CN205832882U - A kind of equipment of fume treatment - Google Patents
A kind of equipment of fume treatment Download PDFInfo
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- CN205832882U CN205832882U CN201620822734.2U CN201620822734U CN205832882U CN 205832882 U CN205832882 U CN 205832882U CN 201620822734 U CN201620822734 U CN 201620822734U CN 205832882 U CN205832882 U CN 205832882U
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- electric cleaner
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- waste water
- pipeline
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- 239000003517 fume Substances 0.000 title claims abstract description 27
- 239000002351 wastewater Substances 0.000 claims abstract description 141
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 108
- 230000023556 desulfurization Effects 0.000 claims abstract description 103
- 239000007788 liquid Substances 0.000 claims abstract description 94
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 59
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 31
- 238000000889 atomisation Methods 0.000 claims description 34
- 239000006228 supernatant Substances 0.000 claims description 32
- 239000000779 smoke Substances 0.000 claims description 25
- 238000005516 engineering process Methods 0.000 claims description 18
- 238000004065 wastewater treatment Methods 0.000 claims description 18
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 15
- 229910052717 sulfur Inorganic materials 0.000 claims description 15
- 239000011593 sulfur Substances 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 13
- 238000005507 spraying Methods 0.000 claims description 8
- 238000001556 precipitation Methods 0.000 claims description 7
- 238000005189 flocculation Methods 0.000 claims description 6
- 230000016615 flocculation Effects 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 239000004744 fabric Substances 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims 1
- 238000007906 compression Methods 0.000 claims 1
- 239000000428 dust Substances 0.000 abstract description 46
- 239000008187 granular material Substances 0.000 abstract description 12
- 230000008878 coupling Effects 0.000 abstract description 2
- 238000010168 coupling process Methods 0.000 abstract description 2
- 238000005859 coupling reaction Methods 0.000 abstract description 2
- 239000003546 flue gas Substances 0.000 description 82
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 79
- 238000000034 method Methods 0.000 description 39
- 230000008569 process Effects 0.000 description 27
- 239000002245 particle Substances 0.000 description 19
- 239000012717 electrostatic precipitator Substances 0.000 description 17
- 239000013618 particulate matter Substances 0.000 description 17
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 16
- 239000007787 solid Substances 0.000 description 16
- 239000007921 spray Substances 0.000 description 14
- 230000000694 effects Effects 0.000 description 8
- 230000005611 electricity Effects 0.000 description 8
- 238000011010 flushing procedure Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 239000002956 ash Substances 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 239000000725 suspension Substances 0.000 description 6
- 241000196324 Embryophyta Species 0.000 description 5
- 235000019738 Limestone Nutrition 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000003245 coal Substances 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000006028 limestone Substances 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- 238000005054 agglomeration Methods 0.000 description 4
- 230000002776 aggregation Effects 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 235000019504 cigarettes Nutrition 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 239000013505 freshwater Substances 0.000 description 4
- 229910001385 heavy metal Inorganic materials 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000013043 chemical agent Substances 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 239000012716 precipitator Substances 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical group [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 2
- TVEXGJYMHHTVKP-UHFFFAOYSA-N 6-oxabicyclo[3.2.1]oct-3-en-7-one Chemical compound C1C2C(=O)OC1C=CC2 TVEXGJYMHHTVKP-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 235000013339 cereals Nutrition 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000009297 electrocoagulation Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 229910052928 kieserite Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 239000004531 microgranule Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- -1 pH value is 4.5~6.5 Substances 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000001089 thermophoresis Methods 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000009692 water atomization Methods 0.000 description 1
- 239000000080 wetting agent Substances 0.000 description 1
Abstract
This utility model relates to fume treatment field, disclose the equipment of a kind of fume treatment, this equipment includes electric cleaner (2), desulfurization unit (3), wet cottrell (4), this equipment also includes atomising device (6) and waste water separator (7), the wastewater outlet of desulfurization unit (3) is connected with the entrance of waste water separator (7), the liquid outlet of described waste water separator (7) is connected with the water inlet of atomising device (6), and the outlet of atomising device (6) is connected with the pipeline of electric cleaner (2) upstream.Use equipment of the present utility model, by electric cleaner and the coupling of wet cottrell, it is possible to be effectively improved the removal efficiency of dust granules thing, it is also possible to realize the zero-emission of waste water.
Description
Technical field
This utility model relates to fume treatment field, in particular it relates to the equipment of a kind of fume treatment.
Background technology
Particulate matter is the primary pollutant of current China city atmospheric environment, and China's flue dust 90% comes spontaneous combustion coal, Qi Zhongchao
Fine particle (PM2.5) pollution problem more serious.Although the efficiency of dust collection of existing dust arrester is up to more than 99%, but this
A little cleaner units are relatively low to the capture rate of superfine particulate matter, still have substantial amounts of superfine particulate matter to enter in air, with the quantity of granule
Meter can reach more than the 90% of fly ash granule sum.The concentration of emission of particulate matter is limited by the up-to-date environmental protection standard that country promulgates
Bring up to 50mg/Nm3, this proposes challenge, existing electrostatic precipitator greatly to China's coal-fired plant flue gas emission control
Mostly it is unable to reach this standard.Use wet cottrell, for SO3, hydrargyrum and desulfurated plaster there is preferable removal effect,
But superfine particulate matter still needed to be improved further removal efficiency.
All there is waste water handling problem in the most traditional limestone-gypsum wet desulfuration technique and wet static dedusting technique.
The impurity of heat-engine plant desulfurized waste water from flue gas and the limestone of desulfurization, mainly include float, oversaturated sulphite,
Sulfate and heavy metal, be the most much the first kind pollutant requiring in national environmental standard to control.Generally desulfurization wastewater
In faintly acid, pH value is 4.5～6.5, and suspension content is generally 1～10g/L, containing Cl-、F-、SO42-、Ca2+、Mg2+Deng cloudy
Cation and micro heavy ion, directly environment can be impacted by outer row.General employing chemistry adding method thereof processes, this method
Technology maturation, but owing to wastewater treatment capacity is big, need substantial amounts of chemical agent, investment and operating cost are higher.Wet electrostatic removes
The waste water of dirt device generally enters desulfurization wastewater treatment system.
At present, the control technological development direction of superfine particulate matter predominantly arranges pretreatment before conventional dust removal equipment and arranges
Execute so that it is by being removed after physically or chemically acting on long great achievement larger particles, including acoustic agglomeration, electrocoagulation, magnetic coagulation,
Chemical agglomeration, steam phase transforming etc..Chemical agglomeration technology can neither change normal production conditions, does not the most change existing electric precipitation
Under conditions of equipment and operating parameter, it is effectively improved electric dust-removing equipment to fine grain removal efficiency, but in the agglomerator sprayed into,
In addition to containing binding agent and wetting agent, also need to add inorganic additives and pH value regulator (such as phosphoric acid), and fresh water (FW) consumption is relatively
Greatly.
Therefore, the equipment developing the superfine particulate matter of a kind of environmental protection and the process of waste water is very important.
Utility model content
In order to overcome prior art, in fume treatment, in dust granules thing, superfine particulate matter removal efficiency is low and waste water
Processing cost is high, the defect of inadequate environmental protection, and this utility model provides the equipment of a kind of fume treatment, uses of the present utility model
Equipment, by electric cleaner and the coupling of wet cottrell, it is possible to be effectively improved the removal efficiency of dust granules thing, also may be used
To realize the zero-emission of waste water.
Specifically, this utility model provides the equipment of a kind of fume treatment, and this equipment includes electric cleaner, desulfurization list
Unit, wet cottrell, the fume emission mouth of described electric cleaner is connected by the smoke inlet of pipeline with described desulfurization unit
Connecing, the exhanst gas outlet of described desulfurization unit is connected with the smoke inlet of described wet cottrell by pipeline, and this equipment is also
Including atomising device and waste water separator, the wastewater outlet of desulfurization unit is connected with the entrance of waste water separator, described useless
The liquid outlet of water separation device is connected with the water inlet of atomising device, the outlet of atomising device and the pipeline of electric cleaner upstream
Connect.
Preferably, the liquid outlet of described waste water separator includes supernatant liquid outlet and lower floor's liquid outlet, described
Supernatant liquid outlet is connected with the sulfur removal technology water inlet of desulfurization unit, described lower floor liquid outlet and the water inlet of atomising device
Connect.
Preferably, described supernatant liquid outlet and described wet cottrell wastewater outlet all with desulfurization unit take off
Sulfur fresh water (FW) entrance connects.
Preferably, the equipment of described fume treatment also includes wastewater treatment equipment, the liquid discharge of described waste water separator
Mouth includes that supernatant liquid outlet and lower floor's liquid outlet, the outlet of described supernatant liquid are connected with the water inlet of described atomising device,
Described lower floor liquid outlet is connected with the entrance of described waste water separator, the outlet of described wastewater treatment equipment and described wet type
The water inlet of electrostatic precipitator connects, and the wastewater outlet of described wet cottrell connects with the entrance of described waste water separator
Connect.
Preferably, described atomising device is blast injection atomising device.
Preferably, described waste water separator is gravity-type solid-liquid separator.
Preferably, described wastewater treatment equipment is chemical flocculation precipitation device.
Preferably, described electric cleaner is electrostatic precipitator and/or electrostatic fabric filter.
Preferably, described desulfurization unit is wet desulphurization device.
Preferably, the position that the outlet of described atomising device is connected with the pipeline of electric cleaner upstream and described electric cleaner
The distance of entrance be not less than 5 meters.
Preferably, described equipment also includes that boiler, the pipeline of described electric cleaner upstream are between boiler and electric cleaner
Pipeline, and there is no it between position and the electric cleaner 2 of the pipeline that sprays into electric cleaner upstream of the drop after described atomization
Its equipment.
This utility model combines the feature of electric cleaner, wet desulphurization and wet cottrell, it is achieved that three's
Organically combine, the most effectively solve desulfurization and the wastewater problem of wet cottrell, realize wastewater zero discharge by circulating and recovering,
Achieve the gathering of superfine particulate matter and grow up, making granular material discharged concentration less than 5mg/Nm3, it is truly realized dust granules thing
Near-zero release.Specifically, this utility model is by spraying into partial desulfurization waste water in the pipeline of electric cleaner upstream, it is not necessary to
Increase any assistant medicament, neither change normal production conditions, the most do not change existing electric dust-removing equipment structurally and operationally parameter, just
The electric dust-removing equipment removal efficiency to dust granules thing can be improved；Meanwhile, this partial desulfurization waste water sprays into the upper of electrostatic precipitator
Evaporating completely in the pipeline of trip, the pollutant in waste water are converted into solid and separate out, and with the dust in flue gas by electric precipitation
Device traps.And another part desulfurization wastewater or enter desulfurization unit as sulfur removal technology water and recycle, or through waste water
Realize recycling as the flushing water of wet cottrell after processing means purified treatment, really realize wastewater zero discharge
With the near-zero release of dust granules thing, reduce operating cost.
The principle of the near-zero release that this utility model is capable of dust granules thing is probably: after the atomization of partial desulfurization waste water
Spray into the pipeline of the upstream of electric cleaner, on the one hand cause flue-gas temperature to reduce, under the ratio resistance of dust after desulfurization wastewater evaporation
Fall, meanwhile, the inorganic salts material of precipitation is (such as CaCl2·2H2O、MgSO4·H2O, NaCl) also can suitably reduce dust than electricity
Resistance, this removal efficiency being all conducive to improving electrostatic precipitator；On the other hand, after flue gas spraying into water smoke, fine particle is had one
Fixed agglomeration, in supersaturated vapor environment, steam is with PM2.5Microgranule is that the nuclei of condensation undergo phase transition, and makes particle size increase
Greatly, quality increases, and produces the effect of diffusion and thermophoresis simultaneously, promotes Particles transport motion and mutually collides, making PM2.5Group
Gather and grow up.Fine water-spray can produce trapping effect to respirable dust, and dust is all increased by the moistening rear particle diameter of water smoke, quality,
And become easily to be removed, even if water smoke is not charged, the humidification uniquely relying on water smoke just can promote the reunion of subparticle, carries
The efficiency of dust collection of high follow-up electric cleaner.
Other features and advantages of the utility model will be described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to offer and is further appreciated by of the present utility model, and constitutes a part for description, with following
Detailed description of the invention be used for explaining this utility model together, but be not intended that restriction of the present utility model.In the accompanying drawings:
Fig. 1 be the one of the equipment of fume treatment of the present utility model preferred embodiment；
Fig. 2 is another preferred embodiment of the equipment of fume treatment of the present utility model.
Description of reference numerals
1 boiler 2 electric cleaner
3 desulfurization unit 4 wet cottrells
5 chimney 6 atomising devices
7 waste water separator 8 wastewater treatment equipments
A fuel B desulfurization wastewater
C supernatant liquid D lower floor liquid
E compressed air F dust waste water
G Gypsum Fibrosum and body refuse H flushing water
I solid residue
Detailed description of the invention
Hereinafter detailed description of the invention of the present utility model is described in detail.It should be appreciated that it is described herein
Detailed description of the invention is merely to illustrate and explains this utility model, is not limited to this utility model.
The end points of scope disclosed in this article and any value are not limited to this accurate scope or value, these scopes or
Value should be understood to the value comprised close to these scopes or value.For numerical range, between the endpoint value of each scope, respectively
Between endpoint value and the single point value of individual scope, and can obtain one or more between single point value with combination with one another
New numerical range, these numerical rangies should be considered the most specifically to disclose.
This utility model provides the equipment of a kind of fume treatment, and this equipment includes electric cleaner 2, desulfurization unit 3, wet type
Electrostatic precipitator 4, the fume emission mouth of described electric cleaner 2 is connected with the smoke inlet of described desulfurization unit 3 by pipeline, institute
The exhanst gas outlet stating desulfurization unit 3 is connected with the smoke inlet of described wet cottrell 4 by pipeline, and this equipment also includes
Atomising device 6 and waste water separator 7, the wastewater outlet of desulfurization unit 3 is connected with the entrance of waste water separator 7, described useless
The liquid outlet of water separation device 7 is connected with the water inlet of atomising device 6, the outlet of atomising device 6 and electric cleaner 2 upstream
Pipeline connects.
Flue gas sequentially passes through electric cleaner 2, desulfurization unit 3, wet cottrell 4, the desulfurization produced by desulfurization unit 3
Waste water obtains liquid and solid residue through waste water separator 7, and the liquid obtained by waste water separator 7 is through atomization dress
After putting the atomization of 6 atomized after drop, the drop after described atomization is sprayed into the pipeline of the upstream of electric cleaner 2.
According to this utility model one preferred embodiment, as it is shown in figure 1, the liquid discharge of described waste water separator 7
Mouth includes supernatant liquid outlet and lower floor's liquid outlet, the outlet of described supernatant liquid and the sulfur removal technology water inlet of desulfurization unit 3
Connecting, described lower floor liquid outlet is connected with the water inlet of atomising device 6.It is highly preferred that the outlet of described supernatant liquid is with described
The wastewater outlet of wet cottrell 4 is all connected with the sulfur removal technology water inlet of desulfurization unit 3.
The liquid that waste water separator 7 obtains includes supernatant liquid and lower floor's liquid, and described supernatant liquid is as desulfurization work
Skill water enters desulfurization unit 3, and described lower floor liquid enters in atomising device 6.It is highly preferred that described supernatant liquid and and described wet
The dust waste water that formula electrostatic precipitator 4 produces all enters desulfurization unit 3 as sulfur removal technology water.
According to another preferred embodiment of the present utility model, as in figure 2 it is shown, the equipment of described fume treatment also wraps
Including wastewater treatment equipment 8, the liquid outlet of described waste water separator 7 includes supernatant liquid outlet and lower floor's liquid outlet, institute
State supernatant liquid outlet to be connected with the water inlet of described atomising device 6, described lower floor liquid outlet and described waste water separator 8
Entrance connect, the outlet of described wastewater treatment equipment 8 is connected with the water inlet of described wet cottrell 4, described wet type
The wastewater outlet of electrostatic precipitator 4 is connected with the entrance of described waste water separator 7.
The liquid that waste water separator 7 obtains includes supernatant liquid and lower floor's liquid, and described supernatant liquid enters atomization dress
Putting 6, lower floor's liquid enters waste water separator 8 and carries out purified treatment, and using the water after purified treatment as wet static dedusting
The flushing water of device 4.
In this utility model, described atomising device 6 can be blast injection atomising device, and the condition of atomization includes
Pressure can be 0.3-0.5MPa, and the liquid drop speed after atomising device is atomized can be 30-50m/s.Compressed air E is used for carrying
Medium for liquid water atomization.
In this utility model, described waste water separator 7 can be gravity-type solid-liquid separator.Described waste water separates dress
Put 7 one aspects and float is had filtration, on the other hand, it is possible to achieve waste water is efficiently separated.Described waste water separates dress
Put 7 and can realize three layers of separating effect according to density difference, including supernatant liquid, lower floor's liquid and solid residue.Wherein, on
Layer liquid and the subnatant decorum liquid that referred to as waste water separator 7 obtains.The density of supernatant liquid is less than 1010kg/m3, excellent
Elect 1000-1009kg/m as3；Containing a small amount of particulate matter and float in lower floor's liquid, density can be 1010-1050kg/m3。
The bottom is solid residue, and described solid residue can include Gypsum Fibrosum and the body refuse G of solid-state.
According to one of the present utility model preferred embodiment, described supernatant liquid C and described wet cottrell 4
Produce dust waste water F all as sulfur removal technology water enter desulfurization unit 3 mode there is no particular limitation, such as can first by
Described supernatant liquid C and described dust waste water F mixes in entering the pipeline before desulfurization unit 3, it is also possible to pass through respectively into
Mouth entrance desulfurization unit 3.Correspondingly, can set on the pipeline of sulfur removal technology water between desulfurization unit 3 and waste water separator 7
Put the entrance of described dust waste water, it is also possible to the pipeline of the sulfur removal technology water between wet cottrell 4 and desulfurization unit 3
On the entrance of described supernatant liquid is set, or between desulfurization unit 3 and waste water separator 7 pipeline of sulfur removal technology water with wet
The pipeline of the sulfur removal technology water between formula electrostatic precipitator 4 and desulfurization unit 3 be arranged in parallel.
According to another preferred embodiment of the present utility model, desulfurization wastewater D and wet type that desulfurization unit 3 produces are quiet
There is no particular limitation for the mode of the dust waste water B entrance waste water separator 7 that electric cleaner 4 produces, such as can be first by institute
State desulfurization wastewater and described dust waste water to mix in entering the pipeline before waste water separator 7, it is also possible to pass through respectively into
Mouth enters waste water separator 7.Correspondingly, can arrange on the pipeline between desulfurization unit 3 and waste water separator 7 described
The entrance of dust waste water, it is also possible to described desulfurization is set on the pipeline between wet cottrell 4 and waste water separator 7
Pipeline between the entrance of waste water, or desulfurization unit 3 with waste water separator 7 separates with waste water with wet cottrell 4
Pipeline between device 7 be arranged in parallel.
In this utility model, described wastewater treatment equipment 8 can be chemical flocculation precipitation device.Preferred according to one
Embodiment, the liquid that waste water separator 7 obtains includes that supernatant liquid and lower floor's liquid, lower floor's liquid enter waste water and separates dress
Put 8 and carry out purified treatment, be purified the water after process and solid residue I, and using the water after purified treatment as wet electrostatic
The flushing water of cleaner unit 4.Purified treatment includes using chemical agent to carry out flocculation sediment, and the condition of flushing water includes that pH value is
6.8-7.5, solid suspension < 100ppm.
In this utility model, described electric cleaner 2 can be connected with boiler 1, and described boiler 1 is those skilled in the art
Known, do not repeat them here.
In this utility model, described flue gas can be the various flue gases needing to remove dust granules thing, can be various
The flue gas that fuel A (such as coal) burns, such as, can be the flue gas from boiler 1 without any process, such as, can come
From the flue gas of boiler of power plant, it is also possible to be the flue gas from steel-making boiler.Described flue gas can also be the cigarette processed through denitration
Gas.
According to this utility model one preferred embodiment, described equipment also includes being arranged on electric cleaner 2 upstream
Denitrification apparatus.Flue gas was carrying out denitration process before electric cleaner 2.The routine that technique is this area that described denitration processes
Select.Such as, described denitration processes and can be selected from low nitrogen burning, SCR (SCR) technique and selective non-catalytic
At least one in reduction denitration (SNCR) technique.Concrete equipment and condition are well known to those skilled in the art, at this not
Repeat again.According to preferred a kind of embodiment, flue gas produces in boiler 1, is passed through electric cleaner after denitration processes
2.There is no particular limitation for the component of flue gas and flow, can be the conventional selection of this area, not repeat them here.
In this utility model, there is no particular limitation for the kind of described electric cleaner 2, can be the conventional choosing of this area
Select.Such as, described electric cleaner 2 can be electrostatic precipitator and/or electrostatic fabric filter, and described electrostatic precipitator is usually dry type
Electrostatic precipitator.The operation flue-gas temperature of described electric cleaner 2 can be 95-160 DEG C.
In this utility model, described desulfurization unit 3 can be wet desulphurization device, the kind of described wet desulphurization device
Can be the conventional selection of this area with structure and service condition.Such as, described wet desulphurization device can include connecting successively
Logical pulping system, absorption tower and gypsum dehydration system.The fume emission mouth of described electric cleaner 2 is by pipeline and described desulfurization
The smoke inlet connection of unit 3 refers to be connected with the smoke inlet on the absorption tower of wet method release unit.When upstream, absorption tower cloth
When being equipped with concentration tower, it is connected the flue gas referring to the concentration tower with wet desulphurization device with the smoke inlet of described desulfurization unit 3
Entrance connects.
In this utility model, the composition of the desulfurization wastewater B that described desulfurization unit 3 produces is ripe by those skilled in the art
Knowing, the most described desulfurization wastewater is generally in faintly acid, and pH value is 4.5-6, and suspension content is 1-10g/L, containing Cl-、F-、
SO4 2-、Ca2+、Mg2+And micro heavy ion.
In this utility model, described wet cottrell 4 is the conventional selection of this area.Such as can use flexibility
Pole plate dedusting, deashing is by the full surface uniform water film gravity flow of pole plate.Preferably, the dedusting that described wet cottrell 4 produces
Waste water F contains a small amount of fine dust and Gypsum Fibrosum drop.
In this utility model, the drop after described atomization sprays into the position of the pipeline of electric cleaner upstream can be bigger
In the range of change, remove as long as heat contained by flue gas can be utilized not have liquid water to enter electricity the droplet evaporation after atomization and guarantee
Dirt device 2.Drop after the most described atomization sprays into the position of the pipeline of electric cleaner upstream and entering of described electric cleaner 2
The distance of mouth is not less than 5 meters (preferably 5-10 rice).Preferably, the flow velocity of flue gas is about 10-15 meter per second, after described atomization
The drop time of staying in the duct is not less than 0.5 second (preferably 0.5-0.8 second).
According to this utility model, the time of staying in the duct of the drop after described atomization refers to the drop after atomization from spray
The pipeline entering electric cleaner upstream starts to electric cleaner 2 the required time.The pipeline of electric cleaner 2 upstream refers to
Flue gas enters the pipeline of electric cleaner 2, the pipeline being i.e. connected with electric cleaner 2 entrance.According to one preferred embodiment, institute
Stating the pipeline of electric cleaner upstream is that the drop after the pipeline between boiler 1 and electric cleaner 2, and described atomization sprays into electricity and removes
Miscellaneous equipment is not had between position and the electric cleaner of the pipeline of dirt device upstream.
In this utility model, the straying quatity of the drop after described atomization can change in a big way, this straying quatity
Can determine according to the temperature of flue gas.Flue-gas temperature before routine Precipitator is generally at 120-150 DEG C at present,
Drop after atomization can evaporate after spraying into, and carries out heat exchange with flue gas, and flue-gas temperature reduces 8-15 DEG C.Preferably implement according to one
Mode, the straying quatity of the drop after described atomization makes the inlet temperature of electric cleaner 2 be not less than 105 DEG C, more preferably 120-
130℃。
In this utility model, electric cleaner 2 outlet flue gas enter desulfurization unit 3 carry out desulfurization, desulfuration efficiency up to
99%, SO in the flue gas after desulfurization2Concentration is less than 35mg/Nm3.Flue gas after desulfurization enters in wet cottrell 4
Carry out ultimate process, can be by the Gypsum Fibrosum carried in flue gas, fine grained, SO3And the heavy metal removing such as Hg.After tested, described wet type
The outlet particle concentration of electrostatic precipitator 4 is less than 5mg/Nm3, it is achieved the near-zero release of dust granules thing.
According to one of the present utility model preferred embodiment, wet cottrell 4 is with chimney 5 by pipeline even
Connect.Flue gas after wet cottrell 4 processes finally is discharged from chimney 5.
Hereinafter by embodiment, this utility model will be described in detail.
In following example, particle concentration, flue gas flow, smoke moisture, flue-gas temperature etc. are all according to coal-fired power plant
Universal testing method and instrument record, with specific reference to GB/T 13931-2002 (electric precipitator performance method of testing).
In embodiment and comparative example, enter in the flue gas of electric cleaner 2 containing following components (representing with volume content):
CO2Content 14.34%, O2Content 3.25%, N2Content 73.47%, SO2Content 0.06%, H2The content of O
8.61%, remaining is the foreign gas of trace.
Electric cleaner 2 is electrostatic precipitator, and desulfurization unit 3 is wet desulphurization device, and wet cottrell 4 is purchased from China
Energy-saving and emission-reduction company limited, atomising device 6 is blast injection atomising device, and waste water separator 7 divides for gravity-type solid-liquid
From device, wastewater treatment equipment 8 is chemical flocculation precipitation device.
Embodiment 1
As it is shown in figure 1, by boiler 1, electric cleaner 2, desulfurization unit 3, wet cottrell 4, chimney 5, atomising device 6
Being attached with waste water separator 7, wherein, the exhanst gas outlet of boiler 1 is connected with the smoke inlet of electric cleaner 2, described electricity
The fume emission mouth of cleaner unit 2 is connected with the smoke inlet of described desulfurization unit 3 by pipeline, the flue gas of described desulfurization unit 3
Outlet is connected by the smoke inlet of pipeline with described wet cottrell 4, the exhanst gas outlet of wet cottrell 4 and cigarette
Chimney 5 connects.The wastewater outlet of desulfurization unit 3 and the wastewater outlet of described wet cottrell 4 all with waste water separator 7
Entrance connects, and the supernatant liquid outlet of described waste water separator 7 is connected with the sulfur removal technology water inlet of desulfurization unit 3, lower floor
Liquid outlet is connected with the water inlet of atomising device 6, and the outlet of atomising device 6 is connected with the pipeline of electric cleaner 2 upstream.Described
The exhanst gas outlet of wet cottrell 4 is connected with chimney 5.
Power is the unit of 300MW, and fuel A (specially coal) burns in boiler 1 and produces flue gas, processes through denitration
Rear entrance electric cleaner 2, the condition that denitration processes includes: using SCR technique, catalyst is vanadium Titanium series catalyst, temperature range
For 290-400 DEG C.
The entrance flue gas temperature of electric cleaner 2 about 130 DEG C, flue gas flow about 1,100,000 Nm3/ h, the particulate matter in flue gas is dense
Degree is 12g/Nm3.The particle concentration of the flue gas after electric cleaner 2 processes is 21mg/Nm3.After electric cleaner 2 processes
Flue gas enters desulfurization unit 3 and processes.SO in desulfurization unit 3, in flue gas2React with lime stone slurry, thus SO2From
Flue gas removes.From absorption tower discharge lime stone slurry through cyclonic separation, wash and be dehydrated after obtain Gypsum Fibrosum, produce simultaneously
Desulfurization wastewater B.The pH value of desulfurization wastewater B is 5.2, and suspension content is 6.3g/L, containing Cl in described desulfurization wastewater-、F-、
SO4 2-、Ca2+、Mg2+.The weight of desulfurization wastewater D about 3.8 tons.
Flue gas desulfuration efficiency after desulfurization unit 3 processes has reached 99%.Flue gas after desulfurization processes enters wet type
Electrostatic precipitator 4.Described wet cottrell 4 uses flexible plate dedusting, and deashing leans on the full surface uniform water film of pole plate certainly
Stream.The dust waste water F that described wet cottrell 4 produces contains a small amount of fine dust and Gypsum Fibrosum drop.Wet cottrell 4
The dust waste water F about 1.2 tons produced.
Desulfurization wastewater B, after the separation of waste water separator 7, realizes three layers of separating effect according to density difference, is divided into
Supernatant liquid, lower floor's liquid and solid residue.Wherein, lower floor's liquid F density about 1030kg/m3, weight about 3 tons, water temperature is about
40 DEG C, enter in atomising device 6 and be atomized under the effect of compressed air E, atomizing pressure about 0.4MPa, the liquid drop speed after atomization
For 40m/s.Drop after atomization sprays into the upstream line of electric cleaner 2, and spraying into a little distance with electric cleaner 2 is 5 meters, flue gas
Flow velocity about 10m/s, the time of staying in the duct of the drop after atomization is 0.5 second.
Through measuring and calculating, lower floor liquid F through atomization after enter electric cleaner 2 upstream line evaporate completely after, in pipeline
Smoke moisture is increased to 9.13% by 8.61%, and flue-gas temperature is reduced to 124 DEG C.Flue gas is in undersaturated condition, higher than acid dew
Point temperature (acid dew-point temperature about 80-95 DEG C), will not produce corrosion to flue and electric cleaner, therefore, there is no need to spray waste water
After access point, pipeline and cleaner unit carry out reforming processing.Meanwhile, the increase of smoke moisture and the reduction of flue-gas temperature, also reduce electricity
The ratio resistance that cleaner unit is mellow lime, is conducive to improving efficiency of dust collection.It addition, because of the reduction of flue-gas temperature and the increasing of humidity of flue gas
Add, decrease the water consumption of FGD (flue gas desulfurization) system.(heavy metal, impurity and each additionally, solids in desulfurization wastewater
Plant slaine etc.) it is suspended in together with ash in flue gas and enters electric cleaner with flue gas, caught by electrode in electric cleaner, with
Ash outer row together, because in desulfurization wastewater, amount of solid and various metal salt concentration are less, physical property and comprehensive utilization to ash will not be produced
Raw impact.
The flue gas that wet cottrell 4 processed discharges through chimney 5, the supernatant liquid C that waste water separator 7 produces
(density 1003kg/m3) and the dust waste water F mixing that produces of wet cottrell 4 after as the sulfur removal technology of desulfurization unit 3
Water, it is achieved that recycle.It addition, collect Gypsum Fibrosum and the body refuse G of the solid-state that waste water separator 7 produces, carry out subsequent treatment,
Solid-state Gypsum Fibrosum is transported to stockyard, body refuse is abandoned.
After tested, outlet particle concentration (dust concentration) the about 21mg/Nm of electric cleaner 23, the outlet of desulfurization unit 3
Particulate matter (carrying containing Gypsum Fibrosum) concentration about 16mg/Nm3, the outlet particle concentration about 4mg/Nm of wet cottrell 43, it is achieved
The near-zero release of dust (＜ 5mg/Nm3).Sprayed into by cycling utilization of wastewater and pipeline, desulfurization unit and wet static dedusting
Device, without arranging outside waste water, is truly realized wastewater zero discharge.
Embodiment 2
Use the equipment of fume treatment same as in Example 1.
The method using fume treatment same as in Example 1, except for the difference that, under waste water separator 7 isolated
The density of layer liquid F is 1010kg/m3, the atomizing pressure in atomising device 6 is about 0.3MPa, and the liquid drop speed after atomization is about
For 30m/s, the drop after atomization sprays into the upstream line of electric cleaner 2, and spraying into a little distance with electric cleaner 2 is 8 meters, flue gas
Flow velocity about 12m/s, the time of staying in the duct of the drop after atomization is 0.6 second.Lower floor liquid F enters electricity after atomization and removes
After the upstream line of dirt device 2 is evaporated completely, the smoke moisture in pipeline is increased to 9.18% by 8.61%, and flue-gas temperature is reduced to
120℃。
After tested, outlet particle concentration (dust concentration) the about 21mg/Nm of electric cleaner 23, the outlet of desulfurization unit 3
Particulate matter (carrying containing Gypsum Fibrosum) concentration about 12mg/Nm3, the outlet particle concentration about 3mg/Nm of wet cottrell 43, it is achieved
The near-zero release of dust (＜ 5mg/Nm3)。
Embodiment 3
Use the equipment of fume treatment same as in Example 1.
The method using fume treatment same as in Example 1, except for the difference that, under waste water separator 7 isolated
The density of layer liquid F is 1050kg/m3, the atomizing pressure in atomising device 6 is about 0.5MPa, and the liquid drop speed after atomization is about
For 50m/s, the drop after atomization sprays into the upstream line of electric cleaner 2, and spraying into a little distance with electric cleaner 2 is 10 meters, cigarette
Gas velocity about 12m/s, the time of staying in the duct of the drop after atomization is 0.8 second.Lower floor liquid F enters electricity after atomization
After the upstream line of cleaner unit 2 is evaporated completely, the smoke moisture in pipeline is increased to 9.02% by 8.61%, and flue-gas temperature reduces
To 125 DEG C.
After tested, outlet particle concentration (dust concentration) the about 21mg/Nm of electric cleaner 23, the outlet of desulfurization unit 3
Particulate matter (carrying containing Gypsum Fibrosum) concentration about 18mg/Nm3, the outlet particle concentration about 4.5mg/Nm of wet cottrell 43, real
Show near-zero release (the ＜ 5mg/Nm of dust3)。
Embodiment 4
As in figure 2 it is shown, by boiler 1, electric cleaner 2, desulfurization unit 3, wet cottrell 4, chimney 5, atomising device
6, waste water separator 7 and wastewater treatment equipment 8 are attached, wherein, and the exhanst gas outlet of boiler 1 and the flue gas of electric cleaner 2
Entrance connects, and the fume emission mouth of described electric cleaner 2 is connected with the smoke inlet of described desulfurization unit 3 by pipeline, described
The exhanst gas outlet of desulfurization unit 3 is connected with the smoke inlet of described wet cottrell 4 by pipeline, desulfurization unit 3 and wet
The wastewater outlet of formula electrostatic precipitator 4 all entrances with waste water separator 7 are connected, the upper liquid of described waste water separator 7
Body outlet is connected with the water inlet of atomising device 6, and the outlet of atomising device 6 is connected with the pipeline of electric cleaner 2 upstream；Described useless
Lower floor's liquid outlet of water separation device 7 is connected with the entrance of wastewater treatment equipment 8, the water out of described wastewater treatment equipment 8
It is connected with the water inlet of wet cottrell 4, the wastewater outlet of described wet cottrell 4 and described waste water separator
The entrance of 7 connects.The exhanst gas outlet of described wet cottrell 4 is connected with chimney 5.
Power is the unit of 300MW, and fuel A (specially coal) burns in boiler 1 and produces flue gas, processes through denitration
Rear entrance electric cleaner 2, the condition that denitration processes includes: using SCR technique, catalyst is vanadium Titanium series catalyst, temperature range
For 290-400 DEG C.
The entrance flue gas temperature of electric cleaner 2 about 130 DEG C, flue gas flow about 1,100,000 Nm3/ h, the particulate matter in flue gas is dense
Degree is 12g/Nm3.The particle concentration of the flue gas after electric cleaner 2 processes is 21mg/Nm3.After electric cleaner 2 processes
Flue gas enters wet desulphurization device 3 and processes.SO in wet desulphurization device 3, in flue gas2React with lime stone slurry,
Thus SO2Remove from flue gas.From absorption tower discharge lime stone slurry through cyclonic separation, wash and be dehydrated after obtain stone
Cream, creates desulfurization wastewater B simultaneously.The pH value of desulfurization wastewater B is 5.5, and suspension content is 4.5g/L, in described desulfurization wastewater
Containing Cl-、F-、SO4 2-、Ca2+、Mg2+.The weight of desulfurization wastewater B about 5 tons.
Flue gas desulfuration efficiency after wet desulphurization device 3 processes has reached 99%.Flue gas after desulfurization processes enters
Wet cottrell 4.Described wet cottrell 4 uses flexible plate dedusting, and deashing is by the uniform water in full surface of pole plate
Film flows automatically.The dust waste water F that described wet cottrell 4 produces contains a small amount of fine dust and Gypsum Fibrosum drop.Wet electrostatic removes
The dust waste water about 1.5 tons that dirt device 4 produces.
Desulfurization wastewater B, after the separation of waste water separator 7, realizes three layers of separating effect according to density difference, is divided into
Supernatant liquid C, lower floor liquid F and solid residue.Wherein, the density of supernatant liquid C about 1005kg/m3, weight about 2 tons, water
Temperature about 40 DEG C, enters in atomising device 6 and is atomized under the effect of compressed air E, atomizing pressure about 0.4MPa, the drop after atomization
Speed is 40m/s.Drop after atomization sprays into the upstream line of electric cleaner 2, and spraying into a little distance with electric cleaner 2 is 5 meters,
Drop after the atomization time of staying in the duct is 0.5 second.
Through measuring and calculating, supernatant liquid C through atomization after enter electric cleaner 2 upstream line evaporate completely after, in pipeline
Smoke moisture is increased to 8.91% by 8.61%, and flue-gas temperature is reduced to 126 DEG C.Flue gas is in undersaturated condition, higher than acid dew
Point temperature (acid dew-point temperature about 80-95 DEG C), will not produce corrosion to flue and electric cleaner, therefore, there is no need to spray waste water
After access point, pipeline and cleaner unit carry out reforming processing.Meanwhile, the increase of smoke moisture and the reduction of flue-gas temperature, also reduce electricity
The ratio resistance that cleaner unit is mellow lime, is conducive to improving efficiency of dust collection.It addition, because of the reduction of flue-gas temperature and the increasing of humidity of flue gas
Add, decrease the water consumption of FGD (flue gas desulfurization) system.(heavy metal, impurity and each additionally, solids in desulfurization wastewater
Plant slaine etc.) it is suspended in together with ash in flue gas and enters electric cleaner with flue gas, caught by electrode in electric cleaner, with
Ash outer row together, because in desulfurization wastewater, amount of solid and various metal salt concentration are less, physical property and comprehensive utilization to ash will not be produced
Raw impact.
The flue gas that wet cottrell 4 processed discharges through chimney 5, lower floor's liquid D that waste water separator 7 produces
Through the purified treatment of wastewater treatment equipment 8, purified treatment includes using chemical agent to carry out flocculation sediment, and by purified treatment
After water as the flushing water of wet cottrell 4.The condition of flushing water includes that pH value is 7.2, and solid suspension is
65ppm。
It addition, collect solid-state Gypsum Fibrosum that waste water separator 7 produces and body refuse H and wastewater treatment equipment 8 produce consolidates
Body residue carries out subsequent treatment, and solid-state Gypsum Fibrosum is transported to stockyard, body refuse and solid residue is abandoned.
After tested, outlet particle concentration (dust concentration) the about 21mg/Nm of electric cleaner 23, wet desulphurization device 3
Outlet particulate matter (carrying containing Gypsum Fibrosum) concentration about 16mg/Nm3, the outlet particle concentration about 4mg/Nm of wet cottrell 43,
Achieve near-zero release (the ＜ 5mg/Nm of dust3).Sprayed into by cycling utilization of wastewater and pipeline, wet desulphurization device and wet type
Electrostatic precipitator, without arranging outside waste water, is truly realized wastewater zero discharge.
Comparative example 1
According to the same manner as in Example 1 by boiler 1, electric cleaner 2, desulfurization unit 3, wet cottrell 4, cigarette
Chimney 5 is attached.Except for the difference that, atomising device 6 and waste water separator 7 are not included.
Power is the unit of 300MW, and fuel A (specially coal) burns in boiler 1 and produces flue gas, processes through denitration
Rear entrance electric cleaner 2.Process according to condition same as in Example 1.
Flue gas discharges through chimney 5 after passing sequentially through electric cleaner 2, desulfurization unit 3, wet cottrell 4.
Through measuring and calculating, the entrance flue gas temperature of electric cleaner 2 130 DEG C, (dust is dense for the outlet particle concentration of electric cleaner 2
Degree) 35mg/Nm3, outlet particulate matter (carrying containing Gypsum Fibrosum) concentration 25mg/Nm of desulfurization unit 33, going out of wet cottrell 4
Mouth particle concentration 7mg/Nm3.The desulfurization wastewater 3.8 tons that desulfurization unit 3 produces, the dedusting that wet cottrell 4 produces is given up
1.2 tons of water, standard discharge after needing to process.
From the result of embodiment and comparative example it can be seen that use the equipment of the fume treatment of this utility model offer, warp
Cross the flue gas after processing, it is achieved that near-zero release (the ＜ 5mg/Nm of dust3), additionally, wet desulphurization device and wet electrostatic remove
Dirt device is without arranging outside waste water, it is achieved that the zero-emission of waste water.And in contrast, in comparative example 1, wet cottrell 4 goes out
Particle concentration in the flue gas of mouth, apparently higher than embodiment 1, also creates a large amount of waste water, in addition it is also necessary to through follow-up place simultaneously
Reason can be discharged.
Preferred implementation of the present utility model described in detail above, but, this utility model is not limited to above-mentioned reality
Execute the detail in mode, in technology concept of the present utility model, the technical solution of the utility model can be entered
The multiple simple variant of row, these simple variant belong to protection domain of the present utility model.
It is further to note that each the concrete technical characteristic described in above-mentioned detailed description of the invention, at not lance
In the case of shield, can be combined by any suitable means.In order to avoid unnecessary repetition, this utility model is to respectively
Plant possible compound mode to illustrate the most separately.
Additionally, combination in any can also be carried out, as long as it is not disobeyed between various different embodiment of the present utility model
Carrying on the back thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (11)
1. an equipment for fume treatment, this equipment includes electric cleaner (2), desulfurization unit (3), wet cottrell (4),
The fume emission mouth of described electric cleaner (2) is connected with the smoke inlet of described desulfurization unit (3) by pipeline, described desulfurization list
The exhanst gas outlet of unit (3) is connected with the smoke inlet of described wet cottrell (4) by pipeline, it is characterised in that this sets
Standby atomising device (6) and the waste water separator (7) of also including, the wastewater outlet of desulfurization unit (3) and waste water separator (7)
Entrance connects, and the liquid outlet of described waste water separator (7) is connected with the water inlet of atomising device (6), atomising device (6)
Outlet is connected with the pipeline of electric cleaner (2) upstream.
Equipment the most according to claim 1, it is characterised in that the liquid outlet of described waste water separator (7) includes
Layer liquid outlet and lower floor's liquid outlet, the outlet of described supernatant liquid is connected with the sulfur removal technology water inlet of desulfurization unit (3), institute
State lower floor's liquid outlet to be connected with the water inlet of atomising device (6).
Equipment the most according to claim 2, it is characterised in that the outlet of described supernatant liquid and described wet cottrell
(4) wastewater outlet all sulfur removal technology water inlets with desulfurization unit (3) are connected.
Equipment the most according to claim 1, it is characterised in that the equipment of described fume treatment also includes wastewater treatment equipment
(8), the liquid outlet of described waste water separator (7) includes supernatant liquid outlet and lower floor's liquid outlet, described supernatant liquid
Outlet is connected with the water inlet of described atomising device (6), described lower floor liquid outlet and the entrance of described waste water separator (8)
Connecting, the outlet of described wastewater treatment equipment (8) is connected with the water inlet of described wet cottrell (4), and described wet type is quiet
The wastewater outlet of electric cleaner (4) is connected with the entrance of described waste water separator (7).
5. according to the equipment described in any one in claim 1-4, it is characterised in that described atomising device (6) is compression sky
Gas jet atomising device.
6. according to the equipment described in any one in claim 1-4, it is characterised in that described waste water separator (7) is attached most importance to
Power type solid-liquid separator.
Equipment the most according to claim 4, it is characterised in that described wastewater treatment equipment (8) is chemical flocculation precipitation dress
Put.
8. according to the equipment described in any one in claim 1-4, it is characterised in that described electric cleaner (2) is that electrostatic removes
Dirt device and/or electrostatic fabric filter.
Equipment the most according to claim 1, it is characterised in that described desulfurization unit (3) is wet desulphurization device.
10. according to the equipment described in any one in claim 1-4, it is characterised in that the outlet of described atomising device (6) with
The position that the pipeline of electric cleaner (2) upstream connects is not less than 5 meters with the distance of the entrance of described electric cleaner (2).
11. according to the equipment described in any one in claim 1-4, it is characterised in that described equipment also includes boiler (1),
The pipeline of described electric cleaner (2) upstream is the pipeline between boiler (1) and electric cleaner (2), and the liquid after described atomization
Drip and there is no miscellaneous equipment between position and the electric cleaner (2) of the pipeline spraying into electric cleaner upstream.
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| CN201620822734.2U CN205832882U (en) | 2016-07-29 | 2016-07-29 | A kind of equipment of fume treatment |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106039911A (en) * | 2016-07-29 | 2016-10-26 | 中国神华能源股份有限公司 | Equipment and method for flue gas treatment |
| CN107051084A (en) * | 2017-04-27 | 2017-08-18 | 浙江菲达环保科技股份有限公司 | Deep temperature reduction coupling humidification puies forward the wastewater zero discharge dust pelletizing system of effect |
-
2016
- 2016-07-29 CN CN201620822734.2U patent/CN205832882U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106039911A (en) * | 2016-07-29 | 2016-10-26 | 中国神华能源股份有限公司 | Equipment and method for flue gas treatment |
| CN107051084A (en) * | 2017-04-27 | 2017-08-18 | 浙江菲达环保科技股份有限公司 | Deep temperature reduction coupling humidification puies forward the wastewater zero discharge dust pelletizing system of effect |
| CN107051084B (en) * | 2017-04-27 | 2023-01-06 | 浙江菲达环保科技股份有限公司 | Wastewater zero-discharge dedusting system with deep cooling, humidifying and efficiency improving functions |
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