CN207371337U - A kind of system for being classified oxidative absorption formula flue gas desulfurization and denitrification - Google Patents
A kind of system for being classified oxidative absorption formula flue gas desulfurization and denitrification Download PDFInfo
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- CN207371337U CN207371337U CN201721342372.8U CN201721342372U CN207371337U CN 207371337 U CN207371337 U CN 207371337U CN 201721342372 U CN201721342372 U CN 201721342372U CN 207371337 U CN207371337 U CN 207371337U
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- oxidant
- flue gas
- oxidation
- oxidative absorption
- oxidative
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- 230000001590 oxidative effect Effects 0.000 title claims abstract description 349
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 156
- 239000003546 flue gas Substances 0.000 title claims abstract description 142
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 139
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 36
- 230000023556 desulfurization Effects 0.000 title claims abstract description 32
- 239000007800 oxidant agent Substances 0.000 claims abstract description 202
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 135
- 230000003647 oxidation Effects 0.000 claims abstract description 134
- 238000001816 cooling Methods 0.000 claims abstract description 23
- 238000012432 intermediate storage Methods 0.000 claims description 63
- 238000003860 storage Methods 0.000 claims description 63
- 239000002002 slurry Substances 0.000 claims description 53
- 238000012546 transfer Methods 0.000 claims description 53
- 235000019738 Limestone Nutrition 0.000 claims description 49
- 239000006028 limestone Substances 0.000 claims description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 239000003795 chemical substances by application Substances 0.000 claims description 38
- 239000007788 liquid Substances 0.000 claims description 33
- 239000000110 cooling liquid Substances 0.000 claims description 14
- 238000009434 installation Methods 0.000 claims description 14
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 12
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 12
- 239000004571 lime Substances 0.000 claims description 12
- 230000009286 beneficial effect Effects 0.000 abstract 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 48
- 229910052602 gypsum Inorganic materials 0.000 description 38
- 239000010440 gypsum Substances 0.000 description 38
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 30
- 239000000243 solution Substances 0.000 description 28
- 239000011259 mixed solution Substances 0.000 description 25
- 238000004537 pulping Methods 0.000 description 25
- 230000000694 effects Effects 0.000 description 17
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 15
- 239000005708 Sodium hypochlorite Substances 0.000 description 14
- 239000007789 gas Substances 0.000 description 12
- UKLNMMHNWFDKNT-UHFFFAOYSA-M sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 description 12
- 229960002218 sodium chlorite Drugs 0.000 description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 11
- 229910052760 oxygen Inorganic materials 0.000 description 11
- 239000001301 oxygen Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- 239000000779 smoke Substances 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- 230000008859 change Effects 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 235000019504 cigarettes Nutrition 0.000 description 7
- 239000000843 powder Substances 0.000 description 7
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 6
- 230000018044 dehydration Effects 0.000 description 5
- 238000006297 dehydration reaction Methods 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- 229910052815 sulfur oxide Inorganic materials 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- -1 wherein Chemical compound 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- 239000003500 flue dust Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000004575 stone Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
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- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000004513 sizing Methods 0.000 description 2
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
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- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 229940077239 chlorous acid Drugs 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
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- 239000004570 mortar (masonry) Substances 0.000 description 1
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- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
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- 239000004317 sodium nitrate Substances 0.000 description 1
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- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
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- 238000005507 spraying Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model belongs to technical field of environment protection equipment, specifically, it is related to a kind of system for being classified oxidative absorption formula flue gas desulfurization and denitrification, the oxidative absorption system connected including cooling oxidative system and with cooling oxidative system, cooling oxidative system is used to carry out stair oxidation to flue gas and cool down, oxidative absorption system is used to carry out secondary oxidation to the flue gas after oxidation and absorb, the oxidative system that cools down includes heat sink and oxidant add-on system, the oxidant add-on system is connected with heat sink, oxidant is delivered to heat sink, stair oxidation is carried out to flue gas, the beneficial effects of the utility model are by setting oxidant add-on system, realize the desulfurization and denitration to flue gas simultaneously first, secondly classification oxidation is carried out to flue gas, greatly improve desulfurization and denitration ability；It by the way that the oxidant in oxidant add-on system had both been transported in heat sink, while is transported in oxidative absorption device, oxidation effectiveness is more preferable compared with oxidation is only carried out by air.
Description
Technical field
The utility model belongs to technical field of environment protection equipment, specifically, is related to a kind of classification oxidative absorption formula flue gas and takes off
The system of sulphur denitration.
Background technology
Flue gas is the mixture of gas and flue dust, is the main reason for polluting residential block air.The ingredient of flue gas is very complicated,
Gas includes water vapour, sulfur dioxide, nitrogen, oxygen, carbon monoxide, carbon dioxide, hydrocarbon and nitrogen oxidation and closes
Object etc., flue dust include ash content, coal grain, oil droplet and high-temperature split product of fuel etc..As it can be seen that flue gas is more to the pollution of environment
The combined pollution of kind poisonous substance.Flue dust is related to the harmfulness of human body and the size of particle, and it is diameter to generate the mostly of harm to human body
Floating dust less than 10um, it is especially maximum with the floating dust harmfulness of 1-2.5um.Oxynitrides and sulfur dioxide form acid rain
One of main matter.
In recent decades, with the continuous improvement of environmental requirement, flue gas desulfurization and denitrification integrated technique has obtained quickly
Development, the flue gas that the mode of flue gas removing at present is mainly formed using individual desulphurization and denitration equipment simple syndication is assembled take off
Sulphur denitration device, its main feature is that NOX, SO2 removing are separately removed, gas removal efficiency is higher, but often there are systems to account for
The problem of ground area is big, initial investment is big and operating cost is high.
In numerous sulfur removal technologies, Limestone-gypsum Wet Flue Gas Desulfurization Process technique is most widely used, technology is the most ripe, just
At present from the point of view of operating condition, the desulfuration efficiency of the technique maintains essentially in more than 90%, and desulfurization effect is very notable, but for cigarette
The removing of NOX almost helpless in gas.Therefore, design it is a kind of improvement cost it is low, can desulphurization denitration be carried out at the same time one
Body equipment becomes urgent problem to be solved.
In view of this it is special to propose the utility model.
Utility model content
The technical problems to be solved in the utility model is to overcome the deficiencies of the prior art and provide a kind of classification oxidative absorption
The system of formula flue gas desulfurization and denitrification by setting oxidant add-on system, realizes desulfurization and denitration to flue gas simultaneously first,
Secondly classification oxidation is carried out to flue gas, greatly improves desulfurization and denitration ability；By by the oxidant in oxidant add-on system
Both it was transported in heat sink, while was transported in oxidative absorption device, with only passes through air in existing oxidative absorption device
It carries out oxidation to compare, the classification oxidation effectiveness of the utility model is more preferable, more preferable to the removal effect of NOx in flue gas and Sox, especially
It is that removal to NOx is particularly evident；Using sodium chlorite and the mixed solution of sodium hypochlorite, obtain the NO in flue gas and SO2
Sufficiently oxidation, compared with prior art, improves the absorbability of NO；The structure can be in original flue gas desulphurization system
It is transformed, it is made to be provided simultaneously with denitration function, the technical matters is simple, and investment, operating cost are low, is taken off in realization NOX, SO2
Except while, effectively control the environmentally friendly cost of enterprise, have broad application prospects；The utility model be particularly suitable for NOx,
The flue gas that the content of SOx is larger is handled.
In order to solve the above technical problems, the utility model is using the basic conception of technical solution：
It is a kind of be classified oxidative absorption formula flue gas desulfurization and denitrification system, including cooling oxidative system and with cool down oxidative system
The oxidative absorption system of connection, cooling oxidative system are used to carry out stair oxidation to flue gas and cool down, and oxidative absorption system is used for
Secondary oxidation is carried out to the flue gas after oxidation and is absorbed, cooling oxidative system includes heat sink and oxidant add-on system, institute
It states oxidant add-on system to connect with heat sink, oxidant is delivered to heat sink carries out stair oxidation to flue gas.
Heat sink includes temperature-reducing tower and the first transfer pipeline for conveying cooling liquid to temperature-reducing tower, oxidant addition
System is connected with the first transfer pipeline and/or connected with temperature-reducing tower；
Preferably, the first transfer pipeline is equipped with power conveying device.
Oxidant add-on system includes oxidation agent storage device；
Oxidation agent storage device in storage oxidant be liquid oxidizer or be oxidant solution, oxidant storage dress
It puts and is connected between temperature-reducing tower by the first transfer pipeline, using the solution of liquid oxidizer or oxidant to the cigarette in temperature-reducing tower
Gas is aoxidized and cooled down；
Alternatively, heat sink further includes cooling liquid storaging device, cooling liquid storaging device passes through first with temperature-reducing tower
Transfer pipeline connects, and oxidation agent storage device is connected with the liquid storaging device that cools down and/or connected with temperature-reducing tower and/or with first
Transfer pipeline connects.
Oxidant add-on system further includes intermediate storage device, aoxidizes defeated by first between agent storage device and temperature-reducing tower
Pipeline connection is sent, the intermediate storage device is arranged on the first transfer pipeline and is connected with the first transfer pipeline, on temperature-reducing tower
Equipped with outgoing line, the outgoing line is connected with intermediate storage device；
Preferably, intermediate storage device includes intermediate storage tank and water supply installation, and intermediate storage tank is arranged on the first transfer pipeline
On, the water supply installation is connected with intermediate storage tank, is diluted oxidant to intermediate storage tank water delivery, is located at centre on the first transfer pipeline
Line segments and outgoing line between storage tank and temperature-reducing tower form circulation line, and circulation line is equipped with power set.
Oxidative absorption system includes oxidative absorption device and the oxidant for supplying oxidant into oxidative absorption device
Supply system, oxidant supply system convey oxidant to oxidative absorption system, and secondary oxidation is carried out to flue gas.
The oxidant supply system includes air supply system and/or for by the oxidant in oxidant add-on system
The adding set of oxidative absorption device is introduced, air supply system and/or adding set are connected with oxidative absorption device；
Preferably, the air supply system includes the air supply pipeline being connected with oxidative absorption device and oxidation wind
Machine, the oxidation fan are arranged on air supply pipeline.
The adding set includes addition pipeline, and the addition pipeline is arranged at oxidant add-on system and oxidative absorption dress
Between putting, for the oxidant in oxidant add-on system to be transported to oxidative absorption device；
Preferably, addition pipeline is the addition for being arranged on first transfer pipeline or being connected with oxidation agent storage device
Branch, the output terminal of the addition branch are connected with oxidative absorption device, and the addition branch road is equipped with liquid pump.
The oxidative absorption device includes oxidative absorption tower and the stone for conveying lime stone slurry into oxidative absorption tower
Mortar supply system, oxidant supply system are connected with lime white supply system and/or with oxidative absorption tower；
Preferably, the output terminal of the addition pipeline is connected with oxidative absorption tower and/or with lime white supply system；
It is highly preferred that lime white supply system includes for lime stone being configured to the pulping device of lime stone slurry, system
The output terminal of sizing device is connected with oxidative absorption tower, is added the output terminal of pipeline and is connected with pulping device and/or with oxidative absorption tower
It connects.
A kind of desulfurizing and denitrifying process carried out in above system, flue gas enter heat sink from the smoke inlet of heat sink
Interior, oxidant add-on system conveys oxidant into heat sink, is cooled down to flue gas and stair oxidation, the flue gas after oxidation
Into oxidative absorption system, flue gas is absorbed oxidative absorption system and secondary oxidation；
Preferably, the oxidant of oxidant add-on system output is divided into two-way：Intermediate storage tank is transported to all the way, is stored up in centre
The mixed solution of certain density oxidant is configured in tank, will be aoxidized by circulation line between intermediate storage tank and temperature-reducing tower
The mixed solution of agent cycles between intermediate storage tank and temperature-reducing tower, and the flue gas in temperature-reducing tower contacts simultaneously with the mixed solution of oxidant
By stair oxidation and cooling, the flue gas after stair oxidation is delivered in oxidative absorption tower；
Another way is transported to pulping device, is transported to after being mixed with the lime stone slurry of preparation in oxidative absorption tower, oxygen
Change and air, oxidant and air are blasted in absorption tower to the flue gas progress secondary oxidation after stair oxidation, and utilize limestone slurry
Liquid, which absorb, forms gypsum slurries, and gypsum slurries are discharged and post-processed out of oxidative absorption tower, obtain gypsum product.
The flow of oxidant storage tank to intermediate storage tank conveying oxidant is 2~5m3/ h, oxidant is conveyed into pulping device
Flow be 10~15m3/h；The flow of the mixed solution of oxidant in circulation line is 10~15m3/ h is low in desulfuration efficiency
After preset value, lime stone slurry is conveyed into oxidative absorption tower, the solid content of lime stone is in the slurries in pulping device
20%~30%；
Preferably, the mixed solution of the oxidant is the mixed solution of sodium chlorite and sodium hypochlorite, wherein, chlorous acid
0.04~0.05mol/L of na concn, sodium hypochlorite concentration are 0.15~0.20mol/L；Sodium hypochlorite and sodium chlorite concentrations ratio
3.7~4.0, preset value 90%.
After adopting the above technical scheme, the utility model has the advantages that compared with prior art：Pass through setting
Oxidant add-on system realizes desulfurization and denitration to flue gas, secondly carries out classification oxidation to flue gas, carry significantly simultaneously first
High desulfurization and denitration ability；By the way that the oxidant in oxidant add-on system had both been transported in heat sink, it is transported to simultaneously
In oxidative absorption device, compared with only carrying out oxidation by air in existing oxidative absorption device, the classification of the utility model
Oxidation effectiveness is more preferable, more preferable to the removal effect of NOx in flue gas and Sox, especially particularly evident to the removal of NOx；Using Asia
The mixed solution of sodium chlorate and sodium hypochlorite makes the NO in flue gas and SO2 sufficiently be aoxidized, compared with prior art, right
The absorbability of NO improves；The structure can be transformed in original flue gas desulphurization system, it is made to be provided simultaneously with denitration work(
Can, the technical matters is simple, and investment, operating cost are low, while NOX, SO2 removing is realized, effectively controls the ring of enterprise
Guaranteed cost has broad application prospects.
Specific embodiment of the present utility model is described in further detail below in conjunction with the accompanying drawings.
Description of the drawings
A part of the attached drawing as the utility model, is further understood from the utility model for providing, this practicality
New schematic description and description does not form the improper restriction to the utility model for explaining the utility model.
Obviously, the accompanying drawings in the following description is only some embodiments, to those skilled in the art, is not paying creation
Property work on the premise of, can also be obtained according to these attached drawings other accompanying drawings.In the accompanying drawings：
Fig. 1 is the structure diagram of the utility model classification oxidative absorption formula flue gas desulfurization and denitrification system；
Fig. 2 is the utility model process flow chart.
In figure：100th, temperature-reducing tower, cooler 101, oxidation agent storage device, oxidant storage tank 102, intermediate storage device
103rd, the first transfer pipeline 104, outgoing line 110, oxidative absorption tower, bubble absorbing tower 120, air supply pipeline 121, oxidation
Wind turbine 130, addition pipeline, addition branch 131, power set 140, pulping device 141, agstone adding set, lime stone
Powder cabin 142, water supply installation 150, gypsum cyclone 151, vacuum belt machine 152, gypsum storage warehouse 160, demister 161, chimney
170th, booster fan.
It should be noted that these attached drawings and word description are not intended to limit the design of the utility model in any way
Scope, but illustrate the concept of the utility model for those skilled in the art by reference to specific embodiment.
Specific embodiment
It is new below in conjunction with this practicality to make the purpose, technical scheme and advantage of the utility model embodiment clearer
The technical solution in embodiment is clearly and completely described in attached drawing in type embodiment, and following embodiment is used to illustrate this
Utility model, but be not intended to limit the scope of the present invention.
Embodiment one
As shown in Figs. 1-2, it is a kind of be classified oxidative absorption formula flue gas desulfurization and denitrification system, including cooling oxidative system and with
The oxidative absorption system of the oxidative system that cools down connection, cooling oxidative system are used to carry out stair oxidation to flue gas and cool down, aoxidize
Absorption system is used to carry out secondary oxidation to the flue gas after oxidation and absorb, and cooling oxidative system includes heat sink and oxidant
Add-on system, the oxidant add-on system are connected with heat sink, and oxidant is delivered to heat sink carries out one to flue gas
Grade oxidation.
Due to containing nitrogen oxide (NO in flue gasX) and sulfur oxide (SOX), it is directly discharged into air, it can be to air
It pollutes.At present, during the desulphurization denitration of flue gas, usually first flue gas is cooled down, then is absorbed or is aoxidized
It absorbs, the oxidative absorption stage is usually passed through air, but since the oxidability of air is limited, oxidation effectiveness is poor, if flue gas
Middle nitrogen oxide (NOX) and sulfur oxide (SOX) content is excessive, NO and SO in flue gas but will be caused2Processing is incomplete,
Clean-up effect is bad.
The utility model by setting oxidant add-on system, make its flue gas can cool down and meanwhile to flue gas but also
Stair oxidation is carried out, the flue gas after oxidation enters back into oxidative absorption system and carries out secondary oxidation, makes by two-stage oxidation in flue gas
Nitrogen oxide (NOX) and sulfur oxide (SOX) be substantially oxidized, oxidation effectiveness is greatly promoted, especially to nitrogen oxide
(NOX) removal effect it is especially prominent.
Further, heat sink includes temperature-reducing tower 100 and the first conveying for conveying cooling liquid to temperature-reducing tower 100
Pipeline 103, oxidant add-on system are connected with the first transfer pipeline 103 and/or connected with temperature-reducing tower 100.
Oxidant add-on system is connected with the first transfer pipeline 103, and oxidant is added in the first transfer pipeline 103,
Oxidant is made to enter temperature-reducing tower 100 with the cooling liquid in the first transfer pipeline 103, in connecing for cooling liquid and flue gas joint
Stair oxidation is carried out to flue gas in contacting surface, NO is made to be oxidized to NO2, make SO2It is oxidized to SO3, oxidation and cooling after flue gas be transported to
Oxidative absorption system, not oxidized NO and SO2By secondary oxidation in oxidative absorption system, by such two-stage oxidation, make
NO and SO in flue gas2It is absorbed to greatest extent, the treatment effect of flue gas is more preferable.
Wherein, the first transfer pipeline 103 is equipped with power conveying device, provides power using power conveying device, realizes
Conveying, power conveying device are generally liquid pump, such as centrifugal pump.
Scheme one, oxidant add-on system include oxidation agent storage device 101, are stored in oxidation agent storage device 101
Oxidant be liquid oxidizer or be oxidant solution, aoxidize defeated by first between agent storage device 101 and temperature-reducing tower 100
Pipeline 103 is sent to connect, the flue gas in temperature-reducing tower 100 is aoxidized and cooled down using the solution of liquid oxidizer or oxidant.
For example, the solution of oxidant can be the mixed solution of oxidant, e.g., the mixing of sodium chlorite and sodium hypochlorite is molten
Liquid.
Oxidant and water are mixed to the solution of oxidant, extremely dropped when the solution of oxidant is passed through the first Pipeline transport
After warm tower 100, the solution and smoke contacts of oxidant, the oxidant carried in one side solution aoxidize flue gas, another
Aspect, solution and the flue gas of oxidant carry out heat exchange, and the flue-gas temperature being lowered into oxidative absorption system is reduced to oxidation
The damage of part-structure in absorption system improves assimilation effect, in another aspect, flue-gas temperature is also higher at this time, makes solution and cigarette
Oxidation efficiency and oxidation rate on gas contact surface greatly improve, and therefore, greatly improve the clean-up effect of flue gas, make smoke evacuation
The flue gas of mouth is purer.
Scheme two, oxidant add-on system include oxidation agent storage device 101, and heat sink further includes cooling fluid storage
Device, cooling liquid storaging device are connected with temperature-reducing tower 100 by the first transfer pipeline 103, oxidation agent storage device 101 and drop
Geothermal liquid storage device connects.
In the program, heat sink further includes cooling liquid storaging device, and e.g., cooling liquid is water, and cool down fluid storage
Device is water tank, and water tank is connected with temperature-reducing tower 100 by the first transfer pipeline 103, and water is conveyed into temperature-reducing tower 100, profit
Cooled down with water to the flue gas in temperature-reducing tower 100, oxidation agent storage device 101 is connected with water tank, at this point, oxidant can be with
It is liquid, solid or gas, the oxidant for such as aoxidizing storage in agent storage device 101 can be Cl2(g), sodium chlorite
(s), the mixed solution of sodium hypochlorite (s) or sodium chlorite and sodium hypochlorite, oxidant be preferably capable of being dissolved in water or
Person can react substance of the generation with oxidisability with water.
Wherein, oxidation agent storage device 101 can also be connected directly with temperature-reducing tower 100, and oxidant is directly appended to drop
In warm tower 100, the flue gas in temperature-reducing tower 100 is aoxidized, oxidation agent storage device 101 can also be with the first transfer pipeline
Oxidant is added to the solution of formation oxidant in the cooling liquid in the first transfer pipeline 103, with scheme two by 103 connections
It compares, can be according to the variation of smoke components, such as the variation of nitrogen oxide content in flue gas, control increases the addition of oxidant
Amount, input amount is few, and adaptability is stronger.
Further, the first transfer pipeline 103 can be that circulation line can also irreversibly deliver pipeline, if Xun Huan
Pipeline can realize recycling for oxidant, make full use of the oxidation of oxidant, reduce the dosage of oxidant, save
Cost.
Further, oxidant add-on system further includes intermediate storage device, aoxidizes agent storage device 101 and temperature-reducing tower
It is connected between 100 by the first transfer pipeline 103, the intermediate storage device is arranged on the first transfer pipeline 103 and with
One transfer pipeline 103 connects, and temperature-reducing tower 100 is equipped with outgoing line 104, and the outgoing line 104 connects with intermediate storage device
It is logical.
Further, intermediate storage device includes intermediate storage tank 102 and water supply installation 142, and intermediate storage tank 102 is arranged on the
It is connected on one transfer pipeline 103 and with the first transfer pipeline 103, the water supply installation 142 is connected with intermediate storage tank 102, Xiang Zhong
Between 102 water delivery of storage tank dilution oxidant, the pipeline on the first transfer pipeline 103 between intermediate storage tank 102 and temperature-reducing tower 100
Section and outgoing line 104 form circulation line, and circulation line is equipped with power set.
Can also be that storage is oxidant in oxidation agent storage device 101, and oxidation agent storage device 101 is stored up to centre
A certain amount of oxidant is conveyed in tank, water supply installation 142 conveys water into intermediate storage tank 102, is made into oxidizing agent solution, centre storage
Tank 102 conveys oxidant by the first transfer pipeline 103 into temperature-reducing tower 100, and flue gas is aoxidized, the liquid warp after oxidation
Outgoing line 104 is transported in intermediate storage tank 102, and circulation line is formed between intermediate storage tank 102 and temperature-reducing tower 100, to oxidation
Agent recycles, and improves the utilization rate of oxidant.
Further, the line segments on the first transfer pipeline 103 between intermediate storage tank 102 and temperature-reducing tower 100 and lead
Go out pipeline 104 and form circulation line, circulation line is equipped with solution pump, and the oxidant for making to store in intermediate storage device is in centre
It is cycled between holding vessel 102 and temperature-reducing tower 100.
Preferably, solution pump is set respectively on the pipeline of intermediate storage tank both sides on the first transfer pipeline 103, is oxygen
The conveying of agent provides power.
Oxidative absorption system includes oxidative absorption device and the oxidant for supplying oxidant into oxidative absorption device
Supply system, oxidant supply system convey oxidant to oxidative absorption system, carry out secondary oxidation to flue gas, are inhaled by aoxidizing
Receiving apparatus carries out secondary oxidation to flue gas, and making that treated, flue gas is purer.
Further, the oxidant supply system includes air supply system and/or for by oxidant add-on system
Interior oxidant introduces the adding set of oxidative absorption device, air supply system and/or adding set and oxidative absorption device
Connection.
Further, the air supply system includes air delivery pipe and the oxidation for being arranged on air delivery pipe road
Wind turbine 121, the outlet side of air delivery pipe are connected with the bottom of oxidative absorption tower 110.Into solution, constantly drum send air, increases
The contact area of big gas-liquid, promotes the progress of oxidative absorption reaction.
Scheme one, oxidant supply system can only be air supply systems, and oxidant add-on system connects with heat sink
It is logical, make NOx in flue gas and SOx in heat sink by stair oxidation, air supply system is connected with oxidative absorption device, will be through
The NOx in the flue gas after stair oxidation and SOx are crossed in oxidative absorption device by secondary oxidation, realizes the classification oxygen to flue gas
Change, flue gas is made to be processed purer.
The air supply system includes the air supply pipeline 120 being connected with oxidative absorption device and oxidation fan 121,
The oxidation fan 121 is arranged on air supply pipeline 120.
Scheme two, oxidant supply system can be used for the oxidant in oxidant add-on system introducing oxidative absorption dress
The adding set put is introduced the oxidant in oxidant add-on system in oxidative absorption device by adding set, to flue gas
Secondary oxidation is carried out, realizes better clean-up effect.
The outlet of oxidant add-on system is divided into two, and one conveys oxidant into heat sink and carries out stair oxidation,
Another conveys oxidant into oxidative absorption system and carries out secondary oxidation, realizes that the classification to flue gas absorbs.
Further, the adding set includes addition pipeline 130, and the addition pipeline 130 is arranged at oxidant addition
Between system and oxidative absorption device, for the oxidant in oxidant add-on system to be transported to 101 in oxidative absorption device.
The addition pipeline 130 is the addition branch connected with oxidation agent storage device 101, the addition branch 130
Output terminal be connected with oxidative absorption device, it is described addition branch 130 be equipped with liquid pump.
Wherein, add pipeline 130 or be arranged on first transfer pipeline 103.
Since the oxidisability of the oxidant in oxidant add-on system is higher, by being set on oxidation agent storage device 101
Addition branch 130 is put, it is using branch 130 is added that the oxidant aoxidized in agent storage device 101 is defeated into oxidative absorption device
It send, secondary oxidation is carried out to flue gas using oxidant, oxidation effectiveness is more preferable.
Scheme three, oxidant supply system are air supply systems and for the oxidant in oxidant add-on system to be drawn
Enter the adding set of oxidative absorption device, the oxidant in oxidant add-on system is introduced oxidative absorption by adding set fills
In putting, and air is conveyed into oxidative absorption device, the two carries out secondary oxidation to flue gas jointly, realizes preferably purification effect
Fruit.
Further, the oxidative absorption device includes oxidative absorption tower 110 and for being conveyed into oxidative absorption tower 110
The lime white supply system of lime stone slurry, oxidant supply system and lime white supply system and/or with oxidative absorption tower 110
Connection.
Further, oxidant supply system includes air supply system and/or adding set, air supply system and oxygen
Change absorption tower 110 to connect.The output terminal of adding set is connected with lime white supply system and/or oxidative absorption tower 110, to lime
Convey supply oxidant in oxidant or direct phase oxidation absorption tower 110 in stone slurries, input terminal and oxidant storage tank 101 or
Person is connected with the first transfer pipeline 103 either with intermediate storage tank 102 or with outgoing line 104.
Preferably, the output terminal of air supply pipeline is connected with the bottom of oxidative absorption tower 110, supplies air to oxidation
In absorption tower 110, and the liquid in oxidative absorption tower 110 is stirred.The input terminal of adding set and oxidant storage tank
101 connections, output terminal is connected with lime white supply system, and oxidant is mixed with lime stone slurry, using lime stone slurry by oxygen
Agent dilutes, then is delivered to lime stone slurry in oxidative absorption tower 110, and two level is carried out to the flue gas in oxidative absorption tower 110
Oxidation.
Wherein, adding the output terminal of pipeline 130 can also be directly connected to oxidative absorption tower 110, and oxidant is directly added
It is added in oxidative absorption tower 110, alternatively, the output terminal and oxidative absorption tower 110 and lime white supply system of addition pipeline 130 are same
When connect.
Wherein, lime white supply system includes for lime stone being configured to the pulping device 140 of lime stone slurry, slurrying
The output terminal of device 140 is connected with oxidative absorption tower 110, adds the output terminal of pipeline 130 and pulping device 140 and/or and oxygen
Change absorption tower 110 to connect.
Wherein or the output terminal of addition pipeline 130 is connected with oxidative absorption tower 110.Add the input of pipeline 130
End connects with the first transfer pipeline 103 and/or is connected with temperature-reducing tower 100.
Further, spray equipment is equipped in temperature-reducing tower 100, spray equipment is arranged on the first transfer pipeline 103 and cooling
On the connected entrance that tower 100 connects.Spray equipment includes the nozzle for being arranged on 100 both sides of temperature-reducing tower.
Oxidant sprays flue gas from nozzle ejection through the first transfer pipeline 103, realizes better spraying effect.
Further, the system for being classified oxidative absorption formula flue gas desulfurization and denitrification further includes gypsum dehydration system, for by oxygen
Change the gypsum slurries formed in absorption tower 110 to discharge and be dehydrated.
Gypsum dehydration system includes gypsum cyclone 150, vacuum belt machine 151.Slurries deposition in oxidative absorption tower 110
It discharges from bottom, is classified by the concentration of gypsum cyclone 150, gypsum crystal afterwards, complete first separation, the calcium plaster after concentration
Liquid is carried out dehydrating again by vacuum belt machine 151, meets the requirements its water content, is store finally by Belt Conveying to gypsum
Storage 152.
Further, oxidative absorption tower 110 is generally bubble absorbing tower 110, connects in flue and bubble absorbing tower 110
Portion connects, and the smoke outlet of bubble absorbing tower 110 is equipped with demister 160, for reducing the droplet content in flue gas.
Embodiment two
As shown in Figs. 1-2, the present embodiment is a kind of specific embodiment of embodiment one, a kind of classification oxidative absorption formula cigarette
The system of desulfurization denitration, including temperature-reducing tower 100, oxidative absorption tower 110, lime stone slurry add-on system, oxidant addition system
System, gypsum dehydration system and air supply system are equipped with connection flue, flue gas warp between temperature-reducing tower 100 and oxidative absorption tower 110
Temperature-reducing tower 100 cools down, aoxidize after entered by flue in absorption tower, lime stone slurry add-on system and air supply system with
Oxidative absorption tower 110 connects, and air and lime stone slurry, oxidant add-on system and cooling are supplied into oxidative absorption tower 110
Tower 100 is connected by transfer pipeline, and stair oxidation is carried out to the flue gas in temperature-reducing tower 100, and oxidative absorption tower 110 is interior in air
Under effect, secondary oxidation is carried out to flue gas.
Temperature-reducing tower 100 includes smoke inlet, exhanst gas outlet, and oxidative absorption tower 110 includes gas inlet and smoke outlet, and flue gas goes out
Mouth is connected with gas inlet by connecting flue, and the flue gas in temperature-reducing tower 100 enters oxidative absorption tower 110 through connecting flue.Into
Mouth is connected with flue, and flue is equipped with booster fan 170, by the flue gas to be processed in flue from into cigarette
Mouth is introduced in temperature-reducing tower 100.
The oxidant add-on system includes oxidant storage tank 101, intermediate storage tank 102 and water supply installation, the first delivery pipe
Road 103 includes the first transfer pipeline leading portion and the first transfer pipeline back segment, oxidant storage tank 101 and intermediate storage tank 102 by the
One transfer pipeline leading portion connects, and centrifugal pump is set on the first transfer pipeline leading portion to provide power, intermediate storage tank 102 and cooling
It is connected between tower 100 by the first transfer pipeline back segment and outgoing line 104, the first transfer pipeline back segment is by intermediate storage tank 102
The mixed solution of interior oxidant is transported in temperature-reducing tower 100, and outgoing line 104 connects intermediate storage tank 102 and temperature-reducing tower 100
It connects, the liquid after the absorption in temperature-reducing tower 100 is imported into intermediate storage tank 102.104 shape of first transfer pipeline back segment and outgoing line
Into circulation line, circulation line is equipped with circulating pump, oxidation liquid is made to be cycled between intermediate storage tank 102 and temperature-reducing tower 100.
Water supply installation 142 is connected with intermediate storage tank 102 by pipeline, is supplied water into intermediate storage tank 102, is diluted from oxidant
Storage tank 101 enters the oxidant of intermediate storage tank 102.
By setting intermediate storage tank 102, a part of oxidant in oxidant storage tank 101 is transported to intermediate storage tank 102
Be made into the mixed solution of oxidant, then by circulation line by the mixed solution of oxidant in intermediate storage tank 102 and temperature-reducing tower 100
Between cycle, make the mixed solution of oxidant that constantly flue gas be absorbed and aoxidized, the mixing for making full use of oxidant is molten
Liquid.
The oxidant of storage is sodium chlorite and sodium hypochlorite in the oxidant storage tank 101.
Wherein, the mixed solution of oxidant can also be stored in oxidant storage tank 101 (such as sodium chlorite and sodium hypochlorite
Mixed solution), into intermediate storage tank 102, importation solution, is cycled, and is inputted in intermediate storage tank 102, is reduced to oxygen on demand
The pollution and waste of the mixed solution of oxidant in agent storage tank 101.At this moment, oxidant storage tank 101 adds equipped with oxidant
Add mouth, oxidant storage tank 101 is connected with water supply installation 142 by water supply pipe, by the oxidant dilution in oxidant storage tank 101
Into the solution of oxidant.On the one hand the mixed liquor of oxidant plays the role of cooling, on the other hand play oxidation, realizes
Simultaneous oxidation and the purpose of cooling.
NO and SO in 100 flue gas of temperature-reducing tower2NO is formed after oxidized mixed solution oxidation2And SO3, shape is absorbed by solution
Into sodium sulphate and sodium nitrate, this step is realized to NO and SO2Cooling simultaneous oxidation, greatly reduce the discharge of NO.
Flue gas after oxidation is transported to by connecting flue in oxidative absorption tower 110.
The lime stone slurry add-on system includes agstone adding set 141 and pulping device 140, and agstone adds
Feeder apparatus 141, water supply installation 142 are connected with pulping device 140, and agstone is added to by agstone adding set 141
In pulping device 140, water supply installation 142 adds in water (generally industry water) in pulping device 140, in pulping device 140
Form lime stone slurry.It is connected between pulping device 140 and oxidative absorption tower 110 by pipeline, pipeline is equipped with liquid pump, will
Lime stone slurry in pulping device 140 is transported in oxidative absorption tower 110.
Agstone adding set 141 is generally limestone powder bin, and powder is delivered to by feed belt after lime stone crushing
It is standby to deposit for use in storehouse.Slurrying case is normally at limestone powder bin lower part, the size exported by adjusting limestone powder bin, so as to
The concentration of lime stone slurry can be controlled.
The air supply system includes the air supply pipeline 120 and oxidation fan that are connected with oxidative absorption tower 110
121, the oxidation fan 121 is arranged on air supply pipeline 120, is delivered air in oxidative absorption tower 110.Air supplies
Pipeline 120 and the bottom of oxidative absorption tower 110 is answered to be connected, air is transported to oxidative absorption from the bottom of oxidative absorption tower 110
In tower 110.
It is not absorbed and not oxidized NOX、SOXEnter with flue gas through connecting flue in oxidative absorption tower 110, by lime
Stone absorbs and air oxidation forms gypsum slurries, this stage is mainly realized to SOXFixation form gypsum, also have to NOX
Preferable assimilation effect.
Gypsum dehydration system includes gypsum cyclone 150, vacuum belt machine 151.After gypsum slurries deposition in absorption tower
It discharges from bottom, is classified by the concentration of gypsum cyclone 150, gypsum crystal, complete first separation, the gypsum slurries after concentration
It is carried out dehydrating again by vacuum belt machine 151, meets the requirements its water content, stored finally by Belt Conveying to gypsum
Storehouse 152.
Said structure can also realize that the classification to flue gas absorbs, and improve to NOX、SOXAbsorption, be especially the increase in
After oxidant add-on system, it is significantly improved to the absorbability of NOx.
Further, on the basis of said structure, addition branch 130 on oxidant storage tank 101 is set, adds branch
130 other end is connected with the pulping device 140 of lime stone slurry add-on system, adds and liquid pump 131 is set on branch 130,
Liquid in oxidant storage tank 101 is transported to pulping device 140, is mixed with the lime stone slurry in pulping device 140, with stone
Lime stone slurries enter in oxidative absorption tower 110.By the mixing liquid collective effect of air and oxidant, two to flue gas are realized
Grade oxidation, further improves to the NO in flue gasX、SOXRemoval, improve the clean-up effect of flue gas.
Further, the outlet end for adding branch 130 is connected with slurrying bottom portion, after lime stone slurry is mixed with oxidant
It is sent into together in oxidative absorption tower 110.
The present embodiment is that a kind of classification oxidative absorption formula flue gas proposed on the basis of limestone-gypsum sulfur removal technology takes off
The cooler 100 in former limestone-gypsum sulfur removal technology may be employed in sulphur denitrating system, temperature-reducing tower 100, is set without newly-built denitration
Standby, it is a series of to solve the problems, such as that up-front investment is big, operating cost is high and takes up a large area etc., realizes flue gas desulfurization and denitrification
Integrated target.Classification oxidative absorption is carried out to flue gas, solves the problems, such as that denitrification efficiency is low in Practical Project.It adopts
By the use of sodium chlorite, sodium hypochlorite as oxidant, coordinate lime stone slurry desulphurization denitration, the NO in effectively removing flue gasX、SO2's
Under the premise of gas, the cost that oxidant in operational process uses is greatly reduced.
Lime stone slurry is absorbent, by the oxidation of level-one spray, cooling in cooler 100, in bubble absorbing tower 110
The problem of realizing to flue gas and desulfurizing and denitrifying, the cost of investment, operation is reduced for enterprise for secondary oxidation, absorption, for
The industrial applications of flue gas desulfurization and denitrification integral system and popularization are of great significance.
Embodiment three
As shown in Figs. 1-2, the present embodiment is the desulfurizing and denitrifying process carried out in the system of embodiment one and embodiment two,
Comprise the following steps
Flue gas enters from the smoke inlet of heat sink in heat sink；
Oxidant add-on system conveys oxidant into heat sink, carries out drop mild oxidation to flue gas, realizes to flue gas
Stair oxidation, the flue gas after oxidation enters oxidative absorption system；
Oxidative absorption system is aoxidized and absorbed to flue gas, realizes the secondary oxidation to flue gas.
Further, the oxidant of oxidant add-on system output is divided into two-way, is transported to intermediate storage device all the way,
The solution of certain density oxidant is configured in intermediate storage device, the solution of oxidant is in intermediate storage device and temperature-reducing tower
It is cycled between 100, the flue gas in absorption tower contacts with the solution of oxidant and by stair oxidation and cooling, the flue gas conveying after oxidation
To oxidative absorption tower 110；
Another way is transported to pulping device 140, and oxidative absorption tower 110 is transported to after being mixed with the lime stone slurry of preparation
Interior, oxidant is carried out flue gas secondary oxidation and is absorbed using lime stone slurry, realizes that absorption cleaning and secondary oxidation, desulfurization take off
Flue gas after nitre is discharged from smoke outlet, is formd gypsum slurries and is discharged and post-processed, obtains product.
Further, the oxidation mixed liquor is the mixed solution of sodium chlorite and sodium hypochlorite, wherein, sodium chlorite is dense
0.04~0.05mol/L, sodium hypochlorite concentration are spent for 0.15~0.20mol/L, and sodium hypochlorite is with sodium chlorite concentrations ratio 3.7
~4.0.
Further, the flow for aoxidizing agent storage device 101 to the mixed solution of intermediate storage device conveying oxidant is 2
~5m3/ h, the flow that the mixed solution of oxidant is conveyed into pulping device 140 are 10~15m3/h；Mixing in circulation line
Liquid inventory is 10~15m3/h。
Further, lime stone slurry is conveyed into oxidative absorption tower 110 less than after preset value in desulfuration efficiency, made
The solid content of lime stone is 20%~30% in slurries in sizing device 140；
Preferably, after desulfuration efficiency is less than 90%, lime stone slurry, slurrying dress are conveyed into oxidative absorption tower 110
The solid content for putting lime stone in the slurries in 140 is 20%~30%.
Heat sink is generally cooler 100, and oxidative absorption device is generally bubble absorbing tower 110.
Flue gas through booster fan 170 after being pressurized, into cooler 100.Oxidation agent storage device 101 divides two-way, and one
Road direction intermediate storage tank 102 conveys the mixed solution of oxidant, and intermediate storage tank 102 is connected with cooler 100 by circulation line, made
Oxidant cycles between intermediate storage tank 102 and cooler 100, cools down to NO, SO2 in the flue gas in cooler 100
And stair oxidation, the flue gas after stair oxidation are admitted in bubble absorbing tower 110, oxidation agent storage device is to intermediate storage device
The flow for conveying mixed solution is 2~5m3/ h,
Another way is transported in pulping device 140, and the flow that mixed solution is conveyed into pulping device is 10~15m3/ h,
Oxidant is mixed with the lime stone slurry in pulping device 140, is then sent to bubble absorbing tower 110, oxidant, lime stone
Mixed liquor contact and NO, SO2 in the flue gas after stair oxidation of slurries react, the flue gas after stair oxidation by secondary oxidation,
SOx after oxidation is simultaneously absorbed by lime stone slurry, forms gypsum slurries, from gypsum slurries discharges subsequently from pulping device 140
Reason forms gypsum product.
In addition, oxidation fan 121 also constantly bulging into absorption tower can send air, flowing and disturbance between gas-liquid are accelerated,
So that contact is more abundant, while the oxygen in air also plays the effect of oxidation NO, SO2 to a certain extent.So far, cigarette
The content of NOX, SO2 in gas have obtained effective reduction, after reducing wherein droplet content using demister 160, can pass through cigarette
Chimney 161 is discharged in air.
In cooler 100, bubble absorbing tower 110, NO, SO2 mainly occur to react as follows：
2NO+ClO2 -+ClO-+H2O→2NO3 -+2Cl-+H+
3SO2+ClO2 -+ClO-+3H2O→2SO4 2-+2Cl-+6H+
CaCO3+SO4 2-+2H+→CaSO4+H2O+CO2
Further, the oxidant aoxidized in agent storage device 101 is transported to cooler 100 and bubble absorbing tower simultaneously
In 110, oxidant carries out stair oxidation in cooler 100 to flue gas, and NO, SO2 in flue gas are oxidized into NO2, SO3,
In 110 inner oxidizing agent of bubble absorbing tower air is coordinated to carry out secondary oxidation to flue gas, SOx is inhaled by lime stone slurry
It receives, flue gas is most discharged after the processing of demister 160 afterwards, and the gypsum slurries after being absorbed in bubble absorbing tower 110 are taken off by gypsum
Become gypsum by-product after water system dehydration.
Wherein, in limestone slurry liquid preparing system, limestone powder bin is delivered to by feed belt after lime stone crushing
It in 141, under gravity, is dropped down onto under limestone powder in bottom pulping device 140, the water provided with water supply installation 142
(being generally general industry with water) is mixed and made into lime stone slurry, and lime stone slurry is sent into oxidation together with after oxidant mixing and is inhaled
It receives in tower.The size of feed flow is depending on the liquid level height of slurries in practical sulphur removal efficiency and oxidative absorption tower.
In the system of classification oxidative absorption formula flue gas desulfurization and denitrification, the oxidizing agent solution in intermediate storage tank 102 is centrifuging
With 15~20m under the action of pump3The flow velocity of/h is transported in cooler 100, and the inside both sides of cooler 100 be furnished with it is several
Nozzle, the mixed solution of oxidant can sufficiently be contacted in the form of atomization with flue gas, play drop mild oxidation flue gas in NO,
The effect of SO2,100 bottom of cooler are equipped with liquid outlet, and liquid outlet is connected with intermediate storage tank 102 by outgoing line 104, makes oxygen
Solution after change is returned in intermediate storage tank 102, forms circulation loop.
In system operation, the liquid height in intermediate storage tank 102 is no more than the 3/4 of itself height.
It can discharge from its bottom after slurries deposition after being reacted in bubble absorbing tower 110, be carried out by gypsum cyclone 150
Concentration and gypsum crystal classification, complete first separation, and the gypsum slurries after then concentrating are taken off again by vacuum belt machine 151
Water process makes its water content become gypsum by-product after meeting the requirements, finally by Belt Conveying to gypsum storage warehouse.Gypsum is used
Way extensively, has certain economic benefit.
The above is only the preferred embodiment of the utility model, and not the utility model is made in any form
Limitation although the utility model has been disclosed with preferred embodiment as above, is not limited to the utility model, any to be familiar with
The technical staff of this patent is not being departed from the range of technical solutions of the utility model, when the technology contents work using above-mentioned prompting
Go out a little change or be modified to the equivalent embodiment of equivalent variations, as long as being the content without departing from technical solutions of the utility model,
According to any simple modification, equivalent change and modification that the technical essence of the utility model makees above example, still belong to
In the range of the utility model.
Claims (10)
1. it is a kind of be classified oxidative absorption formula flue gas desulfurization and denitrification system, which is characterized in that including cooling oxidative system and with drop
The oxidative absorption system of warm oxidative system connection, cooling oxidative system are used to carry out stair oxidation to flue gas and cool down, and oxidation is inhaled
Receipts system is used to carry out secondary oxidation to the flue gas after oxidation and absorb, and cooling oxidative system includes heat sink and oxidant adds
Adding system, the oxidant add-on system are connected with heat sink, and oxidant is delivered to heat sink carries out level-one to flue gas
Oxidation.
A kind of 2. system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 1, which is characterized in that cooling
Device includes temperature-reducing tower and the first transfer pipeline for conveying cooling liquid to temperature-reducing tower, oxidant add-on system and first defeated
It send pipeline connection and/or is connected with temperature-reducing tower；
First transfer pipeline is equipped with power conveying device.
A kind of 3. system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 2, which is characterized in that oxidation
Agent add-on system includes oxidation agent storage device；
Oxidation agent storage device in storage oxidant be liquid oxidizer or be oxidant solution, oxidation agent storage device with
Between temperature-reducing tower by the first transfer pipeline connect, using the solution of liquid oxidizer or oxidant to the flue gas in temperature-reducing tower into
Row is aoxidized and cooled down；
Alternatively, heat sink further includes cooling liquid storaging device, cooling liquid storaging device passes through the first conveying with temperature-reducing tower
Pipeline connection, oxidation agent storage device connect with cooling liquid storaging device and/or connect with temperature-reducing tower and/or conveyed with first
Pipeline connection.
A kind of 4. system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 3, which is characterized in that oxidation
Agent add-on system further includes intermediate storage device, aoxidizes and is connected between agent storage device and temperature-reducing tower by the first transfer pipeline,
The intermediate storage device is arranged on the first transfer pipeline and is connected with the first transfer pipeline, and temperature-reducing tower is equipped with delivery line
Road, the outgoing line are connected with intermediate storage device.
5. a kind of system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 4, which is characterized in that intermediate
Storage device includes intermediate storage tank and water supply installation, and intermediate storage tank is arranged on the first transfer pipeline, and the water supply installation is in
Between storage tank connect, oxidant is diluted to intermediate storage tank water delivery, on the first transfer pipeline between intermediate storage tank and temperature-reducing tower
Line segments and outgoing line form circulation line, and circulation line is equipped with power set.
6. according to a kind of system of any classification oxidative absorption formula flue gas desulfurization and denitrifications of claim 3-5, feature exists
In oxidative absorption system includes oxidative absorption device and supplies system for supplying the oxidant of oxidant into oxidative absorption device
System, oxidant supply system convey oxidant to oxidative absorption system, and secondary oxidation is carried out to flue gas.
7. a kind of system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 6, which is characterized in that described
Oxidant supply system includes air supply system and/or for the oxidant in oxidant add-on system to be introduced oxidative absorption
The adding set of device, air supply system and/or adding set are connected with oxidative absorption device；
The air supply system includes the air supply pipeline and oxidation fan that are connected with oxidative absorption device, the oxidation wind
Machine is arranged on air supply pipeline.
8. a kind of system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 7, which is characterized in that described
Adding set includes addition pipeline, and the addition pipeline is arranged between oxidant add-on system and oxidative absorption device, is used for
Oxidant in oxidant add-on system is transported to oxidative absorption device.
A kind of 9. system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 8, which is characterized in that addition
Pipeline be arranged on first transfer pipeline or for the addition branch that connects of oxidation agent storage device, the addition branch
Output terminal be connected with oxidative absorption device, it is described addition branch road be equipped with liquid pump.
A kind of 10. system for being classified oxidative absorption formula flue gas desulfurization and denitrification according to claim 6, which is characterized in that institute
Stating oxidative absorption device includes oxidative absorption tower and supplies system for conveying the lime white of lime stone slurry into oxidative absorption tower
System, oxidant supply system are connected with lime white supply system and/or with oxidative absorption tower.
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| CN107694314A (en) * | 2017-10-18 | 2018-02-16 | 大唐南京发电厂 | A kind of system and technique for being classified oxidative absorption formula flue gas desulfurization and denitrification |
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