CN203494380U - Ammonia-process desulfurization and denitrification system for sintering flue gas based on hot sinter catalysis - Google Patents
Ammonia-process desulfurization and denitrification system for sintering flue gas based on hot sinter catalysis Download PDFInfo
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- CN203494380U CN203494380U CN201320615566.6U CN201320615566U CN203494380U CN 203494380 U CN203494380 U CN 203494380U CN 201320615566 U CN201320615566 U CN 201320615566U CN 203494380 U CN203494380 U CN 203494380U
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Abstract
The utility model discloses an ammonia-process desulfurization and denitrification system for sintering flue gas based on hot sinter catalysis. The ammonia-process desulfurization and denitrification system is used for solving the problems in the existing sintering flue gas purification that the process is complicated, the energy consumption is high and the equipment investment and operating costs are high. The ammonia-process desulfurization and denitrification system comprises a sintering machine and is characterized in that a sinter outlet of the sintering machine is connected with sinter cooling equipment, and a flue gas outlet of the sintering machine is sequentially connected with a dust removal device, the sinter cooling equipment, a heat exchange boiler, the ammonia-process desulfurization and denitrification system and a chimney. The system disclosed by the utility model has the advantages of simplicity, low energy consumption, no SCR (Selective Catalytic Reduction) catalyst consumption, good desulfurization and denitrification effects, small floor area, low investment and operating costs and environmental friendliness.
Description
Technical field
The utility model relates to a kind of flue gas purification system, specifically a kind of sintering flue gas ammonia method desulfurizing denitrating system based on heat sinter catalytic action.
Background technology
Along with the fast development of China's economy and significantly improving of industrialized level, State of Air pollution is day by day serious.2010, China sulfur dioxide (SO
2) and nitrogen oxide (NO
x) discharge capacity is respectively 2267.8 ten thousand tons and 2276.6 ten thousand tons, all occupies No. 1 in the world, national environmental protection portion environmental statistics annual report in 2010 shows, steel industry SO
2and NO
xdischarge capacity is respectively 176.65 ten thousand tons and 93.10 ten thousand tons, the prostatitis that all occupies each industrial emission source, wherein more than 70% SO
2, more than 50% NO
xfrom stove sintering machine.National environmental protection cloth promulgated by the ministries or commissions of the Central Government in 2012 < < steel sintering, pelletizing industrial air pollution thing discharge standard (GB28662-2012) > >, this standard has proposed new requirement to the discharge of sinter fume atmosphere pollution with controlling.Therefore, steel sintering flue gas desulfurization and denitrification will be steel and iron industry SO
2and NO
xthe center of gravity of emission control.
Sinter fume is the gas that contains multiple pollutant component that various powdery iron-containing raw materials, fuel and flux produce in igniting fusing, high temperature sintering forming process.Sinter fume has the large (4000～6000m of exhaust gas volumn
3/ ton sintering deposit), large (120～180 ℃), CO concentration high (0.5～2.0%) of variations in temperature, SO
2large (1000～the 3000mg/Nm of change in concentration
3), NO
xlow (300～the 500mg/Nm of concentration
3), the feature such as water capacity large (7～12%) and oxygen content high (15～18%).Compare with power-plant flue gas and have many self features, its smoke components is more complicated, changes fluctuation larger, processes more difficult.
Early, through the development of decades, desulfur technology kind is a lot of in external sintering flue gas desulfurization technical research starting, and relatively ripe.In Japan, take limestone-gypsum method and magnesium oxide method as main, the sintering flue gas desulfurization facility of building is in recent years to take activated carbon method as main.European formed and take recirculating fluidized bed as main dry method and semi-dry desulphurization technology general layout.The sintering flue gas desulfurization process that China adopts has more than 10 to plant, and has gone into operation and has mainly contained recirculating fluidized bed method, ammonia-ammonium sulfate method, limestone-gypsum method, NID method etc. at the sintering flue gas desulfurization process of building, and wherein ammonia-ammonium sulfate method desulfurization application is more.
Compare sintering flue gas desulfurization technology, sinter fume denitration technology is relatively less both at home and abroad, and particularly ripe technology still less.China's sinter fume denitration technology research is started late, and does not also develop ripe sinter fume denitration technology at present.But NH
3sCR (NH
3-SCR) method has been successfully applied to coal-fired flue gas denitration.SCR technology refers under catalyst exists, in flue gas, sprays into NH
3, make its optionally with NO
xreaction generates N
2, and not with O
2there is non-selective oxidation, thereby reach, reduce NO
xreduction temperature, raising NO
xthe object of removal efficiency.NH
3the core of-SCR technology is SCR catalyst system; SCR catalyst is different, its reductive NO
xoptimum temperature interval different.The current industrial catalyst (V for SCR denitration
2o
5-WO
3(MoO
3)/TiO
2) in 350～400 ℃ of temperature windows, there is excellent NO
xpurification efficiency, but exist catalyst cost higher, easily vulcanize the problems such as inactivation.
The states such as Germany, the U.S., Japan, Israel are on the basis of flue gas desulfurization, denitration technology research and development, several flue gas and desulfurizing and denitrifying technology have successfully been developed, as active carbon absorbs synchronized desulfuring and denitrifying technique, CuO desulfurizing and denitrifying process, electronic beam method, Absorption via Chemical Complexation etc. simultaneously.China's sinter fume pollutant comprehensive regulation is also in developing stage, and sintering flue gas and desulfurizing and denitrifying technology is also in conceptual phase.At present China's sintering flue gas desulfurization, denitration adopts associated form to carry out substantially, i.e. desulfurization separates processing with denitration, and the method for comparison main flow is the ammonia process of desulfurization-SCR denitration method that combines.The ammonia process of desulfurization-SCR denitration method purifying sintering flue gas that combines mainly contains two kinds of process routes.A kind of be adopt first dedusting again SCR denitration finally carry out the technology path of wet desulphurization, before soon flue-gas denitration process will be placed in sulfur removal technology, sinter fume after dedusting first carries out the denitration of SCR technology, then with the heat-exchanger rig processing of lowering the temperature, finally by flue gas after wet desulphurization device purifies, from chimney, discharge.This technology path exists that technique is more complicated, floor space is large and the SO of flue gas middle and high concentration
2easily make the problems such as SCR denitrating catalyst poisoning and deactivation.In order to prevent dust and SO in flue gas
2toxic action to SCR denitrating catalyst, scholar proposed first dedusting again desulfurization finally carry out the technology path of SCR denitration, after soon flue-gas denitration process will be placed in sulfur removal technology, sinter fume is first after electric precipitation, wet desulphurization, by heater, be warmed up to 350 ℃ of left and right again and carry out denitration, finally, with the heat-exchanger rig processing of lowering the temperature, after purifying, flue gas is discharged through chimney.But because this technique is first carried out wet desulphurization, flue-gas temperature significantly reduces, need to heat up and reach behind 350 ℃ of left and right through heater, can carry out denitration processing.The problems such as this technique exists energy resource consumption larger, and the higher and floor space of operating cost is larger.
Summary of the invention
The purpose of this utility model is in order to solve the problems of the technologies described above, and provides that a kind of system is simple, floor space is little, energy consumption is low, does not consume SCR catalyst, denitration desulfurized effect is good, cost of investment and low, the environment amenable sintering flue gas ammonia method desulfurizing denitrating system based on heat sinter catalytic action of operating cost.
The utility model system comprises sintering machine, and the ore outlet of described sintering machine is connected with sintering deposit cooling device, and the exhanst gas outlet of described sintering machine is connected successively with dust arrester, sintering deposit cooling device, heat exchange boiler, ammonia process of desulfurization denitrating system and chimney.
Described sintering deposit cooling device is comprised of the high temperature section connecting successively and low-temperature zone, the ore outlet of described sintering machine is connected with the high temperature section entrance of sintering deposit cooling device, the exhanst gas outlet of described sintering machine is connected with the high temperature section outlet of sintering deposit cooling device, and the high temperature section entrance of described sintering deposit cooling device is connected with heat exchange boiler.
Use the method for said system to be: to comprise after the dedusting that sintering machine is drawn sintering deposit direct heat transfer in sintering deposit cooling device of 800～900 ℃ that the sinter fume of 120～180 ℃ and sintering machine are drawn, and under sintering deposit effect, carry out optionally catalytic reduction reaction, by the NO in flue gas
xbe converted into N
2, by adding the mode of ammonia to control NH in flue gas in the sinter fume to entering before sintering deposit cooling device
3/ NO
xvolume ratio=0.4～0.5, the heat exchange that goes out sintering deposit cooling device is warming up to the denitration flue gas of 450～500 ℃ and is cooled to after 100～150 ℃ through recovery waste heat, carry out again ammonia process of desulfurization denitration and obtain clean flue gas, by chimney, discharged, the sintering deposit after heat exchange is cooled to below 150 ℃ in sintering deposit cooling device is sent into subsequent processing again.
Further, described in control, enter O in the sinter fume before sintering deposit cooling device
2concentration is percent by volume 14-18%, and NO concentration is 400mg/Nm
3, SO
2concentration be 1400mg/Nm
3.
The composition of described sintering deposit is: Fe content is 55-65wt%, and FeO content is 8.0-15.0wt%, and the content of CaO is 8.0-15wt%, SiO
2content be 5.0-10.0wt%, the content of MgO is 1.0-5.0wt%, other material total content is 0-5.0%.
In described sintering deposit cooling device, described sinter fume time of staying under 400～500 ℃ of environment is no less than 1.6s, under the environment of >=600 ℃, is no less than 0.4s.
In described sintering deposit cooling device, described sinter fume is the time of staying 1.6～2.0s under 400-500 ℃ of environment, the environment time of staying of >=600 ℃, is 0.4～2.0s.
The sinter fume that the utility model is drawn sintering machine and sintering deposit are sent in sintering deposit cooling device simultaneously, utilize the high temperature of sintering deposit to heat up to sinter fume on the one hand, make it meet the requirement of reaction temperature, on the other hand, utilize sintering deposit itself to substitute original SCR catalyst as catalyst and make sinter fume in sintering deposit cooling device, carry out optionally catalytic reduction reaction, reach the object of denitration.
In above-mentioned reaction, the utility model adopts the high temperature sintering ore deposit that sintering machine is drawn to substitute existing SCR catalyst as denitrating catalyst especially, and inventor thinks that heat sinter SCR removes NO
xreaction mechanism be Eley-Rideal type, the main component that plays catalytic action is γ-Fe
2o
3, denitration mechanism as shown in Figure 2.Its action principle is: ammonia is adsorbed on Fe
2o
3on the Lewis acidic site of iron, NH
31 H atom of molecule and Fe
2o
3the reaction of ironing surface Lattice Oxygen, is attracted to Fe from 1 electronics of N atom in ammonia
2o
3upper, meanwhile, electronics is in absorption and be adsorbed transfer mutually between species.The electronics hole forming after electronics shifts is adsorbed the NH that state ammonia produces
2the NH that free radical changes
2 -occupy, be adsorbed NH
31 N in an electrical steering Fe
2o
3in iron ion, the NH of formation
2free radical and produce NH from the NO reaction in gaseous state
2nO intermediate product, then intermediate product is decomposed into N
2and H
2o, then divalent iron ion is oxidized to 3 valency iron ions again by oxygen.γ-Fe
2o
3there is lower activation energy and in metastable condition, make the Lewis acidic site on it more active, easier same NH
3in H atom react, so γ-Fe
2o
3catalytic denitration effect better.
And, inventor also finds to adopt the sintered ore of high temperature to carry out denitration to have multi-effect: 1) in itself composition, contain the composition that acts on catalyst, and from sintering machine, that is to say, while processing sinter fume, the synchronous supply that continue that can effectively guarantee sintering deposit, has guaranteed the demand of catalyst, 2) because sintering machine is continuously supplied with heat sinter in cooling device, even if contain the SO of high concentration in flue gas
2there is not the problem as the sintering deposit generation poisoning and deactivation of catalyst yet, guaranteed normally carrying out of denitration, solved the problem of the first denitration catalyst poisoning inactivation that sulfur removal technology exists again, sinter fume can directly be sent into and in sintering deposit cooling device, first carry out denitration, and after ammonia desulfurizing process is placed on to denitration, thereby also to have solved the first desulfurization resource consumption that denitration exists again large simultaneously, the higher and large problem of floor space of operating cost, 3) high from the sintered ore temperature of sintering machine, be 800～900 ℃, this part heat meets denitration catalyst completely and reacts required reaction temperature requirement, and not needing increases heating device in addition, and the waste heat of sintering deposit is fully used, 4) because sintering deposit temperature can be up to 800～900 ℃, thereby sinter fume in sintering deposit cooling device with later stage of sintering deposit direct heat transfer, its environment temperature around can reach more than 600 ℃, and inventor's unexpected discovery at this temperature, adopt the mode of sinter fume and the reverse direct heat transfer of sintering deposit, can be along with its temperature of flow of flue gas can increase gradually, thereby can first there is the denitration of SCR, when temperature is increased to more than 600 ℃, denitration completes substantially, while now detecting the smoke components after denitration, discovery is under>=600 ℃ of high temperature, in flue gas, have 30～80mg/Nm
3nO
2generate, initial analysis is due to O in sinter fume
2concentration is up to 14～18%, and under>=600 ℃ of high temperature, the NO not being reduced in sinter fume partly can further be oxidized and generate NO
2, and this part of NO
2be conducive to synchronously NOx further be removed when the described ammonia process of desulfurization.
Further, in order to guarantee NO_x Reduction by Effective efficiency, described sinter fume time of staying under 350-600 ℃ of (preferably 400～500 ℃) environment is no less than 1.6s, to guarantee that catalytic reaction is abundant, preferably the time of staying is 1.6-2.0s, overstand can cause catalytic reaction abundant not, and the time of staying, too short meeting made NO and NH
3react abundant not, cause denitration rate low; Under the environment of>=600 ℃, be no less than 0.4s, to guarantee that oxidation reaction fully carries out, preferred 0.4-2.0s, overstand can cause NH
3oxygenation efficiency rise, the time of staying, too short meeting made NO and NH
3react abundant not, cause denitration rate low, consider ammonia utilization rate and adopt sintering deposit as the denitration efficiency of catalyst, preferably NH
3/ NO=0.4-0.5, NH
3/ NO crosses conference and causes NH
3utilization rate is low, the escaping of ammonia is serious, NH
3the too small meeting of/NO causes denitration rate too low.
Further, the composition of having made the sintering deposit of catalyst in the utility model is the sintering deposit of the sintering stone high temperature of drawing, in order to guarantee its efficient catalytic effect, in requirement sintering deposit, Fe content is for being not less than 50wt%, because in sintering deposit catalytic reaction process, the main matter that plays catalytic action is iron-based oxide, more being preferably Fe content is 55-65wt%, FeO content is 8.0-15.0wt%, and the content of CaO is 8.0-15wt%, SiO
2content be 5.0-10.0wt%, the content of MgO is 1.0-5.0wt%, other material total content is 0-5.0%.
In the utility model system, in order to make as early as possible sinter fume be warming up to denitration window temperature, preferred described sinter fume can be directly entered by the high temperature section outlet of sintering deposit cooling device, by high temperature section entrance, discharged, high temperature section and direct reverse contact of sintering deposit, NO_x Reduction by Effective at sintering deposit cooling device.
Beneficial effect:
1. the utility model is usingd iron-based oxide (heat sinter) as the completely alternative existing SCR catalyst of denitrating catalyst, its wide material sources, cost are lower, greatly reduce the operating cost of system, and, sinter fume is directly carried out after dedusting to denitration, also do not exist making the problem as the sintering deposit inactivation of denitrating catalyst.
2. the utility model makes full use of sintering deposit waste heat and heats flue gas, does not need additionally to supplement the energy to flue gas, makes its window temperature that reaches SCR denitration, and after heating, flue-gas temperature reaches 450-500 ℃ simultaneously, can be used;
3. the utility model system is simple, floor space is less, and the catalytic reaction of denitration completes in sintering deposit cooling device, does not need additionally to install SCR denitration reaction system, equipment investment cost; Whole system utilization rate of waste heat is high, and energy conservation and consumption reduction effects is remarkable.
4. the utility model system can realize sintering flue gas and desulfurizing and denitrifying, and good purification, to NO
xcontent up to 300-500mg/Nm
3, sulphur is up to 1000-3000mg/Nm
3sinter fume all applicable, its desulfuration efficiency>=95%, denitration efficiency is 50-70%, the flue gas after purification meets the sinter fume discharge standard (GB28662-2012) of national regulation.
Accompanying drawing explanation
Fig. 1 the utility model process chart and system diagram.
The reaction mechanism figure of Fig. 2 heat sinter SCR NO_x removal.
Fig. 3 is reaction temperature and NH in the utility model
3the impact of/NO comparison denitration efficiency.
The impact of Fig. 4 sinter fume time of staying on denitration efficiency.
Fig. 5 reaction temperature is to NO
2the impact of growing amount.
Wherein, 1-sintering machine, 2-dust arrester, 3-sintering deposit cooling device, 3.1-high temperature section, 3.2-low-temperature zone, 4-heat exchange boiler, 5-ammonia process of desulfurization denitrating system, 6-chimney.
The specific embodiment
The reason of the reaction in described SCR denitration stage is as follows:
When reaction temperature is 350-600 ℃, the NO in flue gas
xwith NH
3under heat sinter effect, carry out optionally catalytic reduction reaction, by the NO in flue gas
xbe converted into N
2(as reaction equation (1)-(3)), thus realize SCR denitration, due to O in sinter fume
2concentration is up to 14-18%, and therefore, under high temperature (>=600 ℃), the NO not reacted partly can further be oxidized and generate NO
2((as reaction equation (4)-(5)).
Described ammonia process of desulfurization denitrating technique, the nitre not removing in desulfurization simultaneously can also simultaneous removing flue gas, its reaction principle is as follows:
Sinter fume after denitration is incorporated in desulphurization denitration tower, adopts ammoniacal liquor as the absorbent of synchronized desulfuring and denitrifying, and its chemical equation is as follows:
2NH
3+H
2O+SO
2→(NH
4)
2SO
3 (6)
NH
3+H
2O+SO
2→NH
4HSO
3 (7)
(NH
4)
2SO
3+H
2O+SO
2→2NH
4HSO
3 (8)
The acid salt NH generating in absorption process
4hSO
3to SO
2do not there is absorbability, along with the carrying out of absorption process, NH in absorption liquid
4hSO
3quantity increase, the absorbability of absorption liquid declines, and therefore need in absorption liquid, supplement ammoniacal liquor (pH that controls absorption liquid is 5.0-6.5), make it be converted into (NH
4)
2sO
3to keep the absorbability of absorption liquid, its equation is as follows:
NH
4HSO
3+NH
3+H
2O→(NH
4)
2SO
3 (9)
To the absorbent of synchronized desulfuring and denitrifying-ammoniacal liquor, adding ferrous salt is that main complexing agent is to improve absorption liquid to NOx complexed absorption effect.Its chemical equation is as follows:
2NH
3+H
2O+2NO
2→2NH
4NO
3 (11)
(NH in absorption liquid
4)
2sO
3except absorbing SO in flue gas
2outward, also to the NO in flue gas
xhave certain reduction, it is as follows that its chemical reaction becomes:
2(NH
4)
2SO
3+2NO→2(NH
4)
2SO
3+N
2 (12)
4(NH
4)
2SO
3+2NO
2→4(NH
4)
2SO
4+N
2 (13)
System embodiment:
The ore outlet of sintering machine 1 is connected with high temperature section 3.1 entrances of sintering deposit cooling device 3, and the exhanst gas outlet of described sintering machine 1 is connected successively with dust arrester 2, sintering deposit cooling device 3, heat exchange boiler 4, ammonia process of desulfurization denitrating system 5 and chimney 6.Described sintering deposit cooling device 3 is comprised of the high temperature section 3.1 connecting successively and low-temperature zone 3.2, the ore outlet of described sintering machine 1 is connected with the high temperature section entrance 3.1 of sintering deposit cooling device 2, the exhanst gas outlet of described sintering machine 1 is connected with high temperature section 3.1 outlets of sintering deposit cooling device 3 through dust arrester 2, and high temperature section 3.1 entrances of described sintering deposit cooling device 2 are connected with heat exchange boiler 4.Described sintering deposit cooling device 2 is preferably ring-like cooler, and the present embodiment comprises 5 cooling sections, by sintering deposit entrance, to outlet, is followed successively by I section, II section, III section, IV section, V section, and wherein I-III section is high temperature section 3.1, and IV section and V section are low-temperature zone 3.2.Described ammonia process of desulfurization denitrating system 5 is the existing system (for prior art, not being described further) that realizes ammonia process of desulfurization denitrating technique.The present embodiment 1 low-temperature zone 3.2 is usingd air as heat transferring medium, and the air outlet slit of low-temperature zone 3.2 is also connected with chimney 6.
Process example:
The flue gas of the 120-180 that sintering machine 1 is drawn ℃ (claiming again sinter fume) is through dust arrester 2 dedustings, and the sinter fume temperature after dedusting is 120-180 ℃, wherein O in flue gas
2content be 14-18vol%, CO
2content be 3.0-7.0vol%, the content of CO is 0-2.0vol%, NO
x,content be 300-500mg/Nm
3(the wherein NO of 90-95%), SO
2,content be 1000-3000mg/Nm
3; In the flue gas after dedusting, spray into NH
3control the NH in flue gas
3/ NO
x=0.4-0.5 sends into high temperature section 3.1 outlets of sintering machine 1; (temperature of the sintering deposit that sintering machine is drawn is 800-900 ℃ to the sintering deposit that sintering machine is drawn, and particle diameter is 1-100mm, and wherein, to add up to total amount 100%, Fe content is 55-65wt%, and FeO content is 8.0-15.0wt%, and the content of CaO is 8.0-15wt%, SiO
2content be 5.0-10.0wt%, the content of MgO is 1.0-5.0wt%, other material total content is 0-5.0%.High temperature section 3.1 entrances by sintering deposit cooling device 3 enter, low-temperature zone outlet is discharged, the reverse direct heat transfer of heat exchanging segment 3.1 in sintering deposit cooling device 3 of described flue gas and sintering deposit, flue gas is in heat exchanging segment Way out traveling process, environment temperature raises gradually, first under the environment of 300-600 ℃, (flue gas is no less than 1.6s in the time of staying of this temperature range, preferred 0.6-2s), heat sinter is as catalyst, the NO in flue gas
xwith NH
3under sintering deposit effect, carry out optionally catalytic reduction reaction and carry out denitration, partly transfer the NO in flue gas to N
2and NO
2, being greater than (flue gas is no less than 0.4s in the time of staying of this temperature range, preferably 0.4-2s) under the environment of 600 ℃, the NO not being reduced partly can further be oxidized and generate NO
2the denitration flue gas of the 450-500 after denitration ℃ is sent into waste heat boiler 4 recovery heat energy by high temperature section entrance 3.1 discharges of tying ore deposit cooling device 3 and is cooled to 100-150 ℃, and the denitration flue gas after heat exchange is introduced ammonia process of desulfurization denitrating system 5 and removed the SO in flue gas by ammonia desulfurizing process
2and NO
x, the temperature of the clean flue gas after desulfurization is down to 50-60 ℃ and is directly discharged through chimney, and the sintering deposit below 150 ℃ in sintering deposit cooling device 2 after heat exchange cooling is discharged and is sent into subsequent processing by the outlet of low-temperature zone 3.1.The cooling medium of described sintering deposit cooling device 2 low-temperature zone 3.2 is air, after heat exchange, is discharged together with clean flue gas by chimney.
The concentration that records NOx in ammonia process of desulfurization operation outlet flue gas is 105-250mg/Nm
3, SO
2concentration be 20-150mg/Nm
3.The utility model desulfuration efficiency is 95-98%, and denitration efficiency is 50-70%.
According to the method described above, the flue gas of the different N Ox concentration that sintering machine 1 is drawn is processed, and it is processed index and sees the following form.
Claims (2)
1. the sintering flue gas ammonia method desulfurizing denitrating system based on heat sinter catalytic action, comprise sintering machine, it is characterized in that, the sintering deposit outlet of described sintering machine is connected with sintering deposit cooling device, and the exhanst gas outlet of described sintering machine is connected successively with dust arrester, sintering deposit cooling device, heat exchange boiler, ammonia process of desulfurization denitrating system and chimney.
2. the system as claimed in claim 1, it is characterized in that, described sintering deposit cooling device is comprised of the high temperature section connecting successively and low-temperature zone, the sintering deposit outlet of described sintering machine is connected with the high temperature section entrance of sintering deposit cooling device, the exhanst gas outlet of described sintering machine is connected with the high temperature section outlet of sintering deposit cooling device, and the high temperature section entrance of described sintering deposit cooling device is connected with heat exchange boiler.
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| CN103900391A (en) * | 2014-04-14 | 2014-07-02 | 北京京诚泽宇能源环保工程技术有限公司 | Selective sintering-machine flue-gas heat exchange and denitration system and method thereof |
| CN107198959A (en) * | 2017-06-13 | 2017-09-26 | 武汉钢铁有限公司 | Sinter flue dust self-catalysis denitrating system |
| CN107198944A (en) * | 2017-06-13 | 2017-09-26 | 武汉钢铁有限公司 | Sintering flue gas self-catalysis denitrating technique based on bellows flue dust UTILIZATION OF VESIDUAL HEAT IN |
| CN107198960A (en) * | 2017-06-13 | 2017-09-26 | 武汉钢铁有限公司 | One kind sintering online self-catalysis denitrification apparatus of flue dust |
| CN107198944B (en) * | 2017-06-13 | 2020-04-07 | 武汉钢铁有限公司 | Self-catalytic denitration process for sintering flue gas based on utilization of waste heat of flue dust of air box |
| CN108355488A (en) * | 2018-03-21 | 2018-08-03 | 中南大学 | A kind of waste gas circulation method of denitration of iron ore pellets |
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