CN102407066A - Sintering flue gas wet denitration method - Google Patents
Sintering flue gas wet denitration method Download PDFInfo
- Publication number
- CN102407066A CN102407066A CN2010102919633A CN201010291963A CN102407066A CN 102407066 A CN102407066 A CN 102407066A CN 2010102919633 A CN2010102919633 A CN 2010102919633A CN 201010291963 A CN201010291963 A CN 201010291963A CN 102407066 A CN102407066 A CN 102407066A
- Authority
- CN
- China
- Prior art keywords
- nox
- denitration
- flue gas
- amount
- oxidation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 239000003546 flue gas Substances 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 52
- 238000005245 sintering Methods 0.000 title abstract description 10
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 46
- 230000003647 oxidation Effects 0.000 claims abstract description 45
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 32
- 239000002002 slurry Substances 0.000 claims abstract description 31
- 239000006028 limestone Substances 0.000 claims abstract description 30
- 235000019738 Limestone Nutrition 0.000 claims abstract description 29
- 230000023556 desulfurization Effects 0.000 claims abstract description 29
- 238000010521 absorption reaction Methods 0.000 claims abstract description 27
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 claims abstract description 19
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims abstract description 12
- 230000005587 bubbling Effects 0.000 claims abstract description 8
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims abstract description 6
- 235000010261 calcium sulphite Nutrition 0.000 claims abstract description 6
- 238000002156 mixing Methods 0.000 claims abstract description 6
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 28
- 239000007789 gas Substances 0.000 claims description 25
- 239000003517 fume Substances 0.000 claims description 18
- 238000009987 spinning Methods 0.000 claims description 17
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 14
- 235000010216 calcium carbonate Nutrition 0.000 claims description 14
- 230000003009 desulfurizing effect Effects 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 4
- 238000005422 blasting Methods 0.000 claims description 3
- 239000010440 gypsum Substances 0.000 abstract description 11
- 229910052602 gypsum Inorganic materials 0.000 abstract description 11
- 230000001590 oxidative effect Effects 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 238000003915 air pollution Methods 0.000 abstract description 2
- 238000010042 air jet spinning Methods 0.000 abstract 1
- 238000003795 desorption Methods 0.000 abstract 1
- 238000011010 flushing procedure Methods 0.000 abstract 1
- 235000010333 potassium nitrate Nutrition 0.000 abstract 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 13
- 230000003197 catalytic effect Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000011575 calcium Substances 0.000 description 4
- 239000007800 oxidant agent Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 208000005156 Dehydration Diseases 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000000205 computational method Methods 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000001360 synchronised effect Effects 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 244000025254 Cannabis sativa Species 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 230000002452 interceptive effect Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention relates to the field of air pollution control, in particular to a sintering flue gas wet denitration process. A sintering flue gas wet denitration method is characterized in that denitration is carried out while a desulfurization device adopts an air-jet spinning absorption tower or other bubbling absorption towers for desulfurization; in the denitration, when desulfurizer limestone slurry is added into a slurry pool of the absorption tower, the limestone slurry amount required by denitration is increased; when the amount of the oxidation air for oxidizing the calcium sulfite into the calcium sulfate is blown into the slurry tank, the oxidation of NO into NO is increased2、N2O5The amount of oxidizing air required. The invention is characterized in that the desulfurization system is additionally provided with a desorption device on the wet limestone gypsum sintering flue gas desulfurization system of the existing gas-jet rotary flushing or other bubbling water bath type desulfurization device, namely under the condition of fully mixing slurry and flue gasAmount of limestone slurry required for saltpeter and increased oxidation of NO to NO2、N2O5The required amount of oxidizing air, thereby realizing the wet denitration process with effective denitration and low operation cost.
Description
Technical field
The present invention relates to a kind of prevention and control of air pollution field, relate in particular to a kind of sinter fume wet method denitrating technique.
Background technology
Gas denitrifying technology mainly contains three kinds: (Selective Catalytic Reduction is called for short SCR to SCR; Selective catalytic reduction), SNCR (Selective Non-Catalytic Reduction; Be called for short SNCR; The SNCR method) and catalytic oxidation/reducing process, wherein: SCR, SNCR all belong to dry method; Catalytic oxidation/reducing process belongs to wet method.What at present, application was maximum is the SCR method.But SCR method engineering cost is extremely expensive, and operating cost is also very high, and floor space is big; Used liquefied ammonia is the national secondary dangerous material, and management maintenance is strict; The solid catalyst waste disposal difficulty that is produced.Catalytic oxidation/reducing process is to adopt the strong oxidizer of special prescription through the catalytic oxidation to NO, and reduction combines with limestone-gypsum spray column desulphurization system then, and strong oxidizer sprays at the spray desulfurizing tower spraying layer, and part NO is removed.Though this method is more simple than SCR, SNCR method; But the catalytic oxidant expense is high; Also need existing desulphurization system transformation and increase some facilities, it is more reasonable that this method is used for going up the denitration of the high NOx concentration of power plant's electricity generation boiler flue gas of desulphurization system.
The concentration of NOx is generally at 300mg/m in the sinter fume
3About, concentration is not high, sets up special denitrification apparatus, as adopts dry techniques such as the main denitration technology SCR of present flue gas, SNCR, and is extremely uneconomical reasonable.Suitable operating cost input also will be arranged catalytic oxidation/reducing process and to the transformation of desulphurization system, therefore, sinter fume is also very unreasonable with this method.But the NOx of sinter fume is not administered and will cause the discharging that exceeds standard (concentration of the boiler comprehensive discharge standard NOx that is about to assign will be controlled at 200mg/m
3).
Existing gas outburst spinning dive sintering flue gas desulfurization technology and equipment are sulfur removal technology systems, and its flow process is seen accompanying drawing 1.Pending sinter fume is after booster fan 1 boosts; At first get into the cooling pretreatment unit 2 before the absorption tower 3; Contact with cool slurry with process for cooling water; Get into subsequently in the gas outburst spinning dive absorption tower 3 according to aerodynamic principle exploitation, all press the back to pour at a high speed to arrange according to certain rules at pressure-stabilizing section, by the gas outburst spinning dive device that some gas blowout pipes are formed, flue gas sprays in the absorption slurries along the gas spurt tangential direction rotary-cut of gas blowout pipe bottom.Described slurries are lime stone slurry, and slurries get into the stock tank that supplies stock tank 10 after slurrying, to inject bottom in the absorption tower 3 by limestone powder bin 8 through batcher 9.Because special gas blowout device; The micro air bubble of ejection is produced violent liquidate in slurries, effect such as shearing, eddy flow, fragmentation; Thereby produce the blending of a height, strong gas-liquid two-phase turbulent region of interfering, greatly promoted the gas-liquid mass transfer effect and the self adaptation power of exhaust gas volumn fluctuation.In this course, the SO in the flue gas
2Deng pollutant abundant concurrent biochemical absorption reaction of mass transfer in liquid phase; Pollutants such as dust residual in the flue gas are also further removed behind contact liq; 3 slurries districts are become micro air bubble by disperse to flue gas on the absorption tower; In three-phase turbulent mass transfer, constantly be purified, break, accomplish purification process until rising to slurries face place.Breeze way and external horizontal flue formula demister 4 (the two closes and is called combined defroster) that flue gas after being purified gets into 3 tops, absorption tower carry out post processing, and clean flue gas reaches the setting index request, by chimney 5 dischargings.The calcium sulfite of the main generation in reaction back is slurries district, 3 bottom on the absorption tower, and the air with oxidation fan 6 pressures blast is oxidized to calcium sulfate, and then crystallization generates gypsum, outward transport utilization after eddy flow and vacuum belt dewaterer 7 dehydrations.
Summary of the invention
The object of the present invention is to provide a kind of sinter fume wet method denitration method; This denitration method is in water-bath type desulfurizer wet type lime stone gypsum sintering flue gas desulfurization systems such as existing gas outburst spinning dive or other bubbling class; Be under the abundant mixing condition of slurries and flue gas ability, be oxidized to NO with increase NO through increasing the required limestone slurry liquid measure of denitration
2, N
2O
5Required oxidation air amount, thus realize the wet method denitrating technique of effective denitration and low operating cost.
To achieve these goals, the present invention adopts following technical scheme:
A kind of sinter fume wet method denitration method; Adopt water-bath type absorption towers such as gas outburst spinning dive absorption tower or other bubbling classes at desulfurizer; Be under the abundant mixing condition of slurries and flue gas; Carry out denitration when realizing desulfurization, said denitration is when the stock tank adding desulfurizing agent lime stone slurry on absorption tower, increases the required limestone slurry liquid measure of denitration; When in stock tank, blasting calcium sulfite oxidation and being the oxidation air amount of calcium sulfate, increase NO and be oxidized to NO
2, N
2O
5Required oxidation air amount.
The computing formula of the lime stone amount that said increase denitration is required is:
NO
XThe amount of removing: R
NOX=Q
Flue gas* C
NOX* η
NOX/ 1000/M
NOX
Need consumption lime stone amount: N
CaCO3, NOX=R
NOX* 0.5 * M
CaCO3/ 1000/1000.
Saidly remove the required air capacity of NOx oxidation to calculate formula following:
G
NO2=Q
Flue gas* C
NO2* η
NO2÷ 1000 ÷ M
NO2* 0.10 * 22.4 ÷ 21% ÷ 1000
G
NO=Q
Flue gas* C
NO* η
NO÷ 1000 ÷ M
NO* 0.90 * 22.4 ÷ 21% ÷ 1000
G
NOX?=?G
NO2?+?G
NO??；
In the above-mentioned formula: R
NOX: NO
XThe amount of removing, mol/h;
N
CaCO3, NOX: NOx is converted into the CaCO that calcium nitrate need consume
3Amount, t/h;
G
NOX: remove the required theoretical air requirement of NOx oxidation, Nm
3/ h;
Q
Flue gas: smoke treatment amount, Nm
3/ h;
C
NOX: NO in the flue gas
XConcentration, mg/Nm
3
η
NOX: denitration efficiency, %;
M
NOX: NO
XMolal weight, g/mol.
The present invention is in water-bath type desulfurizers such as gas outburst spinning dive wet type lime lime-gypsum method sintering desulfuration device or other bubbling class; Be under the abundant mixing condition of slurries and flue gas, be employed in absorption tower increase oxidation air amount the NOx (wherein being mainly NO) that captures in the wet desulfuration tower in the flue gas is oxidized to NO
2, N
2O
5Etc. valence state soluble in water, and then in the reaction tank on absorption tower, increase a certain amount of desulfurizing agent CaCO
3, supply denitration reaction.Through flue gas and CaCO
3The slurries mixed high-efficient mass transferring that fully spins in desulfurization, is achieved many things at one stroke, and makes the NO in the flue gas
2, N
2O
5With the water (H in the slurries
2O) combine to generate nitric acid (HNO
3), nitric acid (HNO
3) and calcium carbonate (CaCO
3) reaction generation calcium nitrate, reach discharged gas fume NOx and remove the effect more than 50%, satisfy the high standard emission request.
Sinter fume wet method denitration method of the present invention is to be oxidized to NO through increasing the required limestone slurry liquid measure of denitration with increase NO
2, N
2O
5Required oxidation air amount, thus realize the wet method denitrating technique of effective denitration and low operating cost.
The present invention compares with the existing SCR denitration technology, and its beneficial effect is following:
1) construction costs is low, special engineering cost need not take place, denitration in desulfurization;
2) operating cost is low, only increases required oxidation air amount and desulfurization dosage;
3) maintenance is low, does not take place separately, and is synchronous with desulfurization;
4) operation control simple and flexible is synchronous with desulfurization, no specific (special) requirements;
5) accessory substance is a calcium nitrate waste water, can be used as the fertilizer of trees and green grass, realizes the zero-emission of waste water;
6) be applicable to water-bath type desulfurizing tower desulphurization systems such as gas outburst spinning dive absorption tower or other bubbling class.
Description of drawings
Fig. 1 is existing gas outburst spinning dive sintering flue gas desulfurization process flow diagram.
Among the figure: 1 booster fan, 2 cooling pretreatment units, 3 gas outburst spinning dive absorption towers, 4 demisters, 5 chimneys, 6 oxidation fans, 7 dewaterers, 8 limestone powder bins, 9 batchers, 10 supply stock tank.
The specific embodiment
Below in conjunction with accompanying drawing and specific embodiment the present invention is described further.
Sinter fume wet method denitration method of the present invention is when desulfurization is carried out on water-bath type absorption towers such as desulfurizer employing gas outburst spinning dive absorption tower or other bubbling classes, carries out denitration.Gas outburst spinning dive wet type limestone-gypsum method sintering desulfuration denitrating technique flow process is as shown in Figure 1.The flue gas that the sintering main exhauster comes out gets into cooling pretreatment unit 2 and carries out preliminary treatment after booster fan 1 supercharging, then gets into 3 desulfurization of gas outburst spinning dive absorption tower, denitration reaction is once accomplished, purifies flue gas up to standard after demister 4 demists from chimney 5 discharges.The oxidation air of denitration oxidation air and desulfurization is blasted by oxidation fan 6; Desulfurization, 250 used order agstones of denitration get into the stock tank that supplies stock tank 10 after slurrying, to inject bottom in the absorption tower 3 by limestone powder bin 8 through batcher 9; Flue gas gets into slurries through the gas outburst spinning dive device; Efficient mass transfer is stirred in rotary-cut, reaches the purpose of desulphurization denitration.
The calcium sulfite of the main generation in reaction back is slurries district, 3 bottom on the absorption tower, and the air with oxidation fan 6 pressures blast is oxidized to calcium sulfate, and then crystallization generates gypsum, outward transport utilization after eddy flow and vacuum belt dewaterer 7 dehydrations.
The present invention need not increase special strong oxidizer and special denitrfying agent, need not increase special denitration device yet, is denitration in desulfurization.
The desulphurization reaction process is following:
Absorb: SO
2(gas)+H
2O → SO
2(dissolving)+H
2O → H
++ HSO
3 -→ 2H
++ SO
3 2-
Dissolving: H
++ CaCO
3→ Ca
2++ HCO
3 -
Oxidation: HSO
3 -+ 1/2O
2(dissolving) → SO
4 2-+ H
+SO
3 2-+ 1/2O
2(dissolving) → SO
4 2-
Neutralization: H
++ HCO
3 -→ H
2O+CO
2
Crystallization: Ca
2++ SO
3 2-+ 1/2H
2O → CaSO
31/2H
2O (Gu)
Ca
2++ SO
4 2-+ 2H
2O → CaSO
42H
2O (Gu)
Whole denitration reaction process is following:
2NO?+?O
2?→?2NO
2
4NO
2?+?O
2?→?2N
2O
5
N
2O
5?＋?H
2O?→?2HNO
3
4NO?+?3O
2?+?2H
2O?→4HNO
3?;
4NO
2?+?O
2?+?2H
2O?→4HNO
3?；
2HNO
3＋CaCO
3?＝Ca（NO
3）
2?+?H
2O+?CO
2
The accessory substance of desulphurization reaction is a gypsum, and the denitration product is a calcium nitrate.
Denitrating technique of the present invention is when the stock tank adding desulfurizing agent lime stone slurry on absorption tower, increases the required limestone slurry liquid measure of denitration; When in stock tank, blasting calcium sulfite oxidation and being the oxidation air amount of calcium sulfate, increase NO and be oxidized to NO
2, N
2O
5Required oxidation air amount.Promptly when calculating the required oxidation theoretical air requirement of desulfurization, consider, calculate and increase the required oxidation air amount of denitration; When confirming desulfurization dosage, to consider, calculate and increase the required CaCO of denitration
3Amount.Oxidation air amount and calcium nitrate amount computing formula that denitration increases are specific as follows:
1, setting removes the required air capacity of NOx oxidation.
G
NO2=Q
Flue gas* C
NO2* η
NO2÷ 1000 ÷ M
NO2* 0.25 * 22.4 ÷ 21% ÷ 1000
G
NO=Q
Flue gas* C
NO* η
NO÷ 1000 ÷ M
NO* 0.75 * 22.4 ÷ 21% ÷ 1000
G
NOX?=?G
NO2?+?G
NO??；
2, set NOx and be converted into the CaCO that calcium nitrate need consume
3Amount
NO
XThe amount of removing: R
NOX=Q
Flue gas* C
NOX* η
NOX/ 1000/M
NOX
Need consumption lime stone amount: N
CaCO3, NOX=R
NOX* 0.5 * M
CaCO3/ 1000/1000
In the formula: G
NOX: remove the required air capacity of NOx oxidation, Nm
3/ h;
R
NOX: NO
XThe amount of removing, mol/h;
N
CaCO3, NOX: NOx is converted into the CaCO that calcium nitrate need consume
3Amount, t/h;
Q
Flue gas: smoke treatment amount, Nm
3/ h;
C
NOX: NO in the flue gas
XConcentration, mg/Nm
3
η
NOX: denitration efficiency, %;
M
NOX: NO
XMolal weight, g/mol.
Embodiment 1
1,300,000/Nm
3Sinter fume adopts gas outburst spinning dive wet type desulfurization method of limestone-gypsum, and the content of NOx is 300mg/Nm in the flue gas
3,, calculate the corresponding oxidation air amount and the corresponding lime stone amount of increase that denitration increases according to the aforementioned calculation formula by the NOx that removes 50%.
(1) transforms NO
XRequired air quantity
1,300,000/Nm
3Because NOx is 300mg/Nm in the sinter fume
3(be mainly NO and NO
2, generally both ratios are 0.75:0.25) and under the forced oxidation condition, oxidation reaction (set conversion ratio and be 50%) can take place, generate nitrate ion, change into calcium nitrate with calcium carbonate then; According to the formula of NOx oxygen required air quantity, calculate NO respectively
2Transform needed theoretical air requirement with NO:
G
NO2=Q
Flue gas* C
NO2* η
NO2÷ 1000 ÷ M
NO2* 0.25 * 22.4 ÷ 21% ÷ 1000
=1300000?×300?×0.25?×?50%?÷?1000?÷?46?×0.25?×22.4÷21%?÷?1000?m
3/h?=28.26?m
3/h
G
NO=Q
Flue gas* C
NO* η
NO÷ 1000 ÷ M
NO* 0.75 * 22.4 ÷ 21% ÷ 1000
=1300000?×?300×0.75?×?50%?÷?1000?÷?30?×0.75?×22.4÷21%?÷?1000?m
3/h?=390?m
3/h
Therefore, remove 50% NO
XThe theoretical air requirement of required increase is:
G
NOX?=?G
NO2?+?G
NO?=?28.26?m
3/h +?390m
3/h?=?418.26?m
3/h
(2) go into to remove NO in the tower flue gas
XThe denitration dosage that needs consumption
NO
XThe amount of removing:
R
NO=Q flue gas * C
NO* η
NOX/ 1000/M
NO
=1,300,000×300×0.75×0.5/1000/30?mol/h?=4875?mol/h
R
NO2=Q flue gas * C
NO2* η
NOX/ 1000/M
NO2
=1,300,000×300×0.25×0.5/1000/46?mol/h?=1059.78?mol/h
R
NOX=R
NO?+?R
NO2=?5934.78?mol/h
The consumption of limestone amount that needs to increase is:
N
CaCO3,NOX=?R
NOX×0.5×M
CaCO3/1000/1000
=5934.78×0.5×100?/1000/1000?t/h?=?0.297?t/h
By calculating oxidation air amount 418.26 m that confirm
3Lime stone amount 0.297 t/h that/h and denitration are required, with the required oxidation air amount of desulfurization and lime stone amount in the lump (same collocation point simultaneously) join and participate in reaction, denitration when reaching desulfurization in the system.The automatic monitoring display denitration efficiency is 50%～60%.
Embodiment 2
700,000/Nm
3Sinter fume adopts gas outburst spinning dive wet type desulfurization method of limestone-gypsum, and the content of NOx is 320mg/Nm in the flue gas
3, in desulfurizing tower,, calculate corresponding oxidation air amount 240.23 m of increase equally by aforementioned calculation formula and computational methods by the NOx that removes 50%
3/ h and corresponding lime stone amount 0.1704 t/h of increase, oxidation air amount and the lime stone amount in the lump adding system required with desulfurization participate in reaction; The flue gas after being purified automatic monitoring system shows that denitration efficiency is 52%～65%.
87.5 ten thousand/Nm
3Sinter fume adopts gas outburst spinning dive wet type desulfurization method of limestone-gypsum, and the content of NOx is 350mg/Nm in the flue gas
3,, calculate the corresponding oxidation air amount 328.44m of increase by aforementioned calculation formula and computational methods by the NOx that removes 50%
3/ h and corresponding lime stone amount 0.233 t/h of increase, oxidation air amount and the lime stone amount in the lump adding system required with desulfurization participate in reaction; Flue gas before and after the sulphur denitration detects data and shows that denitration efficiency is about 55%.
Claims (3)
1. a sinter fume wet method denitration method is characterized in that, adopts water-bath type absorption towers such as gas outburst spinning dive absorption tower or other bubbling classes at desulfurizer, promptly under the abundant mixing condition of slurries and flue gas, carries out denitration in the time of desulfurization; Said denitration is when the stock tank adding desulfurizing agent lime stone slurry on absorption tower, increases the required limestone slurry liquid measure of denitration; When in stock tank, blasting calcium sulfite oxidation and being the oxidation air amount of calcium sulfate, increase NO and be oxidized to NO
2, N
2O
5Required oxidation air amount.
2. sinter fume wet method denitration method according to claim 1, it is characterized in that: the computing formula of the lime stone amount that said increase denitration is required is:
NO
XThe amount of removing: R
NOX=Q
Flue gas* C
NOX* η
NOX/ 1000/M
NOX
Need consumption lime stone amount: N
CaCO3, NOX=R
NOX* 0.5 * M
CaCO3/ 1000/1000
In the formula: R
NOX: NO
XThe amount of removing, molt/h;
N
CaCO3, NOX: NOx is converted into the CaCO that calcium nitrate need consume
3Amount, t/h;
Q
Flue gas: smoke treatment amount, Nm
3/ h;
C
NOX: NO in the flue gas
XConcentration, mg/Nm
3
η
NOX: denitration efficiency, %;
M
NOX: NO
XMolal weight, g/mol;
M
CaCO3: CaCO
3Molal weight, g/mol.
3. sinter fume wet method denitration method according to claim 1 is characterized in that: it is following that the required air capacity of the said NOx of removing oxidation is calculated formula:
G
NO2=Q
Flue gas* C
NO2* η
NO2÷ 1000 ÷ M
NO2* 0.10 * 22.4 ÷ 21% ÷ 1000
G
NO=Q
Flue gas* C
NO* η
NO÷ 1000 ÷ M
NO* 0.90 * 22.4 ÷ 21% ÷ 1000
G
NOX?=?G
NO2?+?G
NO
In the formula: G
NOX:Remove the required air capacity of NOx oxidation, Nm
3/ h;
Q
Flue gas: smoke treatment amount, Nm
3/ h;
C
NOX: NO in the flue gas
XConcentration, mg/Nm
3
η
NOX: denitration efficiency, %;
M
NOX: NO
XMolal weight, g/mol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102919633A CN102407066A (en) | 2010-09-26 | 2010-09-26 | Sintering flue gas wet denitration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102919633A CN102407066A (en) | 2010-09-26 | 2010-09-26 | Sintering flue gas wet denitration method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102407066A true CN102407066A (en) | 2012-04-11 |
Family
ID=45909591
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102919633A Pending CN102407066A (en) | 2010-09-26 | 2010-09-26 | Sintering flue gas wet denitration method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102407066A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108317100A (en) * | 2018-04-04 | 2018-07-24 | 华润电力（沧州运东）有限公司 | A kind of air compressor control method, equipment and system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0226863A1 (en) * | 1985-11-29 | 1987-07-01 | General Electric Company | Method for scrubbing sulfur oxides and nitrogen oxides in a flue gas duct |
| CN101168118A (en) * | 2006-10-25 | 2008-04-30 | 宝山钢铁股份有限公司 | Sintering smoke wet method sulphur removing and dust removing technology |
| CN101259372A (en) * | 2008-04-29 | 2008-09-10 | 刘海清 | High-efficiency flue gas desulfurization denitration dust-removing integrated technique |
| JP2009166013A (en) * | 2008-01-21 | 2009-07-30 | Mitsubishi Heavy Ind Ltd | Exhaust gas treatment system of coal fired boiler |
| CN201493032U (en) * | 2009-08-25 | 2010-06-02 | 国电环境保护研究院 | Limestone/gypsum wet flue gas desulfurization and denitrification integrated device |
-
2010
- 2010-09-26 CN CN2010102919633A patent/CN102407066A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0226863A1 (en) * | 1985-11-29 | 1987-07-01 | General Electric Company | Method for scrubbing sulfur oxides and nitrogen oxides in a flue gas duct |
| CN101168118A (en) * | 2006-10-25 | 2008-04-30 | 宝山钢铁股份有限公司 | Sintering smoke wet method sulphur removing and dust removing technology |
| JP2009166013A (en) * | 2008-01-21 | 2009-07-30 | Mitsubishi Heavy Ind Ltd | Exhaust gas treatment system of coal fired boiler |
| CN101259372A (en) * | 2008-04-29 | 2008-09-10 | 刘海清 | High-efficiency flue gas desulfurization denitration dust-removing integrated technique |
| CN201493032U (en) * | 2009-08-25 | 2010-06-02 | 国电环境保护研究院 | Limestone/gypsum wet flue gas desulfurization and denitrification integrated device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108317100A (en) * | 2018-04-04 | 2018-07-24 | 华润电力（沧州运东）有限公司 | A kind of air compressor control method, equipment and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8110164B2 (en) | Flue-Gas purification and reclamation system and method thereof | |
| CN105056749A (en) | System and method for removing nitric oxides and sulfur oxides in flue gas simultaneously | |
| CN102179146B (en) | Flue gas desulfurization and denitrification system and process based on dielectric barrier discharge combined with lye absorption | |
| US9895657B2 (en) | High-efficiency method for removing sulfur and mercury of coal-fired flue gas, and apparatus thereof | |
| CN101385943A (en) | Simultaneous removal process based on semi-dry method | |
| CN102188897B (en) | Wet flue gas desulfurization and denitrification combined method | |
| CN204891568U (en) | Boiler flue gas integration distributing type SOx/NOx control device | |
| CN102772986B (en) | Flue gas desulfurization and denitration integrated process | |
| CN101632897B (en) | Method for simultaneously removing sulfur oxides and nitric oxides in flue gas | |
| CN108176204A (en) | Flue gas and desulfurizing and denitrifying integrated purification system and purification method | |
| CN101927124A (en) | Flue gas denitrification method | |
| CN105056746A (en) | Method for realizing boiler flue gas integrated distributed desulfurization and denitrification process | |
| CN101543724A (en) | Ammonia desulphurization method suitable for sintering flue gas treatment | |
| CN102716651A (en) | Desulfurization and denitrification integral smoke gas purification treatment system and desulfurization and denitrification integral smoke gas purification treatment process | |
| CN105148698A (en) | Boiler flue gas desulfurization and denitrification system | |
| CN105032140A (en) | System and method for denitrating and desulfurizing sintered flue gas through low-temperature wet method | |
| CN102847430B (en) | System and technology for cleaning flue gas | |
| CN105169923B (en) | One kind improves limestone/lime gypsum wet flue gas desulfurizing technique | |
| CN202844865U (en) | Denitration process system by high-temperature atomization wet method | |
| CN203469804U (en) | Absorption tower device capable of simultaneously desulfurizing and denitrifying smoke | |
| CN206762618U (en) | A kind of dry-wet integratedization desulfuring and denitrifying apparatus | |
| CN102773001B (en) | High-temperature atomization wet denitration process system and denitration method | |
| CN205127700U (en) | System for low temperature wet process is to desulfurization of sintering flue gas denitration | |
| CN102407066A (en) | Sintering flue gas wet denitration method | |
| CN104138701A (en) | Flue gas purifying device of multi-functional coal-fired boiler |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20120411 |