CN104353350B - The flue gas purifying technique realized based on absorbent pretreatment - Google Patents
The flue gas purifying technique realized based on absorbent pretreatment Download PDFInfo
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- CN104353350B CN104353350B CN201410716386.6A CN201410716386A CN104353350B CN 104353350 B CN104353350 B CN 104353350B CN 201410716386 A CN201410716386 A CN 201410716386A CN 104353350 B CN104353350 B CN 104353350B
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Abstract
The invention discloses the flue gas purifying technique realized based on absorbent pretreatment, described flue gas purifying technique includes by flue gas system, the former flue gas in main chimney flue is sent into SO2Absorption system, described flue gas system mainly auxiliary flue and flue collector by being interconnected forms, it is provided with impact grinding pulverizing grading machine in auxiliary flue, former flue gas includes the auxiliary flue gas by auxiliary flue and by the flue gas of flue collector, absorbent sends into impact grinding pulverizing grading machine with auxiliary flue gas, after the primary mixture obtained enters flue collector and flue gas hybrid reaction, deliver to SO in the lump2Absorption system.Present invention is specifically directed to the thick of flue gas purify technique and design, be greatly improved the denitrification efficiency of absorbent, the treatment effeciency improving follow-up desulfurizing and denitrifying process is had high facilitation.
Description
Technical field
The present invention is the flue gas purifying technique realized based on absorbent pretreatment, is specifically related to the technical finesse using desulfurizing and denitrifying process during realizing stack gas cleaning to carry out absorbent, belongs to stack gas cleaning field.
Background technology
The constantly progress of the industry such as oil and chemical industry is while promoting economic development, also pollution is caused to environment, at present, global pollution problem is on the rise, more causing common concern and the attention of countries in the world, the especially discharge etc. of coal-fired power plant, coal-burning boiler and flue gas of refuse burning, the pollution to air is the most serious, it is known that containing substantial amounts of flue dust, carbon dioxide, SO in coal-fired flue-gas2And NOXDeng harmful substance, wherein, the carbon dioxide of fuel combustion discharge is the main matter causing greenhouse effect；SO2、NOXAnd fly ash granule is again the main source of atmospheric pollution；Certainly, the flue dust that the flue gas such as coal-burning boiler produces also is the one of the main reasons causing atmospheric pollution, and its main component is also SO2And NOX.It is reported, China there are about the city suspended particulates level of 70% and exceeds standard, the SO in the peri-urban air of 2/32Exceeding standard, therefore, for improving the air quality of current environment, improvement and the reduction of discharging of these pollutant are the most very urgent.
In China, flue gas desulfurization and denitrification is topmost measure in air contaminant treatment, flue gas desulfurization technique is a lot of both at home and abroad, such as limestone-gypsum method, ammonia process, Dual alkali, rotary spraying technique etc., wherein from the point of view of the desulfurization technology of industrialization, though have that floor space is big, operating cost is high, easy blocking, desulfurizing byproduct difficulty are put, secondary pollution problems and and be unsuitable for China's national situation, but due to history, account for absolute leading position is still limestone-gypsum method.And in terms of gas denitrifying technology, the most selective catalytic reduction method (SCR), SNCR method (SNCR), electron beam irradiation method, impulse electric corona plasma method, red-hot carbon reduction method, low temperature normal atmosphere plasma decomposition method etc. are the most universal with SCR method denitration application the most again.
At present, Application comparison flue gas desulfurization and denitrification technology widely is then to utilize above-mentioned traditional flue gas desulfurization technique combined with SCR denitration technology in the world, with reach can the purpose of desulphurization denitration, although this technology can remove the SO of more than 90%2With more than 80% NOx, but this method in fact remains being applied in combination of independent desulphurization and denitration technology, more have the disadvantage that above-mentioned desulphurization and denitration technology exists concurrently, fail to break away from technological process length, investment is big, operating cost is high, Technical Economy is poor, easily cause secondary pollution problems.From existing patent documentation CN102489129A(industrial flue gas cleaning denitration integrated device and method of work thereof, 2012.06.13), CN203108424U(mono-kind carries out the flue gas processing device of desulfurization and denitration simultaneously, 2013.08.07) it is understood that, combined desulfurization and denitration technology is increasingly becoming the developing direction of smoke gas treatment, but the integrated technique of this kind of fume desulfuring and denitrifying is the most ripe, for improving the treatment effeciency of follow-up desulfurizing and denitrifying process, generally use pretreatment flue to the SO in flue gas in desulfurization process front end2Or NOXSlightly purify, the mode used includes ozone injection, cooling, absorbent etc., and for example patent documentation CN102363095A(flue gas dry desulfurizing process and flue gas dry desulfurizing system thereof, 2012.02.29), CN103990375A(semidry method sintering flue gas integrated purifying method, 2014.08.20) etc., in actual use, the embodiment from the technical process of whole desulfurization (denitration) of its treatment effeciency is but and inconspicuous, therefore, their industrial applications is also and inconspicuous.
Summary of the invention
It is an object of the invention to provide the flue gas purifying technique realized based on absorbent pretreatment, this flue gas purifying technique is specifically designed for the thick of flue gas and purifies technique and design, the flue gas system used mainly auxiliary flue and flue collector by being interconnected forms, by auxiliary flue gas, absorbent can be introduced impact grinding pulverizing grading machine, while absorbent being carried out pretreatment and obtains primary mixture, utilize absorbent that auxiliary flue gas is carried out desulphurization denitration process, absorbent in primary mixture is active because of reaction, mix with flue gas again after being admitted to flue collector and react, it is greatly improved the denitrification efficiency of absorbent, the treatment effeciency improving follow-up desulfurizing and denitrifying process had high facilitation.
The present invention is achieved through the following technical solutions: the flue gas purifying technique realized based on absorbent pretreatment, described flue gas purifying technique includes by flue gas system, the former flue gas in main chimney flue is sent into SO2Absorption system, in tradition flue gas purification system, absorbent is typically to be ground into absorbent granules by grinding machine system after metering, send into flue collector by dry powder ejector the most again mix with former flue gas and react, absorbent is relatively low to the denitrification efficiency of former flue gas, for improving the work efficiency of absorbent, flue gas system is improved by the present invention, in the present invention, described flue gas system mainly auxiliary flue and flue collector by being interconnected forms, it is provided with impact grinding pulverizing grading machine in auxiliary flue, former flue gas includes the auxiliary flue gas by auxiliary flue and by the flue gas of flue collector, absorbent sends into impact grinding pulverizing grading machine with auxiliary flue gas, after the primary mixture obtained enters flue collector and flue gas hybrid reaction, deliver to SO in the lump2Absorption system, when practical operation, the absorbent of impact grinding pulverizing grading machine is sent into pulverized while with auxiliary flue gas, carry out reacting and obtaining primary mixture with auxiliary flue gas, absorbent in this primary mixture is active because of reaction, when being sent to flue collector with flue gas hybrid reaction, its denitrification efficiency is the highest, and practical effect is good.
In the present invention, the former flue gas coming from main chimney flue sends into flue collector through flue gas booster fan, a part of former flue gas enters auxiliary flue through auxiliary flue entrance end, it is referred to as assisting flue gas, the former flue gas of another part continues to stay flue collector, it is referred to as flue gas, auxiliary flue gas drives absorbent to enter impact grinding pulverizing grading machine in the lump, absorbent carry out in impact grinding pulverizing grading machine pretreatment and with auxiliary smoke reaction, the primary mixture obtained delivers to flue collector through auxiliary flue outlet end, after carrying out hybrid reaction with the flue gas in flue collector again, deliver to SO in the lump2Absorption system, in actual application, described flue gas is (9～19) with the volume ratio of auxiliary flue gas: 1.
nullFor preferably realize absorbent pretreatment and auxiliary flue gas slightly walk purification，Tradition grinding machine system is improved by the present invention，Use impact grinding pulverizing grading machine，Described impact grinding pulverizing grading machine includes flour mill、Grader and high-pressure suction fan，Described absorbent and auxiliary flue gas send into flour mill with high-pressure suction fan，Send into grader with auxiliary flue gas again after absorbent is crushed to screen，The absorbent of granularity≤40um mixes acquisition primary mixture with air-flow，The absorbent of granularity ＞ 40um returns again to flour mill and proceeds to pulverize，When practical operation，Auxiliary flue gas and absorbent are first fed to flour mill and carry out pretreatment (pulverizing)，React with auxiliary flue gas while that absorbent being pulverized，Effect due to high-pressure suction fan，Pretreated absorbent is sent into grader in the lump under the drive of auxiliary flue gas again and is screened，Reference area and the porosity of the absorbent that pretreatment makes are significantly greatly increased，The desulfuration efficiency that improve absorbent of high degree.
In the present invention, after absorbent is first fed into absorbent feed bin, flour mill is delivered to again after absorbent conveyer device delivers to absorbent metered dispensing unit, absorbent described in realization sends into flour mill after metering, and when reality is applied, absorbent is the most excessive, simultaneously, also to measure according to the content of pollutant in former flue gas, for former flue gas, its pollutant load is generally 200～9000mg/Nm3In the range of, described absorbent is 100～460g/Nm with the mixing ratio of auxiliary flue gas3, send into flour mill after metering.
Further, described absorbent includes NaHCO3、KHCO3、Mg(HCO3)2In one or more composition mixture.
Another kind of situation, described absorbent includes Na2CO3、K2CO3、CaCO3、MgCO3In one or more composition mixture.
For improving being sufficiently mixed and contacting of primary mixture and flue gas, the present invention arranges gas mixer on described flue collector, described primary mixture and flue gas hybrid reaction in gas mixer, the absorbent in described primary mixture is 6～23g/Nm with the mixing ratio of flue gas3。
In actual production process, high-pressure suction fan can use the following two kinds mode to be configured:
One is, described high-pressure suction fan is arranged at the front end of flour mill, described auxiliary flue gas is sequentially sent to flour mill and grader after sending into high-pressure suction fan along auxiliary flue again, absorbent is then fed directly to flour mill, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, a part of absorbent mixes composition primary mixture with auxiliary flue gas, gas mixer is delivered under the power that high-pressure suction fan provides, another part absorbent returns again to flour mill and proceeds to pulverize.
From above-mentioned situation, described high-pressure suction fan is positive pressure operation, and its operation pressure is 10～13kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 5～8kpa, and another part is then the pressure overcoming gas mixer, about 5 kpa.
Another kind is, described grader is arranged at the front end of high-pressure suction fan, described auxiliary flue gas is sequentially sent to flour mill along auxiliary flue, grader and high-pressure suction fan, absorbent and auxiliary flue gas are admitted to flour mill, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, a part of absorbent mixes composition primary mixture with flue gas, and deliver to gas mixer through high-pressure suction fan, another part absorbent returns again to flour mill and proceeds to pulverize.
From above-mentioned situation, described high-pressure suction fan is negative-pressure operation, and its operation pressure is 10～13kpa, a pressure part for high-pressure suction fan is to overcome the resistance of flour mill and grader, about 5～8kpa, another part is the pressure overcoming gas mixer, about 5 kpa.
In above-mentioned two situations, the pressure of the primary mixture delivering to gas mixer is 5 kpa.
In the present invention, described SO2nullAbsorption system includes being provided with spraying layer and the absorption tower of doctor solution blood circulation，Described flue collector is connected with absorption tower，It is provided with at the top on absorption tower for purifying the flue that gas is discharged，The waste liquid comb discharged for desulfurization slurry then it is provided with in the bottom on absorption tower，Its concrete operations flow process is as follows: the smoke mixture that primary mixture is formed after being admitted to flue collector and flue gas hybrid reaction sends into absorption tower by flue collector again，Spraying layer is arranged in absorption tower，After circulating pump is pressurizeed by doctor solution blood circulation，By doctor solution by the nozzle plenum ejection of distribution on spraying layer，And form the desulfurization droplet that substantial amounts of specific surface area is bigger，On the one hand，Smoke mixture enters the middle part on absorption tower，Rapid decreasing temperature and increasing humidity in tower，And meet head on to contact with the desulfurization droplet of reverse high-speed motion，There is strong action of turbulent flow，Gas、Liquid is biphase carries out abundant mass-and heat-transfer，SO in smoke mixture2Absorbed in a large number；On the other hand, after absorbent granules in smoke mixture enters in tower, on equally with gas flow counterflow, sufficiently contact with top-down doctor solution, the absorbent granules of excess is dissolved in doctor solution, the SO remained in circulation continuation absorption flue gas in tower under the effect of doctor solution blood circulation with desulfurization slurry2、NOYAnd heavy metallic oxide, SO2Removal efficiency may be up to 98%, the purification gas after desulfurization can directly be discharged by flue after reaching discharging standards, and desulfurization slurry is in cyclic process, owing to constantly absorbing SO2, after reaching finite concentration, i.e. delivered to Sewage Disposal by waste liquid comb.
The present invention compared with prior art, has the following advantages and beneficial effect:
(1) present invention is specifically directed to the thick of flue gas purify technique and design, by assisting flue gas that absorbent introduces impact grinding pulverizing grading machine, while absorbent being carried out pretreatment and obtains primary mixture, utilize absorbent that auxiliary flue gas is carried out desulphurization denitration process, absorbent in primary mixture is active because of reaction, mix with flue gas again after being admitted to flue collector and react, it is greatly improved the denitrification efficiency of absorbent, the treatment effeciency improving follow-up desulfurizing and denitrifying process is had high facilitation.
(2) present invention is reasonable in design, flue collector is provided with auxiliary flue, by auxiliary flue gas, absorbent is introduced impact grinding pulverizing grading machine and carry out pretreatment, in the present invention, the air-flow entering impact grinding pulverizing grading machine is auxiliary flue gas, avoid concentration and the EGT using other gas to reduce pollutant in waste gas, simultaneously, owing to introducing air-flow for auxiliary flue gas, while absorbent is carried out pretreatment, auxiliary flue gas can also react with absorbent, and make absorber band active, be conducive to improving the denitrification efficiency of waste gas, in auxiliary flue, the thick purifying rate of waste gas can reach 90～99%.
(3) principle of the invention is simple, auxiliary flue gas and absorbent are introduced to impact grinding pulverizing grading machine with high-pressure suction fan and crush, absorbent spatial dispersion between grader and flour mill and turbulence, and crushed by the synergism of impact grinding pulverizing grading machine and auxiliary flue gas, crushing efficiency is high, the specific surface area and porosity of the preprocessed absorbent obtained is significantly greatly increased, and in actual use, absorbent is crushed to grain graininess≤40um, pore volume is 0. 0317 m3/ g, specific surface area 4.2m2The microgranule of/g.
(4) the auxiliary flue gas that the present invention uses comes from former flue gas, when actually used, owing to the temperature of former flue gas is higher, absorbent is while broken, more effectively can react with auxiliary flue gas, improve the treatment effeciency of absorbent, when actually used, the temperature of the auxiliary flue gas entering impact grinding pulverizing grading machine can reach 90～200 DEG C, and practical effect is good.
(5) the impact grinding pulverizing grading machine that the present invention relates to mainly is made up of flour mill, grader and high-pressure suction fan, unlike traditional grinding machine system, the impact grinding pulverizing grading machine that the present invention uses eliminates the setting of traditional whirlwind and bag collector, avoid the absorbent after pulverizing to reunite, sufficiently maintaining the activity of pretreatment absorbent, practicality is extremely strong.
(6) flexible operation of the present invention, the impact grinding pulverizing grading machine related to includes that two kinds are implemented operating mode, and one is that high-pressure suction fan uses positive pressure operation, is avoided that the absorbent granules abrasion to blower fan after pulverizing, reduces the wear-resisting requirement of equipment；Another kind is that high-pressure suction fan uses negative-pressure operation, is avoided that flour mill and grader occur that dust is revealed, but need to improve the Wear-resistant Treatment degree of high-pressure suction fan.
(7) time for reducing high-pressure suction fan negative-pressure operation, the absorbent granules abrasion to high-pressure suction fan, the runner of the high-pressure suction fan that the present invention relates to uses erosion resistant to process, and has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
(8) present invention is additionally provided with gas mixer on flue collector, this gas mixer can make the primary mixture of feeding flue collector and the mixing that flue gas is full and uniform, be conducive to the absorbent thick purification to flue gas, in flue collector, the primary mixture introduced can reach 80～90% with the first purifying rate of flue gas, and denitrification efficiency is high.
(9) present invention is in improving the rough purification process of flue while denitrification efficiency, also reduces follow-up SO2The purification pressure of absorption system, in actual mechanical process, absorption tower is to SO in smoke mixture2Removal efficiency may be up to 98%, the desulfurization slurry of the generation in sweetening process is then emitted into Sewage Disposal and processes.
Accompanying drawing explanation
Fig. 1 is the control schematic diagram of structure shown in the present invention.
Fig. 2 is structural plan during high-pressure suction fan of the present invention employing positive pressure operation.
Fig. 3 is structural plan during high-pressure suction fan of the present invention employing negative-pressure operation.
Fig. 4 is the structural representation on absorption tower of the present invention.
Wherein 1 flue collector, 2 auxiliary flues, 3 spraying layers, 4 absorption towers, 5 flues, 6 waste liquid combs, 7 circulating pumps.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described in further detail, but embodiments of the present invention are not limited to this.
Embodiment 1:
In traditional flue gas purifying method, the thick technique that purifies of former flue gas is generally included by absorbent: measure absorbent, it is then fed into grinding machine system to pulverize, absorbent granules after pulverizing is sent into flue collector 1 by dry powder ejector again and is mixed with former flue gas and react, in the process, absorbent is usually about 50% to the purification efficiency of former flue gas, desulfuration efficiency is relatively low, therefore, for improving the work efficiency of absorbent, the present invention proposes the flue gas purifying technique realized based on absorbent pretreatment, this flue gas purifying technique includes by flue gas system, the former flue gas in main chimney flue is sent into SO2Absorption system, for overcoming drawbacks described above, flue gas system is improved by the present invention, in the present invention, flue gas system mainly auxiliary flue 2 and flue collector 1 by being interconnected forms, meanwhile, being additionally provided with impact grinding pulverizing grading machine in auxiliary flue 2, its technological process is as follows: the former flue gas coming from main chimney flue delivers to SO along flue collector 12During absorption system, former flue gas is split forming auxiliary flue gas and flue gas, the impact grinding pulverizing grading machine that absorbent is sent in auxiliary flue 2 with auxiliary flue gas carries out pretreatment (pulverizing), it is thus achieved that primary mixture enter flue collector 1 and flue gas hybrid reaction after, deliver to SO in the lump2Absorption system, when practical operation, the absorbent of impact grinding pulverizing grading machine is sent into pulverized while with auxiliary flue gas, carry out reacting and obtaining primary mixture with auxiliary flue gas, absorbent in this primary mixture is active because of reaction, when being sent to flue collector 1 with flue gas hybrid reaction, its denitrification efficiency is the highest, it is proven, absorbent can reach 90～99% to the thick purifying rate of auxiliary flue gas, after primary mixture is sent to flue collector 1, the thick purifying rate of the flue gas in flue collector 1 be can reach 80～90%, simultaneously, follow-up SO can also be effectively reduced2The purification pressure of absorption system, it is the most reasonable to design.
Embodiment 2:
The present embodiment is with the difference of embodiment 1: in the present embodiment, and after former flue gas is split, auxiliary flue gas and the volume ratio by the flue gas of flue collector 1 by auxiliary flue 2 are 9:1 respectively.
In the actual application of the present embodiment, former flue gas sends into flue collector 1 through flue gas booster fan, a part of former flue gas enters auxiliary flue 2 through auxiliary flue 2 arrival end, it is referred to as assisting flue gas, the former flue gas of another part continues to stay flue collector 1, it is referred to as flue gas, auxiliary flue gas drives absorbent to enter impact grinding pulverizing grading machine in the lump, absorbent carry out in impact grinding pulverizing grading machine pretreatment and with auxiliary smoke reaction, the primary mixture obtained delivers to flue collector 1 through flue outlet end, after carrying out hybrid reaction with the flue gas in flue collector 1 again, deliver to SO in the lump2Absorption system.
Embodiment 3:
The present embodiment is with the difference of embodiment 2: in the present embodiment, impact grinding pulverizing grading machine is mainly by flour mill, grader and high-pressure suction fan composition, absorbent and auxiliary flue gas send into flour mill with high-pressure suction fan, send into grader with auxiliary flue gas again after absorbent is crushed to screen, in actual mechanical process, primary mixture can be selected by the rotating speed of regulation grader, in primary mixture, the granularity of absorbent is controlled in 10～40um under normal circumstances, that is: the absorbent of granularity≤40um mixes acquisition primary mixture with auxiliary flue gas, the absorbent of granularity ＞ 40um returns again to flour mill and proceeds to pulverize.
Owing to the introduction volume of absorbent is relevant to the pollutant load in former flue gas, therefore, when actually used, also need the pollutant in former flue gas are monitored, after absorbent being carried out measure control according to Monitoring Data, absorbent is sent into flour mill again, and the present embodiment is applicable to pollutant load at 200mg/Nm3In the range of the thick purification of former flue gas, the absorbent of introducing is 100g/Nm with the mixing ratio of auxiliary flue gas3, after impact grinding pulverizing grading machine pretreatment, absorbent can reach 90% to the thick purifying rate of auxiliary flue gas.
Embodiment 4:
The present embodiment is with the difference of embodiment 3: in the present embodiment, and the absorbent of use includes NaHCO3、KHCO3、Mg(HCO3)2The mixture of composition, NaHCO in this mixture3、KHCO3、Mg(HCO3)2Mass ratio be 1:0.05:0.05, the desulphurization denitration being applicable to former flue gas slightly purifies, and its chemical reaction process includes:
Desulfurization: 2HCO3 —+ SO2
+ ½O2 ↔ SO4 2 —+ H2O + 2CO2；
2HCO3 — + SO3 → SO4 2 — + 2 CO2 + H2O；
Denitration: 2HCO3 —+ SO2 + NO + O2
↔ SO4 2 —+ NO2 + H2O + 2CO2；
2HCO3 — + 2NO2 + ½O2
↔ 2NO3 —+ H2O + 2CO2；
4SO3 + 2NO2
↔ 4SO4 2 — + N2；
2NO + 2SO2 ↔ 2SO3
+ N2；
2HCO3 —+ SO3 ↔ SO4 2 —+ H2O + 2CO2。
Embodiment 5:
The present embodiment is with the difference of embodiment 4: in the present embodiment, and the absorbent of use includes Na2CO3、K2CO3、CaCO3、MgCO3The mixture of composition, Na in this mixture2CO3、K2CO3、CaCO3、MgCO3Mass ratio be 1:0.05:0.1:0.05, it is adaptable to the desulphurization denitration of former flue gas slightly purifies, and its chemical reaction process includes:
Desulfurization: 2CO3 —+ SO2 + ½O2
↔ SO4 2 —+ H2O + 2CO2；
2CO3 — + SO3 → SO4 2 — + 2 CO2 + H2O；
Denitration: 2CO3 —+ SO2 + NO + O2
↔ SO4 2 —+ NO2 + H2O + 2CO2；
2CO3 — + 2NO2 + ½O2
↔ 2NO3 —+ H2O + 2CO2；
4SO3 + 2NO2
↔ 4SO4 2 — + N2；
2NO + 2SO2 ↔ 2SO3
+ N2；
2CO3 —+ SO3 ↔ SO4 2 —+ H2O + 2CO2。
Embodiment 6:
The present embodiment is with the difference of embodiment 3: the present embodiment is provided with gas mixer on flue collector 1, primary mixture and flue gas are sufficiently mixed reaction in gas mixer, for ensureing the denitrification efficiency of flue gas, in primary mixture, absorbent should be 6g/Nm with the mixing ratio of flue gas3.In actual application, determination to the absorbent consumption that flour mill introduces, not only need the total amount of pollutant in former flue gas is detected, also need to the total amount of pollutant in flue collector after gas mixer 1 is detected, both data common feedback just can complete to the metering control system of absorbent, its control flow is as shown in Figure 1, former flue is provided for former flue gas pollutant, flow, pressure, the former flue gas composition detector of temperature diagnosis, the detection signal of former flue gas pollutant delivers to control system, control system calculates, according to former flue gas inspection signal, the total amount of pollutants discharge that need to process, reset the absorbed dose needing to add, absorbent addition signal is transferred to absorbent metered dispensing unit, absorbent is delivered to flour mill.Flue gas inspection instrument after the purification of flue gas pollutant after thick purification, flow, pressure, temperature diagnosis is set on flue after cleaning, after the purification detected, smoke signal feeds back to control system together with the pulse measurement signal of absorbent metered dispensing unit, and absorbent setting value is modified according to the signal fed back and constitutes a complete control system by control system.
Embodiment 7:
The present embodiment is with the difference of embodiment 6: the high-pressure suction fan that the present embodiment uses is arranged at the front end of flour mill, as shown in Figure 2, auxiliary flue gas is sequentially sent to flour mill and grader after sending into high-pressure suction fan along auxiliary flue 2 again, in the present embodiment, high-pressure suction fan is positive pressure operation, it is avoided that the sorbent particle abrasion to blower fan after pulverizing, reduces the wear-resisting requirement of crushing blower.In actual application, absorbent is fed directly to flour mill, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, a part of absorbent mixes composition primary mixture with air-flow, delivers to gas mixer under the power that high-pressure suction fan provides, and another part absorbent returns again to flour mill and proceeds to pulverize.In the present embodiment, the operation pressure of high-pressure suction fan is 10kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 5kpa, another part is then the pressure overcoming gas mixer, about 5 kpa, it may be assumed that the pressure of the primary mixture delivering to gas mixer is 5 kpa.
Embodiment 8:
The present embodiment is with the difference of embodiment 6: the grader that the present embodiment uses is arranged at the front end of high-pressure suction fan, as shown in Figure 3, auxiliary flue gas is sequentially sent to flour mill, grader and high-pressure suction fan along auxiliary flue 2, in the present embodiment, high-pressure suction fan uses negative-pressure operation, it is avoided that pulverizer and grader occur that dust is revealed, but the Wear-resistant Treatment degree of high-pressure suction fan need to be improved.In actual application, absorbent and auxiliary flue gas are admitted to flour mill, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, a part of absorbent mixes composition primary mixture with air-flow, and delivers to gas mixer through high-pressure suction fan, and another part absorbent returns again to flour mill and proceeds to pulverize.In the present embodiment, the operation pressure of high-pressure suction fan is 13kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, it may be assumed that the pressure of the primary mixture delivering to gas mixer is 5 kpa.
In the present embodiment, for avoiding assisting pollutant in flue gas to the abrasion of high-pressure suction fan and corrosion, the flowing of high-pressure suction fan should use erosion resistant to process, has the beneficial effect in rub proofness and the raising high-pressure suction fan service life increasing high-pressure suction fan.
Embodiment 9:
The present embodiment is with the difference of embodiment 1: in the present embodiment, SO2nullAbsorption system includes the absorption tower 4 being provided with spraying layer 3 and doctor solution blood circulation，As described in Figure 4，Flue collector 1 is connected to the middle part on absorption tower 4，It is provided with at the top on absorption tower 4 for purifying the flue 5 that gas is discharged，The waste liquid comb 6 discharged for desulfurization slurry then it is provided with in the bottom on absorption tower 4，Its concrete operations flow process is as follows: the smoke mixture that primary mixture is formed after being admitted to flue collector 1 and flue gas hybrid reaction sends into absorption tower 4 by flue collector 1 again，Spraying layer 3 is arranged in absorption tower 4，Such as，Three layers of spraying layer 3 it are disposed with in absorption tower 4，After circulating pump 7 is pressurizeed by doctor solution blood circulation，By doctor solution by the nozzle plenum ejection of distribution on three layers of spraying layer 3，And form the desulfurization droplet that substantial amounts of specific surface area is bigger，On the one hand，Smoke mixture enters the middle part on absorption tower 4，Rapid decreasing temperature and increasing humidity in tower，And meet head on to contact with the desulfurization droplet of reverse high-speed motion，There is strong action of turbulent flow，Gas、Liquid is biphase carries out abundant mass-and heat-transfer，SO in smoke mixture2Absorbed in a large number；On the other hand, after absorbent granules in smoke mixture enters in tower, on equally with gas flow counterflow, sufficiently contact with top-down doctor solution, the absorbent granules of excess is dissolved in doctor solution, the SO remained in circulation continuation absorption flue gas in tower under the effect of doctor solution blood circulation with desulfurization slurry2、NOYAnd heavy metallic oxide, the spray mist cone of three layers of nozzle generation can reach more than 200% to the coverage rate in desulfurizing tower cross section, SO2Removal efficiency may be up to 98%, the purification gas after desulfurization can directly be discharged by flue 5 after reaching discharging standards, and desulfurization slurry is in cyclic process, owing to constantly absorbing SO2, as Na in desulfurization slurry2SO4Concentration reach 24～28% after, i.e. delivered to Sewage Disposal by waste liquid comb 6.In above process, doctor solution can be selected for sodium carbonate, sodium sulfate, the mixture of sodium nitrate composition.
Embodiment 10:
The present embodiment is applicable to pollutant load at 9000mg/Nm3In the range of the thick purification of former flue gas, former flue gas includes flue gas and the auxiliary flue gas that volume ratio is 19:1, and wherein, auxiliary flue gas sends into impact grinding pulverizing grading machine along auxiliary flue 2, and flue gas is then sent to gas mixer along flue collector 1.
Being disposed with flour mill, grader and high-pressure suction fan in auxiliary flue 2, auxiliary flue gas sends into the flour mill of auxiliary flue 2 along auxiliary flue 2 entrance；Absorbent is first fed into absorbent feed bin, then after absorbent conveyer device, deliver to absorbent metered dispensing unit, flour mill it is re-fed into after metering, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, regulation grader rotating speed is to 600r/min, after controlling to pulverize, the granularity of absorbent is 30～40um, the absorbent of absorbent granules degree ＞ 40um returns flour mill and proceeds to pulverize, meet the absorbent that granularity is 30～40um and then mix acquisition primary mixture with auxiliary flue gas；The purpose of high-pressure suction fan is to provide power for auxiliary flue gas, makes auxiliary flue gas that absorbent can be driven to send into grader from flour mill, and the primary mixture obtained also has certain pressure, the feeding gas mixer that energy is stable, reacts with flue gas.In the present embodiment, absorbent selects NaHCO3, its introduction volume is 460g/Nm with the maximum mixing ratio of auxiliary flue gas3, the pressure of high-pressure suction fan is set as 13kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, it may be assumed that the pressure of the primary mixture delivering to gas mixer is 5 kpa.
In the present embodiment, for avoiding pollutant in flue gas to the abrasion of high-pressure suction fan and corrosion, the flowing of high-pressure suction fan should use erosion resistant to process, and has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
Absorbent is after impact grinding pulverizing grading machine pretreatment, in auxiliary flue 2, the thick purifying rate of auxiliary flue gas be can reach 95%, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mixing with the flue gas in flue collector 1, the absorbent in primary mixture is 23g/Nm with the maximum mixing ratio of flue gas3, after being adequately mixed reaction, the purifying rate of flue gas can reach 85%, it is not necessary to carries out gas powder separation, directly delivers to SO by flue collector 12Absorption system.
In the present embodiment, SO2nullAbsorption system includes the absorption tower 4 being provided with spraying layer 3 and doctor solution blood circulation，As described in Figure 4，Flue collector 1 is connected to the middle part on absorption tower 4，It is provided with at the top on absorption tower 4 for purifying the flue 5 that gas is discharged，The waste liquid comb 6 discharged for desulfurization slurry then it is provided with in the bottom on absorption tower 4，Its concrete operations flow process is as follows: the smoke mixture that primary mixture is formed after being admitted to flue collector 1 and flue gas hybrid reaction sends into absorption tower 4 by flue collector 1 again，Spraying layer 3 is arranged in absorption tower 4，Such as，Three layers of spraying layer 3 it are disposed with in absorption tower 4，After circulating pump 7 is pressurizeed by doctor solution blood circulation，By doctor solution by the nozzle plenum ejection of distribution on three layers of spraying layer 3，And form the desulfurization droplet that substantial amounts of specific surface area is bigger，On the one hand，Smoke mixture enters the middle part on absorption tower 4，Rapid decreasing temperature and increasing humidity in tower，And meet head on to contact with the desulfurization droplet of reverse high-speed motion，There is strong action of turbulent flow，Gas、Liquid is biphase carries out abundant mass-and heat-transfer，SO in smoke mixture2Absorbed in a large number；On the other hand, after absorbent granules in smoke mixture enters in tower, on equally with gas flow counterflow, sufficiently contact with top-down doctor solution, the absorbent granules of excess is dissolved in doctor solution, the SO remained in circulation continuation absorption flue gas in tower under the effect of doctor solution blood circulation with desulfurization slurry2、NOYAnd heavy metallic oxide, the spray mist cone of three layers of nozzle generation can reach more than 200% to the coverage rate in desulfurizing tower cross section, SO2Removal efficiency may be up to 98%, the purification gas after desulfurization can directly be discharged by flue 5 after reaching discharging standards, and desulfurization slurry is in cyclic process, owing to constantly absorbing SO2, as Na in desulfurization slurry2SO4Concentration reach 24% after, i.e. delivered to Sewage Disposal by waste liquid comb 6.In above process, doctor solution can be selected for sodium carbonate, the mixture of sodium sulfate composition.
Embodiment 11:
The present embodiment is applicable to pollutant load at 6000mg/Nm3In the range of the thick purification of former flue gas, former flue gas includes flue gas and the auxiliary flue gas that volume ratio is 14:1, and wherein, auxiliary flue gas sends into impact grinding pulverizing grading machine along auxiliary flue 2, and flue gas is then sent to gas mixer along flue collector 1.
Being disposed with high-pressure suction fan, flour mill and grader in auxiliary flue 2, auxiliary flue gas is sequentially sent to the high-pressure suction fan in auxiliary flue 2 and flour mill along auxiliary flue 2 entrance；Absorbent is first fed into absorbent feed bin, then after absorbent conveyer device, deliver to absorbent metered dispensing unit, flour mill it is re-fed into after metering, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, regulation grader rotating speed is to 800r/min, after controlling to pulverize, the granularity of absorbent is 20～40um, the absorbent of absorbent granules degree ＞ 40um returns flour mill and proceeds to pulverize, meet the absorbent that granularity is 20～40um and then mix acquisition primary mixture with auxiliary flue gas；The purpose of high-pressure suction fan is to provide power for auxiliary flue gas, makes auxiliary flue gas that absorbent can be driven to send into grader from flour mill, and the primary mixture obtained also has certain pressure, the feeding gas mixer that energy is stable, reacts with flue gas.In the present embodiment, absorbent selects Na2CO3, its introduction volume is 225g/Nm with the maximum mixing ratio of auxiliary flue gas3, the pressure of high-pressure suction fan is set as 12kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 5～8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, it may be assumed that the pressure of the primary mixture delivering to gas mixer is 5 kpa.
Absorbent is after impact grinding pulverizing grading machine pretreatment, in auxiliary flue 2, the thick purifying rate of auxiliary flue gas be can reach 95%, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mixing with the flue gas in flue collector 1, the absorbent in primary mixture is 15g/Nm with the maximum mixing ratio of flue gas3, after being adequately mixed reaction, the purifying rate of flue gas can reach 90%, it is not necessary to carries out gas powder separation, directly delivers to SO by flue collector 12Absorption system.
In the present embodiment, SO2nullAbsorption system includes the absorption tower 4 being provided with spraying layer 3 and doctor solution blood circulation，As described in Figure 4，Flue collector 1 is connected to the middle part on absorption tower 4，It is provided with at the top on absorption tower 4 for purifying the flue 5 that gas is discharged，The waste liquid comb 6 discharged for desulfurization slurry then it is provided with in the bottom on absorption tower 4，Its concrete operations flow process is as follows: the smoke mixture that primary mixture is formed after being admitted to flue collector 1 and flue gas hybrid reaction sends into absorption tower 4 by flue collector 1 again，Spraying layer 3 is arranged in absorption tower 4，Such as，Three layers of spraying layer 3 it are disposed with in absorption tower 4，After circulating pump 7 is pressurizeed by doctor solution blood circulation，By doctor solution by the nozzle plenum ejection of distribution on three layers of spraying layer 3，And form the desulfurization droplet that substantial amounts of specific surface area is bigger，On the one hand，Smoke mixture enters the middle part on absorption tower 4，Rapid decreasing temperature and increasing humidity in tower，And meet head on to contact with the desulfurization droplet of reverse high-speed motion，There is strong action of turbulent flow，Gas、Liquid is biphase carries out abundant mass-and heat-transfer，SO in smoke mixture2Absorbed in a large number；On the other hand, after absorbent granules in smoke mixture enters in tower, on equally with gas flow counterflow, sufficiently contact with top-down doctor solution, the absorbent granules of excess is dissolved in doctor solution, the SO remained in circulation continuation absorption flue gas in tower under the effect of doctor solution blood circulation with desulfurization slurry2、NOYAnd heavy metallic oxide, the spray mist cone of three layers of nozzle generation can reach more than 200% to the coverage rate in desulfurizing tower cross section, SO2Removal efficiency may be up to 98%, the purification gas after desulfurization can directly be discharged by flue 5 after reaching discharging standards, and desulfurization slurry is in cyclic process, owing to constantly absorbing SO2, as Na in desulfurization slurry2SO4Concentration reach 28% after, i.e. delivered to Sewage Disposal by waste liquid comb 6.In above process, doctor solution can be selected for the mixture of sodium carbonate composition.
Embodiment 12:
The present embodiment is with the difference of embodiment 9: the present embodiment is applicable to pollutant load at 4000mg/Nm3In the range of the thick purification of former flue gas, former flue gas includes flue gas and the auxiliary flue gas that volume ratio is 12:1, and wherein, auxiliary flue gas sends into impact grinding pulverizing grading machine along auxiliary flue 2, and flue gas is then sent to gas mixer along flue collector 1.
Being disposed with flour mill, grader and high-pressure suction fan in auxiliary flue 2, auxiliary flue gas sends into the flour mill of auxiliary flue 2 along auxiliary flue 2 entrance；Absorbent is first fed into absorbent feed bin, then after absorbent conveyer device, deliver to absorbent metered dispensing unit, flour mill it is re-fed into after metering, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, regulation grader rotating speed is to 1000r/min, after controlling to pulverize, the granularity of absorbent is 10～40um, the absorbent of absorbent granules degree ＞ 40um returns flour mill and proceeds to pulverize, meet the absorbent that granularity is 10～40um and then mix acquisition primary mixture with auxiliary flue gas；The purpose of high-pressure suction fan is to provide power for auxiliary flue gas, makes auxiliary flue gas that absorbent can be driven to send into grader from flour mill, and the primary mixture obtained also has certain pressure, the feeding gas mixer that energy is stable, reacts with flue gas.In the present embodiment, absorbent selects mass ratio to be NaHCO3: Mg (HCO3)2The mixture of=1:0.1 composition, its introduction volume is 143g/Nm with the maximum mixing ratio of auxiliary flue gas3, the pressure of high-pressure suction fan is set as 12kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 7kpa, another part is the pressure overcoming gas mixer, about 5 kpa, it may be assumed that the pressure of the primary mixture delivering to gas mixer is 5 kpa.
Absorbent is after impact grinding pulverizing grading machine pretreatment, in auxiliary flue 2, the thick purifying rate of auxiliary flue gas be can reach 92%, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mixing with the flue gas in flue collector 1, the absorbent in primary mixture is 11g/Nm with the maximum mixing ratio of flue gas3, after being adequately mixed reaction, the purifying rate of flue gas can reach 80%, it is not necessary to carries out gas powder separation, directly delivers to SO by flue collector 12Absorption system.
In the present embodiment, for avoiding pollutant in flue gas to the abrasion of high-pressure suction fan and corrosion, the flowing of high-pressure suction fan should use erosion resistant to process, and has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
Embodiment 13:
The present embodiment is with the difference of embodiment 9: the present embodiment is applicable to pollutant load at 8000mg/Nm3In the range of the thick purification of former flue gas, former flue gas includes flue gas and the auxiliary flue gas that volume ratio is 18:1, and wherein, auxiliary flue gas sends into impact grinding pulverizing grading machine along auxiliary flue 2, and flue gas is then sent to gas mixer along flue collector 1.
Being disposed with high-pressure suction fan, flour mill and grader in auxiliary flue 2, auxiliary flue gas is sequentially sent to the high-pressure suction fan in auxiliary flue 2 and flour mill along auxiliary flue 2 entrance；Absorbent is first fed into absorbent feed bin, then after absorbent conveyer device, deliver to absorbent metered dispensing unit, flour mill it is re-fed into after metering, absorbent spatial dispersion in flour mill and turbulence, and be broken by the synergism of flour mill and auxiliary flue gas, the absorbent being broken is delivered to grader under the drive of auxiliary flue gas and is screened, regulation grader rotating speed is to 1000r/min, after controlling to pulverize, the granularity of absorbent is 10～40um, the absorbent of absorbent granules degree ＞ 40um returns flour mill and proceeds to pulverize, meet the absorbent that granularity is 10～40um and then mix acquisition primary mixture with auxiliary flue gas；The purpose of high-pressure suction fan is to provide power for auxiliary flue gas, makes auxiliary flue gas that absorbent can be driven to send into grader from flour mill, and the primary mixture obtained also has certain pressure, the feeding gas mixer that energy is stable, reacts with flue gas.In the present embodiment, absorbent selects mass ratio to be Na2CO3: K2CO3The mixture of=1:0.05 composition, its introduction volume is 410g/Nm with the maximum mixing ratio of auxiliary flue gas3, the pressure of high-pressure suction fan is set as 13kpa, and this operation pressure part is to overcome the resistance of flour mill and grader, about 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, it may be assumed that the pressure of the primary mixture delivering to gas mixer is 5 kpa.
Absorbent is after impact grinding pulverizing grading machine pretreatment, in auxiliary flue 2, the thick purifying rate of auxiliary flue gas be can reach 94%, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mixing with the flue gas in flue collector 1, the absorbent in primary mixture is 2 1g/Nm with the maximum mixing ratio of flue gas3, after being adequately mixed reaction, the purifying rate of flue gas can reach 89%, it is not necessary to carries out gas powder separation, directly delivers to SO by flue collector 12Absorption system.
The above, be only presently preferred embodiments of the present invention, and the present invention not does any pro forma restriction, every above example is made according to the technical spirit of the present invention any simple modification, equivalent variations, within each falling within protection scope of the present invention.
Claims (11)
1. the flue gas purifying technique realized based on absorbent pretreatment, described flue gas purifying technique includes by flue gas system, the former flue gas in main chimney flue is sent into SO2Absorption system, it is characterized in that: described flue gas system mainly auxiliary flue (2) and flue collector (1) by being interconnected forms, it is provided with impact grinding pulverizing grading machine in auxiliary flue (2), former flue gas includes the auxiliary flue gas by auxiliary flue (2) and the flue gas by flue collector (1), absorbent sends into impact grinding pulverizing grading machine with auxiliary flue gas, after the primary mixture obtained enters flue collector (1) and flue gas hybrid reaction, deliver to SO in the lump2Absorption system, described flue gas is (9～19) with the volume ratio of auxiliary flue gas: 1.
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 1, it is characterized in that: described impact grinding pulverizing grading machine includes flour mill, grader and high-pressure suction fan, described absorbent and auxiliary flue gas send into flour mill with high-pressure suction fan, send into grader with auxiliary flue gas again after absorbent is crushed to screen, the absorbent of granularity≤40um mixes acquisition primary mixture with air-flow, and the absorbent of granularity ＞ 40um returns again to flour mill and proceeds to pulverize.
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 2, it is characterised in that: described absorbent sends into flour mill after metering, and described absorbent is 100～460g/Nm with the mixing ratio of auxiliary flue gas3。
4. according to the flue gas purifying technique realized based on absorbent pretreatment described in any one of claims 1 to 3, it is characterised in that: described absorbent includes NaHCO3、KHCO3、Mg(HCO3)2In one or more composition mixture.
5. according to the flue gas purifying technique realized based on absorbent pretreatment described in any one of claims 1 to 3, it is characterised in that: described absorbent includes Na2CO3、K2CO3、CaCO3、MgCO3In one or more composition mixture.
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 2, it is characterized in that: on described flue collector (1), gas mixer is set, described primary mixture and flue gas hybrid reaction in gas mixer, the absorbent in described primary mixture is 6～23g/Nm with the mixing ratio of flue gas3。
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 2, it is characterized in that: described high-pressure suction fan is arranged at the front end of flour mill, described auxiliary flue gas is sequentially sent to flour mill and grader after sending into high-pressure suction fan along auxiliary flue (2) again.
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 7, it is characterised in that: described high-pressure suction fan is positive pressure operation, and its operation pressure is 10～13kpa.
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 2, it is characterized in that: described grader is arranged at the front end of high-pressure suction fan, described auxiliary flue gas is sequentially sent to flour mill, grader and high-pressure suction fan along auxiliary flue (2).
The flue gas purifying technique realized based on absorbent pretreatment the most according to claim 9, it is characterised in that: described high-pressure suction fan is negative-pressure operation, and its operation pressure is 10～13kpa.
11. according to the flue gas purifying technique realized based on absorbent pretreatment described in any one of claims 1 to 3,6～10, it is characterised in that: described SO2Absorption system includes the absorption tower (4) being provided with spraying layer (3) and doctor solution blood circulation, described flue collector (1) is connected with absorption tower (4), it is provided with at the top of absorption tower (4) for purifying the flue (5) that gas is discharged, is then provided with, in the bottom of absorption tower (4), the waste liquid comb (6) discharged for desulfurization slurry.
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| CN105056750A (en) * | 2015-08-10 | 2015-11-18 | 成都华西堂投资有限公司 | Dry flue gas desulphurization, denitrification and dust-removal integrated purification system |
| CN105771578A (en) * | 2016-04-03 | 2016-07-20 | 西南科技大学 | Integration technology for raw material processing and smoke desulfurizing |
| CN108114591B (en) * | 2017-12-28 | 2020-08-21 | 山东义丰环保机械股份有限公司 | Low-temperature flue gas treatment method |
| CN108392976A (en) * | 2018-05-21 | 2018-08-14 | 宁波市北仑环保固废处置有限公司 | A kind of sodium bicarbonate automation deacidification system and its process |
| CN115105935A (en) * | 2022-07-13 | 2022-09-27 | 中冶京诚工程技术有限公司 | Flue gas desulfurization and denitrification system and method for blast furnace hot blast stove |
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