CN104353350A - Smoke purification technology implemented based on adsorbent pretreatment - Google Patents
Smoke purification technology implemented based on adsorbent pretreatment Download PDFInfo
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- CN104353350A CN104353350A CN201410716386.6A CN201410716386A CN104353350A CN 104353350 A CN104353350 A CN 104353350A CN 201410716386 A CN201410716386 A CN 201410716386A CN 104353350 A CN104353350 A CN 104353350A
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Abstract
The invention discloses a smoke purification technology implemented based on adsorbent pretreatment. According to the smoke purification technology, raw smoke in a main flue is conveyed into a SO2 absorption system through a smoke system; the smoke system mainly comprises an auxiliary flue and the main flue which are communicated with each other; an impact pulverizing grading machine is arranged in the auxiliary flue; the raw smoke comprises auxiliary smoke passing through the auxiliary flue and flue gas passing through the main flue; an absorbent is conveyed into the impact pulverizing grading machine along with the auxiliary smoke, and an obtained gas-powder mixture enters the main flue and is subjected to mixing reaction with the flue gas; the obtained mixture is conveyed to the SO2 absorption system. The smoke purification technology is designed specially for rough purification of the flue gas, so that the desulfuration and denitration efficiency of the absorbent is greatly improved; the smoke purification technology has an extremely effect for promoting the treatment efficiency of a subsequent desulfuration and denitration technology.
Description
Technical field
The present invention is the flue gas purifying technique realized based on absorbent pretreatment, is specifically related to use desulfurizing and denitrifying process to realize in the process of stack gas cleaning, to the technical finesse that absorbent carries out, belonging to stack gas cleaning field.
Background technology
The continuous 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 cause common concern and the attention of countries in the world, especially the discharge etc. of coal-fired power plant, coal-burning boiler and flue gas of refuse burning, quite serious to the pollution of air, we know, containing a large amount of flue dust, carbon dioxide, SO in coal-fired flue-gas
2and NO
xetc. harmful substance, wherein, the carbon dioxide of fuel combustion discharge is the main matter causing greenhouse effects; SO
2, NO
xand fly ash granule is again the main source of atmosphere pollution; Certainly, the flue dust that the flue gases such as coal-burning boiler produce also is the one of the main reasons causing atmosphere pollution, and its main component is also SO
2and NO
x.It is reported, China about has the city suspended particulates level of 70% to exceed standard, the SO in the peri-urban air of 2/3
2exceed standard, therefore, for improving the air quality of current environment, the improvement of these pollutants is very urgent especially with reduction of discharging.
In China, flue gas desulfurization and denitrification is topmost measure in air contaminant treatment, domestic and international flue gas desulfurization technique is a lot, as limestone-gypsum method, ammonia process, Dual alkali, rotary spraying technique etc., wherein from the desulfur technology of industrialization, though have that floor space is large, operating cost is high, easy blocking, desulfurizing byproduct difficulty put, secondary pollution problems and and be unwell to China's national situation, due to history, what account for absolute leading position is still limestone-gypsum method.And in gas denitrifying technology, then 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 methods etc. are wherein general with SCR method denitration application again.
At present, in the world Application comparison widely flue gas desulfurization and denitrification technology be then utilize above-mentioned traditional flue gas desulfurization technique and SCR denitration technology combined, can the object of desulphurization denitration to reach, although this technology can remove the SO of more than 90%
2with more than 80% NOx, but this method in fact remains combinationally using of independent desulphurization and denitration technology, more have the disadvantage that above-mentioned desulphurization and denitration technology exists concurrently, failed to break away from technological process length, investment is large, operating cost is high, Technical Economy is poor, easily cause secondary pollution problems.From existing patent document 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) we know, combined desulfurization and denitration technology becomes the developing direction of smoke gas treatment gradually, but the integrated technique of this kind of fume desulfuring and denitrifying is often ripe not enough, for improving the treatment effeciency of follow-up desulfurizing and denitrifying process, usually adopt pretreatment flue to the SO in flue gas in desulfurization process front end
2or NO
xslightly purify, the mode used comprises ozone injection, cooling, absorbent etc., and for example patent document CN102363095A(flue gas dry desulfurizing process and flue gas dry desulfurizing system thereof, 2012.02.29), CN103990375A(semidry method sinter fume integrated purifying method, 2014.08.20) etc., in actual use, its treatment effeciency from the embodiment the technical process of whole desulfurization (denitration) but and not obvious, therefore, their industrial applications also and not obvious.
Summary of the invention
The object of the present invention is to provide the flue gas purifying technique realized based on absorbent pretreatment, this flue gas purifying technique specially for flue gas thick process for purifying and design, the flue gas system adopted is primarily of the auxiliary flue be interconnected and flue collector composition, absorbent can be introduced impact grinding pulverizing grading machine by auxiliary flue gas, pretreatment is being carried out to absorbent and while obtaining primary mixture, absorbent is utilized to carry out desulphurization denitration process to auxiliary flue gas, absorbent in primary mixture has activity because of reaction, mix with flue gas again after being admitted to flue collector and react, improve the denitrification efficiency of absorbent greatly, to the treatment effeciency improving follow-up desulfurizing and denitrifying process, there is 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 comprises sends into SO by the former flue gas in main chimney flue by flue gas system
2absorption system, in traditional flue gas purification system, absorbent is normally ground into absorbent granules by grinding machine system after metering, and then carry out mixing and reacting with former flue gas by dry powder injector feeding flue collector, the denitrification efficiency of absorbent to former flue gas is lower, for improving the operating efficiency of absorbent, the present invention improves flue gas system, in the present invention, described flue gas system is primarily of the auxiliary flue be interconnected and flue collector composition, impact grinding pulverizing grading machine is provided with in auxiliary flue, former flue gas comprises by the auxiliary flue gas of auxiliary flue and the flue gas by 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 lump
2absorption 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 has activity because of reaction, when being sent to flue collector and flue gas hybrid reaction, its denitrification efficiency is also higher, 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, the former flue gas of a part enters auxiliary flue through auxiliary flue entrance end, be called auxiliary flue gas, the former flue gas of another part continues to stay flue collector, be called flue gas, auxiliary flue gas drives absorbent to enter impact grinding pulverizing grading machine in the lump, absorbent in impact grinding pulverizing grading machine, carry out 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 lump
2absorption system, in actual application, the volume ratio of described flue gas and auxiliary flue gas is (9 ~ 19): 1.
For the thick step of the pretreatment and auxiliary flue gas that better realize absorbent purifies, the present invention improves traditional grinding machine system, adopt impact grinding pulverizing grading machine, described impact grinding pulverizing grading machine comprises flour mill, grader and high-pressure suction fan, described absorbent and auxiliary flue gas send into flour mill with high-pressure suction fan, absorbent is sent into grader with auxiliary flue gas again after being pulverized and is screened, the absorbent of granularity≤40um mixes with air-flow and obtains primary mixture, the absorbent of granularity > 40um returns flour mill again and proceeds to pulverize, when practical operation, first auxiliary flue gas and absorbent are admitted to flour mill and carry out pretreatment (pulverizing), react with auxiliary flue gas while that absorbent being pulverized, due to the effect of high-pressure suction fan, pretreated absorbent is sent into again grader in the lump and is screened under the drive of auxiliary flue gas, the reference area of the absorbent that pretreatment makes and porosity greatly increase, the desulfuration efficiency that improve absorbent of high degree.
In the present invention, after first absorbent sends into absorbent feed bin, deliver to after absorbent metered dispensing unit through absorbent conveying device again and deliver to flour mill, absorbent described in realization sends into flour mill after metering, and when practical application, absorbent is usually excessive, simultaneously, also will measure according to the content of pollutant in former flue gas, for former flue gas, its pollutant load is usually at 200 ~ 9000mg/Nm
3scope in, the mixing ratio of described absorbent and auxiliary flue gas is 100 ~ 460g/Nm
3, send into flour mill after metering.
Further, described absorbent comprises NaHCO
3, KHCO
3, Mg (HCO
3)
2in one or more composition mixtures.
Another kind of situation, described absorbent comprises Na
2cO
3, K
2cO
3, CaCO
3, MgCO
3in one or more composition mixtures.
For the abundant mixing that improves primary mixture and flue gas with contact, 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 and the mixing ratio of flue gas are 6 ~ 23g/Nm
3.
In actual production process, high-pressure suction fan can adopt the following two kinds mode to arrange:
One is, described high-pressure suction fan is arranged at the front end of flour mill, described auxiliary flue gas sends into flour mill and grader successively again after high-pressure suction fan sent into by auxiliary flue, absorbent then directly delivers to flour mill, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, part absorbent mixes with auxiliary flue gas and forms primary mixture, gas mixer is delivered under the power that high-pressure suction fan provides, another part absorbent returns flour mill again and proceeds to pulverize.
From above-mentioned situation, described high-pressure suction fan is positive pressure operation, and its operating pressure is 10 ~ 13kpa, this operating pressure part for overcoming the resistance of flour mill and grader, about 5 ~ 8kpa, another part then for overcoming the pressure of 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 sends into flour mill successively along auxiliary flue, grader and high-pressure suction fan, absorbent and auxiliary flue gas are admitted to flour mill, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, part absorbent mixes with flue gas and forms primary mixture, and deliver to gas mixer through high-pressure suction fan, another part absorbent returns flour mill again and proceeds to pulverize.
From above-mentioned situation, described high-pressure suction fan is negative-pressure operation, and its operating pressure is 10 ~ 13kpa, a pressure part for high-pressure suction fan is for overcoming 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 delivering to the primary mixture of gas mixer is 5 kpa.
In the present invention, described SO
2absorption system comprises the absorption tower being provided with spraying layer and the doctor solution circulatory system, described flue collector is connected with absorption tower, the flue of discharging for purified gas is provided with at the top on absorption tower, the waste liquid comb of discharging for desulfurization slurry is then 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, the doctor solution circulatory system is to after circulating pump pressurization, doctor solution is sprayed by the nozzle plenum that spraying layer distributes, and form the larger desulfurization droplet of a large amount of specific areas, 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 two-phase carries out abundant mass-and heat-transfer, SO in smoke mixture
2absorbed in a large number, on the other hand, absorbent granules in smoke mixture enters after in tower, on equally with gas flow counterflow, contact fully with top-down doctor solution, excessive absorbent granules is dissolved in doctor solution, continues to absorb SO residual in flue gas under the effect of the doctor solution circulatory system with desulfurization slurry at tower Inner eycle
2, NO
yand heavy metallic oxide, SO
2removal efficiency up to 98%, can directly can be discharged by flue after the purified gas after desulfurization reaches discharging standards, desulfurization slurry in cyclic process, owing to constantly absorbing SO
2, after reaching finite concentration, namely deliver to Sewage Disposal by waste liquid comb.
The present invention compared with prior art, has the following advantages and beneficial effect:
(1) the present invention specially for flue gas thick process for purifying and design, by auxiliary flue gas, absorbent is introduced impact grinding pulverizing grading machine, pretreatment is being carried out to absorbent and while obtaining primary mixture, absorbent is utilized to carry out desulphurization denitration process to auxiliary flue gas, absorbent in primary mixture has activity because of reaction, mix with flue gas again after being admitted to flue collector and react, improve the denitrification efficiency of absorbent greatly, to the treatment effeciency improving follow-up desulfurizing and denitrifying process, there is high facilitation.
(2) the 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, enter the air-flow of impact grinding pulverizing grading machine for auxiliary flue gas, avoid the concentration and the EGT that adopt other gas to reduce pollutant in waste gas, simultaneously, owing to introducing air-flow for auxiliary flue gas, carrying out pretreated to absorbent while, auxiliary flue gas can also react with absorbent, and make absorbent with activity, be conducive to the denitrification efficiency improving 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 into impact grinding pulverizing grading machine with high-pressure suction fan and carry out fragmentation, the spatial dispersion of absorbent between grader and flour mill and turbulence, and it is broken by the synergy of impact grinding pulverizing grading machine and auxiliary flue gas, crushing efficiency is high, the specific surface area and porosity of the absorbent obtained through pretreatment greatly increases, and in actual use, absorbent is crushed to grain graininess≤40um, pore volume is 0. 0317 m
3/ g, specific area 4.2m
2the particulate of/g.
(4) the auxiliary flue gas that the present invention adopts comes from former flue gas, when reality uses, because the temperature of former flue gas is higher, absorbent is while fragmentation, can react by more effective and auxiliary flue gas, improve the treatment effeciency of absorbent, when reality uses, the temperature entering the auxiliary flue gas of 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 forms primarily of flour mill, grader and high-pressure suction fan, with traditional grinding machine system unlike, the impact grinding pulverizing grading machine that the present invention adopts eliminates traditional whirlwind and the setting of bag collector, avoid the absorbent after pulverizing to reunite, maintain the activity of pretreatment absorbent fully, practicality is extremely strong.
(6) flexible operation of the present invention, the impact grinding pulverizing grading machine related to comprises two kinds and implements operating mode, and one is that high-pressure suction fan adopts positive pressure operation, can avoid pulverizing the wearing and tearing of rear absorbent granules to blower fan, reduce the wear-resisting requirement of equipment; Another kind is that high-pressure suction fan adopts negative-pressure operation, flour mill and grader can be avoided to occur that dust is revealed, but need improve the Wear-resistant Treatment degree of high-pressure suction fan.
(7) time for reducing high-pressure suction fan negative-pressure operation, absorbent granules is to the wearing and tearing of high-pressure suction fan, the runner of the high-pressure suction fan that the present invention relates to adopts erosion resistant process, has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
(8) the present invention is also provided with gas mixer on flue collector, this gas mixer can make full and uniform the mixing of the primary mixture of feeding flue collector and flue gas, be conducive to the thick purification of absorbent to flue gas, in flue collector, the primary mixture introduced and the first purifying rate of flue gas can reach 80 ~ 90%, and denitrification efficiency is high.
(9) the present invention is in the rough purification process of raising flue while denitrification efficiency, also reduces follow-up SO
2the purification pressure of absorption system, in actual mechanical process, absorption tower is to SO in smoke mixture
2removal efficiency can up to 98%, the desulfurization slurry of the generation in sweetening process is then disposed to Sewage Disposal and processes.
Accompanying drawing explanation
Fig. 1 is the control schematic diagram of illustrated structure.
Structural plan when Fig. 2 is high-pressure suction fan of the present invention employing positive pressure operation.
Structural plan when Fig. 3 is 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 flue, 3-spraying layer, 4-absorption tower, 5-flue, 6-waste liquid comb, 7-circulating pump.
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 thereto.
Embodiment 1:
In traditional flue gas purifying method, the thick process for purifying of absorbent to former flue gas generally includes: measure absorbent, then send into grinding machine system to pulverize, absorbent granules after pulverizing is sent into flue collector 1 by dry powder injector again and is carried out mixing and reacting with former flue gas, in the process, the purification efficiency of absorbent to former flue gas is generally about 50%, desulfuration efficiency is lower, therefore, for improving the operating efficiency of absorbent, the present invention proposes the flue gas purifying technique realized based on absorbent pretreatment, this flue gas purifying technique comprises sends into SO by the former flue gas in main chimney flue by flue gas system
2absorption system, for overcoming above-mentioned defect, the present invention improves flue gas system, in the present invention, flue gas system forms primarily of the auxiliary flue 2 be interconnected and flue collector 1, meanwhile, in auxiliary flue 2, be also provided with impact grinding pulverizing grading machine, its technological process is as follows: the former flue gas coming from main chimney flue delivers to SO along flue collector 1
2in the process of absorption system, former flue gas is shunted forms 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 (pulverizings), after the primary mixture of acquisition enters flue collector 1 and flue gas hybrid reaction, delivers to SO in the lump
2absorption 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 has activity because of reaction, when being sent to flue collector 1 with flue gas hybrid reaction, its denitrification efficiency is also higher, be proven, the thick purifying rate of absorbent to auxiliary flue gas can reach 90 ~ 99%, after primary mixture is sent to flue collector 1, can 80 ~ 90% be reached to the thick purifying rate of the flue gas in flue collector 1, simultaneously, follow-up SO can also be effectively reduced
2the purification pressure of absorption system, it is very reasonable to design.
Embodiment 2:
The difference of the present embodiment and embodiment 1 is: in the present embodiment, and after former flue gas is shunted, the auxiliary flue gas respectively by auxiliary flue 2 and the volume ratio by the flue gas of flue collector 1 are 9:1.
In the actual application of the present embodiment, former flue gas sends into flue collector 1 through flue gas booster fan, the former flue gas of a part enters auxiliary flue 2 through auxiliary flue 2 arrival end, be called auxiliary flue gas, the former flue gas of another part continues to stay flue collector 1, be called flue gas, auxiliary flue gas drives absorbent to enter impact grinding pulverizing grading machine in the lump, absorbent in impact grinding pulverizing grading machine, carry out 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 lump
2absorption system.
Embodiment 3:
The difference of the present embodiment and embodiment 2 is: in the present embodiment, impact grinding pulverizing grading machine is primarily of flour mill, grader and high-pressure suction fan composition, absorbent and auxiliary flue gas send into flour mill with high-pressure suction fan, absorbent is sent into grader with auxiliary flue gas again after being pulverized and is screened, in actual mechanical process, regulate the rotating speed of grader can select primary mixture, in primary mixture, the granularity of absorbent is controlled in 10 ~ 40um under normal circumstances, that is: the absorbent of granularity≤40um mixes with auxiliary flue gas and obtains primary mixture, the absorbent of granularity > 40um returns flour mill again and proceeds to pulverize.
Because the introduction volume of absorbent is relevant to the pollutant load in former flue gas, therefore, when reality uses, also need to monitor the pollutant in former flue gas, after measure control being carried out to absorbent according to Monitoring Data, again absorbent is sent into flour mill, the present embodiment is applicable to pollutant load at 200mg/Nm
3scope in the thick purification of former flue gas, the absorbent of introducing and the mixing ratio of auxiliary flue gas are 100g/Nm
3, after the pretreatment of impact grinding pulverizing grading machine, the thick purifying rate of absorbent to auxiliary flue gas can reach 90%.
Embodiment 4:
The difference of the present embodiment and embodiment 3 is: in the present embodiment, and the absorbent of use comprises NaHCO
3, KHCO
3, Mg (HCO
3)
2the mixture of composition, NaHCO in this mixture
3, KHCO
3, Mg (HCO
3)
2mass ratio be 1:0.05:0.05, the desulphurization denitration being applicable to former flue gas slightly purifies, and its chemical reaction process comprises:
Desulfurization: 2HCO
3 -+ SO
2+ O
2sO
4 2-+ H
2o+2CO
2;
2HCO
3 —+ SO
3→ SO
4 2—+ 2 CO
2+ H
2O；
Denitration: 2HCO
3 -+ SO
2+ NO+O
2sO
4 2-+ NO
2+ H
2o+2CO
2;
2HCO
3 —+ 2NO
2+ ?O
2? 2NO
3 —+ H
2O + 2CO
2；
4SO
3+ 2NO
2? 4SO
4 2—+ N
2；
2NO + 2SO
2? 2SO
3+ N
2；
2HCO
3 —+ SO
3? SO
4 2—+ H
2O + 2CO
2。
Embodiment 5:
The difference of the present embodiment and embodiment 4 is: in the present embodiment, and the absorbent of use comprises Na
2cO
3, K
2cO
3, CaCO
3, MgCO
3the mixture of composition, Na in this mixture
2cO
3, K
2cO
3, CaCO
3, MgCO
3mass ratio be 1:0.05:0.1:0.05, the desulphurization denitration being applicable to former flue gas slightly purifies, and its chemical reaction process comprises:
Desulfurization: 2CO
3 -+ SO
2+ O
2sO
4 2-+ H
2o+2CO
2;
2CO
3 —+ SO
3→ SO
4 2—+ 2 CO
2+ H
2O；
Denitration: 2CO
3 -+ SO
2+ NO+O
2sO
4 2-+ NO
2+ H
2o+2CO
2;
2CO
3 —+ 2NO
2+ ?O
2? 2NO
3 —+ H
2O + 2CO
2；
4SO
3+ 2NO
2? 4SO
4 2—+ N
2；
2NO + 2SO
2? 2SO
3+ N
2；
2CO
3 —+ SO
3? SO
4 2—+ H
2O + 2CO
2。
Embodiment 6:
The difference of the present embodiment and embodiment 3 is: the present embodiment is provided with gas mixer on flue collector 1, primary mixture and flue gas is abundant hybrid reaction in gas mixer, for ensureing the denitrification efficiency of flue gas, in primary mixture, the mixing ratio of absorbent and flue gas should be 6g/Nm
3.In actual application, to the determination of the absorbent consumption that flour mill is introduced, not only need to detect the total amount of pollutant in former flue gas, also need to detect the total amount of pollutant in flue collector after gas mixer 1, both data common feedback just can complete to the metering control system of absorbent, its control flow as shown in Figure 1, former flue is arranged and is used 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 the total amount of pollutants discharge that need process according to former flue gas inspection signal, reset the absorbed dose of radiation needing to add, by absorbent addition Signal transmissions to absorbent metered dispensing unit, absorbent is delivered to flour mill.After cleaning flue is arranged flue gas inspection instrument after the purification of flue gas pollutant after thick purification, flow, pressure, temperature diagnosis, after the purification detected, smoke signal feeds back to control system together with the pulse measurement signal of absorbent metered dispensing unit, and control system to be revised absorbent setting value according to the signal fed back and formed a complete control system.
Embodiment 7:
The difference of the present embodiment and embodiment 6 is: the high-pressure suction fan that the present embodiment adopts is arranged at the front end of flour mill, as shown in Figure 2, auxiliary flue gas sends into flour mill and grader successively again after high-pressure suction fan sent into by auxiliary flue 2, in the present embodiment, high-pressure suction fan is positive pressure operation, can avoid pulverizing the wearing and tearing of rear sorbent particle to blower fan, reduce the wear-resisting requirement of crushing blower.In actual application, absorbent directly delivers to flour mill, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, part absorbent mixes with air-flow and forms primary mixture, under the power that high-pressure suction fan provides, deliver to gas mixer, and another part absorbent returns flour mill again and proceeds to pulverize.In the present embodiment, the operating pressure of high-pressure suction fan is 10kpa, and this operating pressure part is for overcoming the resistance of flour mill and grader, about 5kpa, another part is then for overcoming the pressure of gas mixer, and about 5 kpa, that is: the pressure delivering to the primary mixture of gas mixer is 5 kpa.
Embodiment 8:
The difference of the present embodiment and embodiment 6 is: the grader that the present embodiment adopts is arranged at the front end of high-pressure suction fan, as shown in Figure 3, auxiliary flue gas sends into flour mill, grader and high-pressure suction fan successively along auxiliary flue 2, in the present embodiment, high-pressure suction fan adopts negative-pressure operation, pulverizer and grader can be avoided to occur that dust is revealed, but the Wear-resistant Treatment degree of high-pressure suction fan need be improved.In actual application, absorbent and auxiliary flue gas are admitted to flour mill, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, part absorbent mixes with air-flow and forms primary mixture, and delivers to gas mixer through high-pressure suction fan, and another part absorbent returns flour mill again and proceeds to pulverize.In the present embodiment, the operating pressure of high-pressure suction fan is 13kpa, and this operating pressure part is for overcoming the resistance of flour mill and grader, about 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, that is: the pressure delivering to the primary mixture of gas mixer is 5 kpa.
In the present embodiment, for avoiding the pollutant in auxiliary flue gas to the abrasion and corrosion of high-pressure suction fan, the flowing of high-pressure suction fan should adopt erosion resistant process, has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
Embodiment 9:
The difference of the present embodiment and embodiment 1 is: in the present embodiment, SO
2absorption system comprises the absorption tower 4 being provided with spraying layer 3 and the doctor solution circulatory system, as described in Figure 4, flue collector 1 is connected to the middle part on absorption tower 4, the flue 5 of discharging for purified gas is provided with at the top on absorption tower 4, the waste liquid comb 6 of discharging for desulfurization slurry is then 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 are furnished with in absorption tower 4, after the doctor solution circulatory system is pressurizeed to circulating pump 7, the nozzle plenum of doctor solution by distribution on three layers of spraying layer 3 is sprayed, and form the larger desulfurization droplet of a large amount of specific areas, 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 two-phase carries out abundant mass-and heat-transfer, SO in smoke mixture
2absorbed in a large number, on the other hand, absorbent granules in smoke mixture enters after in tower, on equally with gas flow counterflow, contact fully with top-down doctor solution, excessive absorbent granules is dissolved in doctor solution, continues to absorb SO residual in flue gas under the effect of the doctor solution circulatory system with desulfurization slurry at tower Inner eycle
2, NO
yand heavy metallic oxide, the spray mist cone of three layers of nozzle generation can reach more than 200%, SO to the coverage rate in desulfurizing tower cross section
2removal efficiency up to 98%, can directly can be discharged by flue 5 after the purified gas after desulfurization reaches discharging standards, desulfurization slurry in cyclic process, owing to constantly absorbing SO
2, as Na in desulfurization slurry
2sO
4concentration reach 24 ~ 28% after, namely deliver to Sewage Disposal by waste liquid comb 6.In above process, doctor solution can select the mixture that sodium carbonate, sodium sulphate, sodium nitrate form.
Embodiment 10:
The present embodiment is applicable to pollutant load at 9000mg/Nm
3scope in the thick purification of former flue gas, former flue gas comprises the flue gas and 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.
In auxiliary flue 2, be disposed with flour mill, grader and high-pressure suction fan, auxiliary flue gas sends into the flour mill of auxiliary flue 2 along auxiliary flue 2 entrance, first absorbent sends into absorbent feed bin, then after absorbent conveying device, absorbent metered dispensing unit is delivered to, flour mill is sent into again after metering, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, regulate grader rotating speed to 600r/min, controlling the granularity of absorbent after pulverizing is 30 ~ 40um, the absorbent of absorbent granules degree > 40um returns flour mill and proceeds to pulverize, meeting granularity is that the absorbent of 30 ~ 40um then mixes with auxiliary flue gas and obtains primary mixture, the object of high-pressure suction fan is as auxiliary flue gas provides power, and make auxiliary flue gas that absorbent can be driven to send into grader from flour mill, the primary mixture obtained also has certain pressure, and feeding gas mixer that can be stable, reacts with flue gas.In the present embodiment, NaHCO selected by absorbent
3, the maximum mixing ratio of its introduction volume and auxiliary flue gas is 460g/Nm
3, the pressure setting of high-pressure suction fan is 13kpa, and this operating pressure part is for overcoming the resistance of flour mill and grader, about 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, that is: the pressure delivering to the primary mixture of gas mixer is 5 kpa.
In the present embodiment, for avoiding the pollutant in flue gas to the abrasion and corrosion of high-pressure suction fan, the flowing of high-pressure suction fan should adopt erosion resistant process, has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
Absorbent is after the pretreatment of impact grinding pulverizing grading machine, can 95% be reached to the thick purifying rate of auxiliary flue gas in auxiliary flue 2, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mix with the flue gas in flue collector 1, the maximum mixing ratio of the absorbent in primary mixture and flue gas is 23g/Nm
3, after abundant hybrid reaction, the purifying rate of flue gas can reach 85%, without the need to carrying out the separation of gas powder, directly delivers to SO by flue collector 1
2absorption system.
In the present embodiment, SO
2absorption system comprises the absorption tower 4 being provided with spraying layer 3 and the doctor solution circulatory system, as described in Figure 4, flue collector 1 is connected to the middle part on absorption tower 4, the flue 5 of discharging for purified gas is provided with at the top on absorption tower 4, the waste liquid comb 6 of discharging for desulfurization slurry is then 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 are furnished with in absorption tower 4, after the doctor solution circulatory system is pressurizeed to circulating pump 7, the nozzle plenum of doctor solution by distribution on three layers of spraying layer 3 is sprayed, and form the larger desulfurization droplet of a large amount of specific areas, 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 two-phase carries out abundant mass-and heat-transfer, SO in smoke mixture
2absorbed in a large number, on the other hand, absorbent granules in smoke mixture enters after in tower, on equally with gas flow counterflow, contact fully with top-down doctor solution, excessive absorbent granules is dissolved in doctor solution, continues to absorb SO residual in flue gas under the effect of the doctor solution circulatory system with desulfurization slurry at tower Inner eycle
2, NO
yand heavy metallic oxide, the spray mist cone of three layers of nozzle generation can reach more than 200%, SO to the coverage rate in desulfurizing tower cross section
2removal efficiency up to 98%, can directly can be discharged by flue 5 after the purified gas after desulfurization reaches discharging standards, desulfurization slurry in cyclic process, owing to constantly absorbing SO
2, as Na in desulfurization slurry
2sO
4concentration reach 24% after, namely deliver to Sewage Disposal by waste liquid comb 6.In above process, doctor solution can select the mixture that sodium carbonate, sodium sulphate form.
Embodiment 11:
The present embodiment is applicable to pollutant load at 6000mg/Nm
3scope in the thick purification of former flue gas, former flue gas comprises the flue gas and 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.
In auxiliary flue 2, be disposed with high-pressure suction fan, flour mill and grader, auxiliary flue gas sends into high-pressure suction fan in auxiliary flue 2 and flour mill successively along auxiliary flue 2 entrance, first absorbent sends into absorbent feed bin, then after absorbent conveying device, absorbent metered dispensing unit is delivered to, flour mill is sent into again after metering, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, regulate grader rotating speed to 800r/min, controlling the granularity of absorbent after pulverizing is 20 ~ 40um, the absorbent of absorbent granules degree > 40um returns flour mill and proceeds to pulverize, meeting granularity is that the absorbent of 20 ~ 40um then mixes with auxiliary flue gas and obtains primary mixture, the object of high-pressure suction fan is as auxiliary flue gas provides power, and make auxiliary flue gas that absorbent can be driven to send into grader from flour mill, the primary mixture obtained also has certain pressure, and feeding gas mixer that can be stable, reacts with flue gas.In the present embodiment, Na selected by absorbent
2cO
3, the maximum mixing ratio of its introduction volume and auxiliary flue gas is 225g/Nm
3, the pressure setting of high-pressure suction fan is 12kpa, and this operating pressure part is for overcoming the resistance of flour mill and grader, about 5 ~ 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, that is: the pressure delivering to the primary mixture of gas mixer is 5 kpa.
Absorbent is after the pretreatment of impact grinding pulverizing grading machine, can 95% be reached to the thick purifying rate of auxiliary flue gas in auxiliary flue 2, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mix with the flue gas in flue collector 1, the maximum mixing ratio of the absorbent in primary mixture and flue gas is 15g/Nm
3, after abundant hybrid reaction, the purifying rate of flue gas can reach 90%, without the need to carrying out the separation of gas powder, directly delivers to SO by flue collector 1
2absorption system.
In the present embodiment, SO
2absorption system comprises the absorption tower 4 being provided with spraying layer 3 and the doctor solution circulatory system, as described in Figure 4, flue collector 1 is connected to the middle part on absorption tower 4, the flue 5 of discharging for purified gas is provided with at the top on absorption tower 4, the waste liquid comb 6 of discharging for desulfurization slurry is then 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 are furnished with in absorption tower 4, after the doctor solution circulatory system is pressurizeed to circulating pump 7, the nozzle plenum of doctor solution by distribution on three layers of spraying layer 3 is sprayed, and form the larger desulfurization droplet of a large amount of specific areas, 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 two-phase carries out abundant mass-and heat-transfer, SO in smoke mixture
2absorbed in a large number, on the other hand, absorbent granules in smoke mixture enters after in tower, on equally with gas flow counterflow, contact fully with top-down doctor solution, excessive absorbent granules is dissolved in doctor solution, continues to absorb SO residual in flue gas under the effect of the doctor solution circulatory system with desulfurization slurry at tower Inner eycle
2, NO
yand heavy metallic oxide, the spray mist cone of three layers of nozzle generation can reach more than 200%, SO to the coverage rate in desulfurizing tower cross section
2removal efficiency up to 98%, can directly can be discharged by flue 5 after the purified gas after desulfurization reaches discharging standards, desulfurization slurry in cyclic process, owing to constantly absorbing SO
2, as Na in desulfurization slurry
2sO
4concentration reach 28% after, namely deliver to Sewage Disposal by waste liquid comb 6.In above process, doctor solution can select the mixture that sodium carbonate forms.
Embodiment 12:
The difference of the present embodiment and embodiment 9 is: the present embodiment is applicable to pollutant load at 4000mg/Nm
3scope in the thick purification of former flue gas, former flue gas comprises the flue gas and 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.
In auxiliary flue 2, be disposed with flour mill, grader and high-pressure suction fan, auxiliary flue gas sends into the flour mill of auxiliary flue 2 along auxiliary flue 2 entrance, first absorbent sends into absorbent feed bin, then after absorbent conveying device, absorbent metered dispensing unit is delivered to, flour mill is sent into again after metering, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, regulate grader rotating speed to 1000r/min, controlling the granularity of absorbent after pulverizing is 10 ~ 40um, the absorbent of absorbent granules degree > 40um returns flour mill and proceeds to pulverize, meeting granularity is that the absorbent of 10 ~ 40um then mixes with auxiliary flue gas and obtains primary mixture, the object of high-pressure suction fan is as auxiliary flue gas provides power, and make auxiliary flue gas that absorbent can be driven to send into grader from flour mill, the primary mixture obtained also has certain pressure, and feeding gas mixer that can be stable, reacts with flue gas.In the present embodiment, absorbent selects mass ratio to be NaHCO
3: Mg (HCO
3)
2the mixture of=1:0.1 composition, the maximum mixing ratio of its introduction volume and auxiliary flue gas is 143g/Nm
3, the pressure setting of high-pressure suction fan is 12kpa, and this operating pressure part is for overcoming the resistance of flour mill and grader, about 7kpa, another part is the pressure overcoming gas mixer, about 5 kpa, that is: the pressure delivering to the primary mixture of gas mixer is 5 kpa.
Absorbent is after the pretreatment of impact grinding pulverizing grading machine, can 92% be reached to the thick purifying rate of auxiliary flue gas in auxiliary flue 2, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mix with the flue gas in flue collector 1, the maximum mixing ratio of the absorbent in primary mixture and flue gas is 11g/Nm
3, after abundant hybrid reaction, the purifying rate of flue gas can reach 80%, without the need to carrying out the separation of gas powder, directly delivers to SO by flue collector 1
2absorption system.
In the present embodiment, for avoiding the pollutant in flue gas to the abrasion and corrosion of high-pressure suction fan, the flowing of high-pressure suction fan should adopt erosion resistant process, has the rub proofness increasing high-pressure suction fan and the beneficial effect improving high-pressure suction fan service life.
Embodiment 13:
The difference of the present embodiment and embodiment 9 is: the present embodiment is applicable to pollutant load at 8000mg/Nm
3scope in the thick purification of former flue gas, former flue gas comprises the flue gas and 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.
In auxiliary flue 2, be disposed with high-pressure suction fan, flour mill and grader, auxiliary flue gas sends into high-pressure suction fan in auxiliary flue 2 and flour mill successively along auxiliary flue 2 entrance, first absorbent sends into absorbent feed bin, then after absorbent conveying device, absorbent metered dispensing unit is delivered to, flour mill is sent into again after metering, the spatial dispersion of absorbent in flour mill and turbulence, and be broken by the synergy of flour mill and auxiliary flue gas, the absorbent be broken is delivered to grader and is screened under the drive of auxiliary flue gas, regulate grader rotating speed to 1000r/min, controlling the granularity of absorbent after pulverizing is 10 ~ 40um, the absorbent of absorbent granules degree > 40um returns flour mill and proceeds to pulverize, meeting granularity is that the absorbent of 10 ~ 40um then mixes with auxiliary flue gas and obtains primary mixture, the object of high-pressure suction fan is as auxiliary flue gas provides power, and make auxiliary flue gas that absorbent can be driven to send into grader from flour mill, the primary mixture obtained also has certain pressure, and feeding gas mixer that can be stable, reacts with flue gas.In the present embodiment, absorbent selects mass ratio to be Na
2cO
3: K
2cO
3the mixture of=1:0.05 composition, the maximum mixing ratio of its introduction volume and auxiliary flue gas is 410g/Nm
3, the pressure setting of high-pressure suction fan is 13kpa, and this operating pressure part is for overcoming the resistance of flour mill and grader, about 8kpa, another part is the pressure overcoming gas mixer, about 5 kpa, that is: the pressure delivering to the primary mixture of gas mixer is 5 kpa.
Absorbent is after the pretreatment of impact grinding pulverizing grading machine, can 94% be reached to the thick purifying rate of auxiliary flue gas in auxiliary flue 2, the primary mixture obtained is exported by auxiliary flue 2 and delivers to gas mixer with the pressure of 5 kpa, mix with the flue gas in flue collector 1, the maximum mixing ratio of the absorbent in primary mixture and flue gas is 2 1g/Nm
3, after abundant hybrid reaction, the purifying rate of flue gas can reach 89%, without the need to carrying out the separation of gas powder, directly delivers to SO by flue collector 1
2absorption system.
The above is only preferred embodiment of the present invention, and not do any pro forma restriction to the present invention, every any simple modification, equivalent variations done above embodiment according to technical spirit of the present invention, all falls within protection scope of the present invention.
Claims (12)
1., based on the flue gas purifying technique that absorbent pretreatment realizes, described flue gas purifying technique comprises sends into SO by the former flue gas in main chimney flue by flue gas system
2absorption system, it is characterized in that: described flue gas system is primarily of the auxiliary flue (2) be interconnected and flue collector (1) composition, impact grinding pulverizing grading machine is provided with in auxiliary flue (2), former flue gas comprises 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, the primary mixture obtained delivers to SO after entering flue collector (1) and flue gas hybrid reaction in the lump
2absorption system.
2. the flue gas purifying technique realized based on absorbent pretreatment according to claim 1, is characterized in that: the volume ratio of described flue gas and auxiliary flue gas is (9 ~ 19): 1.
3. the flue gas purifying technique realized based on absorbent pretreatment according to claim 2, it is characterized in that: described impact grinding pulverizing grading machine comprises flour mill, grader and high-pressure suction fan, described absorbent and auxiliary flue gas send into flour mill with high-pressure suction fan, absorbent is sent into grader with auxiliary flue gas again after being pulverized and is screened, the absorbent of granularity≤40um mixes with air-flow and obtains primary mixture, and the absorbent of granularity > 40um returns flour mill again and proceeds to pulverize.
4. the flue gas purifying technique realized based on absorbent pretreatment according to claim 3, it is characterized in that: described absorbent sends into flour mill after metering, the mixing ratio of described absorbent and auxiliary flue gas is 100 ~ 460g/Nm
3.
5. the flue gas purifying technique realized based on absorbent pretreatment according to any one of Claims 1 to 4, is characterized in that: described absorbent comprises NaHCO
3, KHCO
3, Mg (HCO
3)
2in one or more composition mixtures.
6. the flue gas purifying technique realized based on absorbent pretreatment according to any one of Claims 1 to 4, is characterized in that: described absorbent comprises Na
2cO
3, K
2cO
3, CaCO
3, MgCO
3in one or more composition mixtures.
7. the flue gas purifying technique realized based on absorbent pretreatment according to claim 3, 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 and the mixing ratio of flue gas are 6 ~ 23g/Nm
3.
8. the flue gas purifying technique realized based on absorbent pretreatment according to claim 3, it is characterized in that: described high-pressure suction fan is arranged at the front end of flour mill, described auxiliary flue gas sends into flour mill and grader successively again after high-pressure suction fan sent into by auxiliary flue (2).
9. the flue gas purifying technique realized based on absorbent pretreatment according to claim 8, it is characterized in that: described high-pressure suction fan is positive pressure operation, its operating pressure is 10 ~ 13kpa.
10. the flue gas purifying technique realized based on absorbent pretreatment according to claim 3, it is characterized in that: described grader is arranged at the front end of high-pressure suction fan, described auxiliary flue gas sends into flour mill, grader and high-pressure suction fan successively along auxiliary flue (2).
11. flue gas purifying techniques realized based on absorbent pretreatment according to claim 10, it is characterized in that: described high-pressure suction fan is negative-pressure operation, its operating pressure is 10 ~ 13kpa.
12. according to Claims 1 to 4,7 ~ 11 any one based on absorbent pretreatment realize flue gas purifying technique, it is characterized in that: described SO
2absorption system comprises the absorption tower (4) being provided with spraying layer (3) and the doctor solution circulatory system, described flue collector (1) is connected with absorption tower (4), be provided with the flue (5) of discharging for purified gas at the top of absorption tower (4), be then provided with the waste liquid comb (6) of discharging for desulfurization slurry in the bottom of absorption tower (4).
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN108114591A (en) * | 2017-12-28 | 2018-06-05 | 山东义丰环保机械股份有限公司 | A kind of flue gas processing 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 |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5993765A (en) * | 1995-05-16 | 1999-11-30 | Metallgesellschaft Aktiengesellschaft | Process for the dry desulfurization of a combustion gas |
| CN101099918A (en) * | 2007-06-06 | 2008-01-09 | 中电投远达环保工程有限公司 | Adsorption tower smoke directly ventilating technology |
| CN102580517A (en) * | 2011-01-18 | 2012-07-18 | 刘上光 | Fume desulfurization system and method by adopting dried alkali electrostatic spraying and fume humidifying cooling method |
| CN203417599U (en) * | 2013-08-28 | 2014-02-05 | 成都信鑫信息技术有限公司 | Flue-gas desulfurization control device in power field |
-
2014
- 2014-12-02 CN CN201410716386.6A patent/CN104353350B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5993765A (en) * | 1995-05-16 | 1999-11-30 | Metallgesellschaft Aktiengesellschaft | Process for the dry desulfurization of a combustion gas |
| CN101099918A (en) * | 2007-06-06 | 2008-01-09 | 中电投远达环保工程有限公司 | Adsorption tower smoke directly ventilating technology |
| CN102580517A (en) * | 2011-01-18 | 2012-07-18 | 刘上光 | Fume desulfurization system and method by adopting dried alkali electrostatic spraying and fume humidifying cooling method |
| CN203417599U (en) * | 2013-08-28 | 2014-02-05 | 成都信鑫信息技术有限公司 | Flue-gas desulfurization control device in power field |
Non-Patent Citations (1)
| Title |
|---|
| 李晓芸等: "《火电厂有害气体控制技术》", 31 March 2005 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN108114591A (en) * | 2017-12-28 | 2018-06-05 | 山东义丰环保机械股份有限公司 | A kind of flue gas processing method |
| 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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