpds produces elemental carbon under certain conditions is referred to as to analyse the carbon reaction.CO is being arranged, H
2, CO
2, CH
4Deng the occasion of mixed gas, can produce elemental carbon according to following reaction under certain conditions.
2CO-CO
2+C……………(1)
CO+H
2-H
2O+C……………(2)
CH
4-2H
2+C...............(3)
Multiple evidence contain in the reducing gas heat-processed of CO (carbon monoxide converter) gas composition, analyse carbon and be reflected at 400～700 ℃ of warm areas and produce inevitably, especially under the condition that metallic iron or catalyzer exist for very.The direct result of analysing the carbon reaction is, not only the quality of reducing gas is affected, and be used to carry the metal tube such as the superalloy steel pipe matrix that add thermal reduction gas to become fragile, high-temperature behavior worsens, under certain temperature and pressure condition, its life-span shortens greatly, causes gas leakage when serious, produces security incident.
At the problems referred to above, people have proposed many processing methodes to the heating process that heating contains high-concentration carbon monoxide gas.The method of the production sponge iron of inventing among the Chinese patent CN 1167506A and implementing in the device of this method has adopted two step method to add the technology of thermal reduction gas.Be about to contain the reducing gas of carbon monoxide and hydrogen, at first the mode with interchanger is heated to 400 ℃ with reducing gas, and then promotes the temperature of reducing gas self with directly the burn method of reducing gas of oxygen.So just avoided reduction air elutriation carbon reaction under 400～700 ℃ of conditions.But the shortcoming of this technology is tangible, it is in the burning heat-processed in second step, and the partially combusted result of carbon monoxide and hydrogen is that the oxidisability of reducing gas improves greatly, thereby reduced the quality of reducing gas, directly influenced the efficient of follow-up direct reducing process and the utilization coefficient of shaft furnace.
Chinese patent CN1275624.A has set forth the processing method that a kind of coal generating gas is produced sponge iron.In the method, mentioned the technology with the process furnace of 2 parallel connections heating reducing gas, two mutual accumulation of heats of process furnace and heat exchange are heated to for example 800～1000 ℃ of required temperature ranges by the accumulation of heat stone ball of process furnace with reducing gas.The defective of this method is, directly-heated adopts cold reducing gas to enter the heat exchange of ball bed, and stone ball heat transfer temperature difference is big, bottom stone ball efflorescence is serious, have a strong impact on chimney valve sealing, the air leak rate of air curtain of pebble stove dustiness of flue gas when burning stove is closely related, so the reducing gas that this method is missed from chimney valve is more.In addition, in this method, directly burn stove with cooled coal gas and combustion air and heat up, not only Combustion of Hot Air Furnace extends heating period, and heat-exchange periodic is also short, and whole process furnace operation energy consumption is higher.
Chinese patent CN1570152A has mentioned a kind of method of obtaining high wind-warm syndrome with pure blast furnace gas.The principal character of this method is how to utilize low-calorie blast furnace gas to obtain high wind-warm syndrome to be used for blast furnace ironmaking.Its heating target is air but not reducing gas.Another feature of this method is, utilized the front preheating process technology, combustion air is carried out two step preheatings, improve the theoretical combustion temperature of pebble stove, and then raising hotblast stove vault district temperature to 1300～1350 ℃, thereby make wind-warm syndrome reach the wind-warm syndrome level of 1200 ℃ of these large blast furnaces, the while has also been improved the thermo-efficiency of hotblast stove.Should be noted that the heating reducing gas and add warm air many significant differences are arranged: air heating does not exist analyses the carbon reaction, so this method is to the not preheating of medium " air " of need heat exchange.Thereby the also not mentioned Pulverization ratio that how to reduce the ball bed of this method improves this problem of sealing property of chimney valve.And this is crucial when adding thermal reduction gas to pebble stove, because leak out this moment, means that then directly some reducing gas is lost from flue.
Summary of the invention
The present invention be directed to the prior art deficiency, and a kind of technology and device thereof that heats reducing gas is provided, be used for Shaft Furnace Direct Reduction Process.It is characterized in that,
The technology of reducing gass such as a kind of heating high concentration CO and hydrogen comprises the steps:
A) to utilize temperature be 250～320 ℃ of hot-blast stove fumes that combustion air and burning coal gas are carried out front preheating process one time, with its temperature increase to 130～150 ℃; Combustion air, burning coal gas are carried out preheating, improve the thermo-efficiency of hotblast stove;
B) cold reducing gas is carried out the front preheating process first time, utilizing temperature is 250～320 ℃ of hot-blast stove fume heat exchange in hot tube heat exchanger, with its temperature increase to 130～150 ℃;
C) the pebble stove heat storage operation of burning, combustion air and burning coal gas with a front preheating process burn stove, produce 1200～1300 ℃ high-temperature flue gas, to enter pebble stove through the reducing gas of front preheating process for the first time, with high-temperature flue gas and the heat exchange of pebble stove ball bed, the reducing gas temperature is warming up to 850～950 ℃ from 130～150 ℃.
Further, can also carry out two preposition heat exchange of step to cold reducing gas, promptly by combustion air and the fuel gas of a flue gas generator burning part through preheating, produce about 800～900 ℃ flue gas of temperature, this flue gas mixes with waste gas of hot-blast stove flue, enter plug-in type or single hose interchanger, in interchanger, the reducing gas temperature is warming up to about 400 ℃ from 130～150 ℃, again reducing gas is sent into pebble stove and is carried out heat exchange and heat up, with temperature increase to required temperature 1100-1200 ℃ of reduction shaft furnace.Cold reducing gas is carried out two preposition heat exchange of step, help to overcome in the reducing gas heat temperature raising process and in the ball bed of hotblast stove middle and lower part, to analyse the carbon reaction, thereby realize utilizing the processing method of pebble stove heating steady in a long-term reducing gas.
Again, with nitrogen furnace atmosphere is replaced the security of hotblast stove during with the heat exchange of raising reducing gas during heat exchange.
A kind of pebble stove that is used for the reducing gas heating of the present invention comprises body of heater, and it is provided with a cavity, and cavity top is the combustion chamber, is connected with combustion air and coal combustion feed channel with hot air duct, ceramic burner through hot blast valve respectively; The cavity middle part is ball bed district, the installing heat storage; A gas passage is established in the cavity bottom, reducing gas induction trunk, flue gas exhaust channel; And be equiped with fire grate, fire grate pipe dust-removal system hot-blast furnace body comprises combustion chamber, heat-storing sphere bed and has the fire grate system of dedusting function; Described reducing gas induction trunk, flue gas exhaust channel are divided into the gas passage both sides, and described flue gas exhaust channel mouth and fire grate pipe exhanst gas outlet form a difference of altitude, forming when flue gas is discharged flows downward earlier turns around suddenly upwards to flow again, and dust in flue gas is separated.
Described heat storage is high alumina, corundum porcelain ball or magnalium ball.
Two-section type ball bed in 400 of hotblast stove middle and lower part～' 700 ℃ warm area adopts the corundum porcelain ball of surface compact but not the high alumina matter ball of porous insert, causes carbon to infiltrate the stone ball to avoid reducing the reaction of air elutriation carbon, takes place to prevent stone ball powder phenomenon-tion.The accumulation of heat of Φ 40～80mm magnalium ball is adopted in heat-storing sphere bed middle and upper part, to prevent the bonding reaction of high-temperature flue gas.
Also be provided with gas and distribute the guiding awl, be fixed in fire grate top, the uniform distribution of air-flow when being used for the heat exchange of reducing gas goal bed, thus prolong the heat exchange air-supply time.
Set up the safety anti-explosive valve at the pebble stove arch crown part, the safe pressure of explosion trap is consistent with the higher limit of reducing gas top pressure fluctuation range.
To the pebble stove heat storage operation of burning, combustion air and burning coal gas with a front preheating process burn stove, produce 1200～1300 ℃ high-temperature flue gas, after high-temperature flue gas and the heat exchange of ball bed, temperature is reduced to 250～320 ℃, through fire grate, enters the fire grate pipe, after fire grate pipe exit changes direction, enter the waste gas flue.Crude particle dust in the flue gas enters the dust collecting of fire grate bottom, regularly discharges.
The present invention compared with the prior art, advantage of the present invention is:
(1) the present invention is a kind of processing method that adopts top combustion stove heating reducing gas, it is characterized by follow-on pebble stove bottom construction.Hotblast stove fire grate top is provided with the trilateral reducing gas and distributes the guiding awl, and the uniform distribution of air-flow when being used for the heat exchange of reducing gas goal bed prolongs the heat exchange air-supply time more than 15%.Two-section type ball bed, 400～700 ℃ of warm areas in the hotblast stove middle and lower part adopt the corundum porcelain ball of surface compacts but not the high alumina matter ball of porous insert, cause carbon to infiltrate the stone ball to avoid reducing the reaction of air elutriation carbon, have prevented that stone ball powder phenomenon-tion from taking place.Employing has the fire grate system of dedusting function, and the stone ball dust that the ball bed still is difficult to avoid producing separates, and efficiency of dust collection reaches more than 60%, and protection flue trip valve has prevented the gas leak phenomenon generation.
(2) reducing gas is through secondary front preheating process to 400 ℃, and the heat transfer temperature difference that has reduced warm area in 400～700 ℃ of scopes in ball bed bottom is more than 350 ℃, avoids or greatly improve analysing carbon and being reflected in the spheroid and producing.And prolong heat-exchange time more than 30%.In addition, compare with the partial combustion temperature-rising method, reducing gas is in the heat temperature raising process, and the quality of reducing gas changes hardly.
(3) adopt combustion air, gas-fired front preheating process technology, used preheating medium comes from the useless flue gas of hot blast stove burning, improves and burns the thermo-efficiency that stove heats up, and combustion pebble stove in itself and modified version top combined, reduced the cost of reducing gas heat temperature raising.
(4) in order to improve the security of combustion formula pebble stove when heating reducing gas, set up explosion trap in pebble stove baking top bit, the safe pressure of explosion trap is consistent with the higher limit of reducing gas top pressure fluctuation range.The security of hotblast stove is replaced furnace atmosphere with nitrogen during heat exchange when improving the reducing gas heat exchange.
Description of drawings
Fig. 1 is the process flow sheet of one embodiment of the invention;
Fig. 2 is the structural representation of pebble stove of the present invention.
Embodiment
Referring to Fig. 1, embodiments of the invention 1.
This enforcement heating H
2/ CO is than the reducing gas that is 0.7, wherein CO+H
2〉=92%, its composition sees Table 1.Adopt the pebble stove heating reducing gas more than 2 or 2.The air that is bloated by combustion air blower fan 1 carries out interchanger 2 through volume damper 16, interchanger 2 can be single tube type or multitube type hot tube heat exchanger, heat transferring medium is to be 250～320 ℃ of hot-blast stove fumes, temperature rises to 130～150 ℃ after the combustion air heat exchange, cold burning coal gas 3 also rises to 130～150 ℃ through temperature after the tubular heat exchanger heat exchange, air and combustion gas through front preheating process, except that sub-fraction is used to the flue gas generator burning through valve 28 and valve 29, furnace operating is burnt in the accumulation of heat that all is used for hotblast stove.Combustion air enters ceramic burner 32 through butterfly valve 30, combustion gas and burns after gas valve 31 mixes.The 10th, follow-on top ignition pebble stove, the temperature that produces behind combustion air and the coal combustion gas firing is 1250～1400 ℃ a high-temperature flue gas heat balls bed, self is cooled to 250～320 ℃ and drains into flue through fire grate dust removing tube system row and chimney valve 35.The dustiness of flue gas when fire grate is about 500mg/Nm
3, flue gas is swerved behind dust removing tube and is drained into flue tube, and the crude particle dust in the flue gas then has little time to catch up with the dust collecting that falls into the dust removing tube bottom because of the rapid change of direction.Flue gas in the flue is drained in the atmosphere by chimney 14.
Need the cold reducing gas of heating to carry out the secondary front preheating process earlier, cold reducing gas 5 enters tubular heat exchanger 6 through valve 24, and the heat transferring medium of tubular heat exchanger 6 still is the stack gas from smoke extractor 9.Temperature rises to 130～150 ℃ after the cold reducing gas heat exchange, enters plug-in type interchanger 7 through valve 27, and temperature further rises to about 400 ℃, enters the hotblast stove heat exchange through valve 33 again.The security of hotblast stove is replaced furnace atmosphere with nitrogen during heat exchange when improving the reducing gas heat exchange.Reducing gas is rapidly heated in the hotblast stove middle and lower part to more than 700 ℃ in hotblast stove, reenter top ball bed and be warming up to 1050～1150 ℃, deliver to hot air duct through hot blast valve 39, in hot air duct, mix the suitable thermal reduction gas 13 of back formation temperature with cold reducing gas 12, deliver to shaft furnace again with temperature adjustment.Colder reducing gas direct heat exchange of reduction pneumatic transmission " wind " time " air-supply " after secondary is preposition is more than the time lengthening to 130%.
The temperature of table 1 embodiment 1 and composition change
Hotblast stove 11 switches use mutually with hotblast stove 10, and promptly when hotblast stove 10 was in the ventilation state that adds the thermal reduction gas state or be commonly called as, hotblast stove 11 was in burning accumulation of heat state or waiting status.Vice versa.
Embodiment 2:
This enforcement heating H
2/ CO is than the reducing gas that is 1.58, wherein CO+H
2〉=92%.Adopt the pebble stove heating reducing gas more than 2 or 2.The air that is bloated by combustion air blower fan 1 carries out interchanger 2 through volume damper 16, interchanger 2 can be single tube type hot tube heat exchanger or multitube type hot tube heat exchanger, heat transferring medium is to be 250～320 ℃ of hot-blast stove fumes, temperature rises to 130～150 ℃ after the combustion air heat exchange, cold burning coal gas 3 also rises to 130～150 ℃ through temperature after the tubular heat exchanger heat exchange, air and combustion gas through front preheating process, except that sub-fraction is used to the flue gas generator burning through valve 28 and valve 29, furnace operating is burnt in the accumulation of heat that all is used for hotblast stove.Combustion air enters ceramic burner 32 through butterfly valve 30, combustion gas and burns after gas valve 31 mixes.The 10th, follow-on top ignition pebble stove, the temperature that produces behind combustion air and the coal combustion gas firing is 1250～1400 ℃ a high-temperature flue gas heat balls bed, self is cooled to 250～320 ℃ and drains into flue through chimney valve 35, and drained in the atmosphere by chimney 14.
Need the cold reducing gas of heating to carry out the secondary front preheating process earlier, cold reducing gas 5 enters tubular heat exchanger 6 through valve 24, and the heat transferring medium of tubular heat exchanger 6 still is the stack gas from smoke extractor 9.Temperature rises to 130～150 ℃ after the cold reducing gas heat exchange, enters plug-in type interchanger 7 through valve 27, and temperature further rises to about 400 ℃, enters the hotblast stove heat exchange through valve 33 again.The security of hotblast stove is replaced furnace atmosphere with nitrogen during heat exchange when improving the reducing gas heat exchange.Reducing gas is rapidly heated to more than 700 in the hotblast stove middle and lower part in hotblast stove, reenter top ball bed and be warming up to 1050～1150 ℃, deliver to hot air duct through hot blast valve 39, in hot air duct, mix the suitable thermal reduction gas 13 of back formation temperature with cold reducing gas 12, deliver to shaft furnace again with temperature adjustment.
The temperature of table 2 embodiment 2 and composition change
See also Fig. 2 again, a kind of pebble stove 10 that is used for the reducing gas heating of the present invention comprises body of heater, and it is provided with a cavity 100, cavity top is combustion chamber 101, is connected with combustion air and coal combustion feed channel with hot air duct, ceramic burner 30 through hot blast valve 20 respectively; Cavity middle part 102 is ball bed district, installing heat storage 40; A gas passage 50 is established in the cavity bottom, reducing gas induction trunk 60, flue gas exhaust channel 70; And being equiped with fire grate 80, fire grate pipe dust-removal system 90, described reducing gas induction trunk 60, flue gas exhaust channel 70 are divided into gas passage 50 both sides.
Described heat storage 40 is high alumina, corundum porcelain ball or magnalium ball.
Also be provided with gas and distribute guiding awl 110, be fixed in fire grate 80 tops, the uniform distribution of air-flow when being used for the heat exchange of reducing gas goal bed, thus prolong the heat exchange air-supply time.
Set up explosion trap 120 at pebble stove body of heater 10 arch crown parts; Body of heater 100 heat storage places also have for heat storage such as metathetical pulp cutlets 130 such as high alumina, corundum porcelain ball or magnalium ball; Body of heater 100 gas passages 104 bottoms also have lets out ash mouth 140.
Claims (9)
1. the technology of a heating high concentration CO reducing gas comprises the steps:
A) to utilize temperature be 250～320 ℃ of hot-blast stove fumes carries out front preheating process one time to combustion air and burning coal gas, with its temperature increase to 130～150 ℃;
B) cold reducing gas is carried out the front preheating process first time, utilizing temperature is 250～320 ℃ of hot-blast stove fume heat exchange in hot tube heat exchanger, with its temperature increase to 130～150 ℃;
C) the pebble stove heat storage operation of burning, combustion air and burning coal gas with a front preheating process burn stove, produce 1200～1300 ℃ high-temperature flue gas, to enter pebble stove through the reducing gas of front preheating process for the first time, with high-temperature flue gas and the heat exchange of pebble stove ball bed, the reducing gas temperature is warming up to 850～950 ℃ from 130～150 ℃.
2. the technology of heating high concentration CO reducing gas as claimed in claim 1, it is characterized in that, by combustion air and the fuel gas of a flue gas generator burning part through preheating, produce about 800～900 ℃ flue gas of temperature, this flue gas mixes with waste gas of hot-blast stove flue, enter plug-in type or single hose interchanger, in interchanger, the reducing gas temperature is warming up to 400 ℃ from 130～150 ℃; Again reducing gas is sent into pebble stove and is carried out heat exchange and heat up, carry out heat exchange with spheroid in the hotblast stove, with temperature increase to 1050-1200 ℃.
3. the technology of heating high concentration CO reducing gas as claimed in claim 2 is characterized in that, the thermal reduction gas after the heating and a part of cold reducing gas are mixed " wind " operation, obtain 850～950 ℃ of the required optimal temperatures of end-use.
4. the technology of heating high concentration CO reducing gas as claimed in claim 1 is characterized in that, with nitrogen furnace atmosphere is replaced during heat exchange.
5. the technology of heating high concentration CO reducing gas as claimed in claim 2 is characterized in that, the cold reducing gas of reducing gas heating back outlet temperature through being blended into hot air duct is adjusted to 850～950 ℃ of the required optimal temperatures of end-use.
6. pebble stove that is used for reducing gas heating, it comprises,
Body of heater, it is provided with a cavity, and cavity top is the combustion chamber, is connected with combustion air and coal combustion feed channel with hot air duct, ceramic burner through hot blast valve respectively; The cavity middle part is ball bed district, the installing heat storage; A gas passage is established in the cavity bottom, reducing gas induction trunk, flue gas exhaust channel; And be equiped with fire grate, fire grate pipe dust-removal system; It is characterized in that described reducing gas induction trunk, flue gas exhaust channel are divided into the gas passage both sides, described in addition exhaust-duct mouth and fire grate exhanst gas outlet are formed with a difference of altitude.
7. pebble stove as claimed in claim 6 is characterized in that, described heat storage is high alumina, corundum porcelain ball or magnalium ball.
8. pebble stove as claimed in claim 6 is characterized in that, also is provided with gas and distributes the guiding awl, is fixed in fire grate top.
9. pebble stove as claimed in claim 6 is characterized in that the body of heater dome portions also is provided with explosion trap.
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|---|---|---|---|
| CNB2005100273989A CN100398668C (en) | 2005-06-30 | 2005-06-30 | Technological process and apparatus for heating high concentration CO and other reducing gas |
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|---|---|---|---|
| CNB2005100273989A CN100398668C (en) | 2005-06-30 | 2005-06-30 | Technological process and apparatus for heating high concentration CO and other reducing gas |
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| CN100398668C true CN100398668C (en) | 2008-07-02 |
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| CN106967861B (en) * | 2017-05-26 | 2022-05-27 | 中冶京诚工程技术有限公司 | Time-sharing preheating system for combustion air of hot blast stove |
| CN115155281B (en) * | 2022-07-08 | 2024-07-23 | 中钢设备有限公司 | Flue gas denitration hot-blast furnace |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3493344A (en) * | 1966-12-21 | 1970-02-03 | John C St Clair | Revolving pebble bed heat exchanger |
| CN2075653U (en) * | 1990-08-08 | 1991-04-24 | 梁汉诒 | Concentrate heat exchange strong wind warm ball type hot wind furnace group |
| CN1237639A (en) * | 1999-05-31 | 1999-12-08 | 宝山钢铁(集团)公司 | High air-temperature high furnace space gas preheating method |
| CN1570152A (en) * | 2004-05-10 | 2005-01-26 | 四川大学 | High wind temperature obtaining method using pure blast furnace gas combustion |
| CN1600868A (en) * | 2004-10-10 | 2005-03-30 | 北京科技大学 | A method for preheating hot blast stove gas and combustion-supporting air of high blast furnace |
-
2005
- 2005-06-30 CN CNB2005100273989A patent/CN100398668C/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3493344A (en) * | 1966-12-21 | 1970-02-03 | John C St Clair | Revolving pebble bed heat exchanger |
| CN2075653U (en) * | 1990-08-08 | 1991-04-24 | 梁汉诒 | Concentrate heat exchange strong wind warm ball type hot wind furnace group |
| CN1237639A (en) * | 1999-05-31 | 1999-12-08 | 宝山钢铁(集团)公司 | High air-temperature high furnace space gas preheating method |
| CN1570152A (en) * | 2004-05-10 | 2005-01-26 | 四川大学 | High wind temperature obtaining method using pure blast furnace gas combustion |
| CN1600868A (en) * | 2004-10-10 | 2005-03-30 | 北京科技大学 | A method for preheating hot blast stove gas and combustion-supporting air of high blast furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1888086A (en) | 2007-01-03 |
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