CN108218144B - Lead and zinc dressing wastewater treatment equipment and processing method - Google Patents
Lead and zinc dressing wastewater treatment equipment and processing method Download PDFInfo
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- CN108218144B CN108218144B CN201810207625.3A CN201810207625A CN108218144B CN 108218144 B CN108218144 B CN 108218144B CN 201810207625 A CN201810207625 A CN 201810207625A CN 108218144 B CN108218144 B CN 108218144B
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- 239000011701 zinc Substances 0.000 title claims abstract description 66
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 64
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 64
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 27
- 238000003672 processing method Methods 0.000 title claims abstract description 16
- 239000002351 wastewater Substances 0.000 claims abstract description 122
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 73
- 230000007246 mechanism Effects 0.000 claims abstract description 68
- 238000005273 aeration Methods 0.000 claims abstract description 65
- 239000010802 sludge Substances 0.000 claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims abstract description 22
- 150000002500 ions Chemical class 0.000 claims abstract description 17
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 31
- 230000001376 precipitating effect Effects 0.000 claims description 29
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 239000006228 supernatant Substances 0.000 claims description 13
- 239000003957 anion exchange resin Substances 0.000 claims description 11
- 238000004062 sedimentation Methods 0.000 claims description 10
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 239000010865 sewage Substances 0.000 claims description 6
- 239000002244 precipitate Substances 0.000 claims description 5
- 238000002203 pretreatment Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 3
- 238000010899 nucleation Methods 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 2
- 239000005864 Sulphur Substances 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims description 2
- 239000013049 sediment Substances 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims 2
- 229910002092 carbon dioxide Inorganic materials 0.000 claims 2
- 239000001569 carbon dioxide Substances 0.000 claims 1
- 230000000694 effects Effects 0.000 description 13
- 238000000034 method Methods 0.000 description 11
- 238000012545 processing Methods 0.000 description 9
- 239000005416 organic matter Substances 0.000 description 8
- 239000011347 resin Substances 0.000 description 7
- 230000008901 benefit Effects 0.000 description 6
- 229920005989 resin Polymers 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 238000005342 ion exchange Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000004064 recycling Methods 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 150000001450 anions Chemical class 0.000 description 3
- 238000005188 flotation Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 229910020218 Pb—Zn Inorganic materials 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 244000299461 Theobroma cacao Species 0.000 description 2
- 235000009470 Theobroma cacao Nutrition 0.000 description 2
- 239000012445 acidic reagent Substances 0.000 description 2
- 238000005276 aerator Methods 0.000 description 2
- -1 benzene alkene terpene Chemical class 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000009388 chemical precipitation Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
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- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N monobenzene Natural products C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000006213 oxygenation reaction Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 235000019994 cava Nutrition 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 229940116901 diethyldithiocarbamate Drugs 0.000 description 1
- LMBWSYZSUOEYSN-UHFFFAOYSA-N diethyldithiocarbamic acid Chemical compound CCN(CC)C(S)=S LMBWSYZSUOEYSN-UHFFFAOYSA-N 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- ZOOODBUHSVUZEM-UHFFFAOYSA-N ethoxymethanedithioic acid Chemical compound CCOC(S)=S ZOOODBUHSVUZEM-UHFFFAOYSA-N 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- JQJCSZOEVBFDKO-UHFFFAOYSA-N lead zinc Chemical compound [Zn].[Pb] JQJCSZOEVBFDKO-UHFFFAOYSA-N 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- RECVMTHOQWMYFX-UHFFFAOYSA-N oxygen(1+) dihydride Chemical compound [OH2+] RECVMTHOQWMYFX-UHFFFAOYSA-N 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 238000012372 quality testing Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 235000007586 terpenes Nutrition 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
- 239000012991 xanthate Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/62—Heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/422—Treatment of water, waste water, or sewage by ion-exchange using anionic exchangers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/19—SO4-S
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention discloses a kind of lead and zinc dressing wastewater treatment equipment and processing methods, the lead and zinc dressing wastewater treatment equipment, including the pH value for adjusting lead and zinc dressing waste water to settle the pretreatment pool and the aerobe reaction pond of the COD value for reducing pretreatment pool water outlet that remove heavy metal ion.Aerobe reaction pond includes the aeration zone and settling zone to communicate with each other, and aeration zone is connected to pretreatment pool, and has and be suspended in the aerobe sludge in lead and zinc dressing waste water by being aerated mechanism.Aerobe reaction pond further includes the sulfate radical removal mechanism being connected to settling zone for reducing settling zone water outlet sulfate concentration.For above-mentioned lead and zinc dressing wastewater treatment equipment on the basis of removing lead and zinc dressing heavy metals ion and reducing lead and zinc dressing COD value of waste water, creative increasing reduces sulfate radical removal mechanism, so that effluent quality meets mill water requirement.
Description
Technical field
The present invention relates to beneficiation wastewater reuse fields, particularly, are related to a kind of lead and zinc dressing wastewater treatment equipment.In addition,
The invention further relates to a kind of processing methods including above-mentioned lead and zinc dressing waste water.
Background technique
Nonferrous metals ore floatation process supervenes a large amount of beneficiation wastewater, and every annual emissions reach hundred million tons of 12-15, occupy
30% or so of non-ferrous metal industrial wastewater.This waste water contains plurality of heavy metal ion and xanthate, benzene alkene terpene, diethyldithiocarbamate, humic
The organic pollutants such as sour sodium, complicated component, strong toxicity, concentration are high, seriously affect environment of mining area.Therefore, the processing of beneficiation wastewater
It is significant to the environment and water resource scarcity problem that solve relevant range with reuse.
" lead, the Zn Cr coating pollutant emission standard (GB25466-2010) " of implementation is to lead and zinc dressing enterprise from 2012
Water pollution control index proposes more strict requirements.Currently, the processing for beneficiation wastewater, chemical precipitation-advanced oxidation
(Fenton process or ClO2Oxidation), the methods of membrane technology reagent consumption amount is big, higher cost, and individually biochemical treatment then exist it is useless
The problem that water biodegradability is low, water treatment effect is bad.Therefore, economic, efficient lead and zinc dressing wastewater treatment how is researched and developed
There is huge market capacity and broad application prospect with reuse technology.
Summary of the invention
The present invention provides a kind of lead and zinc dressing wastewater treatment equipment and processing methods, to solve lead and zinc dressing waste water cost
Technical problem higher, treatment effect is bad.
The technical solution adopted by the invention is as follows:
One aspect of the present invention provides a kind of lead and zinc dressing wastewater treatment equipment, including for adjusting lead and zinc dressing waste water
PH value removes the pretreatment pool of heavy metal ion and the aerobe reaction of the COD value for reducing pretreatment pool water outlet to settle
Pond.
Aerobe reaction pond includes the aeration zone and settling zone to communicate with each other, and aeration zone is connected to pretreatment pool, and is had
There is the aerobe sludge being suspended in lead and zinc dressing waste water by being aerated mechanism.
Aerobe reaction pond further includes the sulfate radical being connected to settling zone for reducing settling zone water outlet sulfate concentration
Removal mechanism.
Further, sulfate radical removal mechanism is anion exchange resin mechanism.
Further, the quantity of aeration zone is two, and two aeration zones are connected to pretreatment pool, and settling zone is arranged two
In a aeration zone and communicate therewith.
Further, settling zone bottom is equipped with the slope that the sludge for that will precipitate returns to aeration zone, and aeration zone bottom is set
There is mud discharging mouth.
Further, pretreatment pool is equipped with CO2It is aerated mechanism.
Another aspect of the present invention provides a kind of processing method of lead and zinc dressing wastewater treatment, comprising the following steps:
Lead and zinc dressing waste water is passed through in pretreatment pool, pH value is adjusted and generates to precipitating, and supernatant is transferred to aerobic
Biological reaction pool.
Enter settling zone, aerobe sludge settling point after the aerobe sludge reaction that supernatant and aeration zone suspend
From the waste water after precipitating flows out, and water outlet COD is lower than 40mg/L.
Waste water after precipitating is handled through sulfate radical removal mechanism reduces sulfate ion concentration, obtains recycle-water, recycle-water
Sulfate ion concentration be lower than 1000mg/L, it is preferable that the sulfate ion concentration of recycle-water be lower than 800mg/L.
Further, it is 8.5~10 that pH value is adjusted in pretreatment pool, and standing 2~4 hours complete to precipitating.
Residence time of the supernatant in aerobe reaction pond is 8~12 hours.
Further, aerobe sludge is made using acclimation, acclimation are as follows:
It takes sludge sewage as seed sludge, is added in aerobe reaction pond, sludge seeding amount is
SV30: 20%~30%.
The domestication in one day per stage of 5 stages is set, and steps up waste water load after pretreatment, per stage pretreatment
Waste water/clear water volume ratio is respectively 1:5,2:4,3:3,4:2,5:1, waste water after all pretreatments of finally intaking afterwards.
Biochemical indicator is SV during domestication30: 20%~30%, dissolved oxygen concentration: 2~4mg/L is discharged COD:< 40mg/
L。
Further, residence time of the waste water after precipitating in sulfate radical removal mechanism is 0.5~1 hour.
Further, sulfate radical removal mechanism is anion exchange resin mechanism, and the processing method of lead and zinc dressing waste water is also
Including being regenerated using 1.1 times of NaOH solutions, the regeneration period is 1 day.
The invention has the following advantages: above-mentioned lead and zinc dressing wastewater treatment equipment, including pretreatment pool, aerobe
Reaction tank and sulfate radical removal mechanism.PH value is adjusted first in pretreatment pool makes the heavy metal ion in lead and zinc dressing waste water
Precipitating is formed to then contact by pretreated waste water with the aerobe sludge in aeration zone by sedimentation removal
Reaction removes organic matter to reduce COD value, and aerobe sludge settles in settling zone, and top water body flow to sulfate radical removal
Most sulfate ion is removed in mechanism, obtains recycle-water.Applicant is by a large amount of the study found that lead and zinc dressing waste water
Middle sulfate ion is very big on waste water recycling influence, and when its concentration is higher, aeneficiation effect is poor, it is difficult to meet mill water
It is required that and other anion are then relatively small on waste water recycling influence.Thus above-mentioned lead and zinc dressing wastewater treatment equipment is being gone
Except lead and zinc dressing heavy metals ion and on the basis of reducing lead and zinc dressing COD value of waste water, creative increases reduction sulphur
Acid group removal mechanism, so that effluent quality meets mill water requirement.
Other than objects, features and advantages described above, there are also other objects, features and advantages by the present invention.
Below with reference to figure, the present invention is described in further detail.
Detailed description of the invention
The attached drawing constituted part of this application is used to provide further understanding of the present invention, schematic reality of the invention
It applies example and its explanation is used to explain the present invention, do not constitute improper limitations of the present invention.In the accompanying drawings:
Fig. 1 is the lead and zinc dressing wastewater treatment equipment schematic diagram of the preferred embodiment of the present invention；
Fig. 2 is the lead and zinc dressing wastewater treatment equipment schematic diagram of another preferred embodiment of the present invention.
Description of symbols: 100, pretreatment pool；200, aerobe reaction pond；300, sulfate radical removal mechanism；400,
Slope；
210, aeration zone；220, settling zone；230, it is aerated mechanism；240, baffle；250, overflow port；260, overflow launder.
Specific embodiment
The embodiment of the present invention is described in detail below in conjunction with attached drawing, but the present invention can be defined by the claims
Implement with the multitude of different ways of covering.
Referring to Fig.1~2, the preferred embodiment of the present invention provides a kind of lead and zinc dressing wastewater treatment equipment, including is used for
The pH value of lead and zinc dressing waste water is adjusted to settle and remove the pretreatment pool 100 of heavy metal ion and for reducing pretreatment pool 100
The aerobe reaction pond 200 of the COD value of water outlet.Aerobe reaction pond 200 includes the aeration zone 210 to communicate with each other and precipitating
Area 220, aeration zone 210 are connected to pretreatment pool 100, and are had and be suspended in lead and zinc dressing waste water by being aerated mechanism 230
Aerobe sludge.Aerobe reaction pond 200 further includes being connected to be discharged sulfuric acid for reducing settling zone 220 with settling zone 220
The sulfate radical removal mechanism 300 of root concentration.
Above-mentioned lead and zinc dressing wastewater treatment equipment, referring to Fig. 2, including pretreatment pool 100,200 and of aerobe reaction pond
Sulfate radical removal mechanism 300, three is sequentially communicated by pipeline.Lead and zinc dressing waste water enters pretreatment pool 100 by water inlet
In, lead and zinc dressing waste water is usually alkalescent, and pretreatment pool 100 is by being added acid reagent or being passed through CO2Gas aerating regulation
The pH value of waste water, so that heavy metal ion forms precipitating to by sedimentation removal.Supernatant liquor is entered aerobic by water outlet
In the aeration zone 210 of biological reaction pool 200.Aeration mechanism 230 is equipped in aeration zone 210, be continually fed into waste water air or
Oxygen so that waste water contacts oxygenation with air in pond, and stirs waste water and the oxygen of air is accelerated to shift into waste water, and prevent
Aerobe sludge sinks, and reinforces the contact of aerobe, organic matter and dissolved oxygen, carries out oxidation point to the organic matter in waste water
Solution reduces the COD value that pretreatment pool 100 is discharged.
Aeration zone 210 and settling zone 220 can be equipped with baffle 240, and baffle 240 is not complete by aeration zone 210 and settling zone 220
Full partition, thus waste water in aeration zone 210 and aerobe sludge can enter under aeration mechanism 230 and self-propagating effect
Settling zone 220.Preferably, baffle 240 is obliquely installed from aeration zone 210 to 220 direction of settling zone from top to bottom, in aeration mechanism
Under 230 help, facilitates aerobe sludge and realize interior circulation between aeration zone 210 and settling zone 220, to improve aeration zone
Sludge concentration in 210, the design advantageously reduce system operation energy consumption.
It is heavy that waste water and aerobe sludge in aeration zone 210 can enter under aeration mechanism 230 and self-propagating effect
Shallow lake area 220, the not set aeration mechanism 230 in settling zone 220.Aerobe sludge sinks down into 220 bottom of settling zone under the effect of gravity
Portion, 220 top of settling zone or the waste water outflow close to top enter sulfate radical removal mechanism 300.Preferably, settling zone 220
Top is equipped with overflow port 250 and overflow launder 260, and the water outlet of pretreatment pool 100 continues into aerobe reaction pond 200, and good
Waste water after the separation of oxygen biological sludge is spilled over in overflow launder 260 from top overflow port 250, then through the pipeline in overflow launder 260
Flow out to sulfate radical removal mechanism 300.This kind of mode can guarantee that the waste water at the top of settling zone 220 can flow out, and greatly reduce
Waste water not yet separates the probability flowed out with aerobe sludge.
Preferably, referring to Fig.1, also it can increase advection sedimentation between pretreatment pool 100 and aerobic biological reaction pool 200
Pond, in pretreatment pool 100 after the pH value of adjusting lead and zinc dressing waste water, waste water, which enters in horizontal sedimentation tank, to be carried out in precipitating removing
Metal ion.PH can also be increased after sulfate radical removal mechanism 300 and adjust reactor, the pH value of recycle-water is tentatively adjusted.
Common lead and zinc dressing wastewater treatment equipment only includes the structure and removal organic matter for removing heavy metal precipitation object
Structure, however the wastewater treatment equipment treated waste water can not reuse continue ore dressing, thus can not actually save choosing
Mining water.Inventor is by a large amount of the study found that the wastewater treatment equipment treated waste water is just because of sulfate ion
Excessive concentration, causing that treated, waste water can not circulating and recovering.Based on this, inventor is provided with sulfate radical removal on this basis
Mechanism 300, sulfate radical removal mechanism 300 is connected to settling zone 220 is discharged sulfate concentration reduction for settling zone 220, disappears substantially
Influence in addition to sulfate ion to ore dressing efficiently solves the problems, such as the circulating and recovering of beneficiation wastewater, the rate of recovery of floatable minerals
It is close with clear water with grade, wastewater recycle rate is improved, production cost is reduced.Sulfate radical removal mechanism 300 can be yin
Ion exchange resin mechanism, reverse osmosis membrane separation mechanism, chemical precipitation method mechanism.
The invention has the following advantages: above-mentioned lead and zinc dressing wastewater treatment equipment, including it is pretreatment pool 100, aerobic
Biological reaction pool 200 and sulfate radical removal mechanism 300.PH value is adjusted first in pretreatment pool 100 makes lead and zinc dressing waste water
In heavy metal ion form precipitating to by sedimentation removal, then will be by pretreated waste water and aeration zone 210
Aerobe sludge haptoreaction, remove organic matter to reduce COD value, aerobe sludge settles in settling zone 220, on
Portion's water body flow to the most sulfate ion of removal in sulfate radical removal mechanism 300, obtains recycle-water.Applicant passes through a large amount of
The study found that lead and zinc dressing sulfate radical in waste water ion pair waste water recycling influence very big, the aeneficiation effect when its concentration is higher
It is poor, it is difficult to meet the requirement of mill water.Thus above-mentioned lead and zinc dressing wastewater treatment equipment is in removal lead and zinc dressing waste water weight
On the basis of metal ion and reduction lead and zinc dressing COD value of waste water, creative increasing reduces sulfate radical removal mechanism 300,
So that effluent quality meets mill water requirement.
Optionally, referring to Fig. 2, sulfate radical removal mechanism 300 is anion exchange resin mechanism.Anion exchange resin machine
Structure concrete form can be anion-exchange column, internal to load anion exchange resin, by upper level be discharged in anion such as
Sulfate radical is replaced by hydroxyl and is retained.Anion exchange resin mechanism is lower compared to chemical precipitation method agency cost.Anion
Exchanger resin mechanism has the advantages that treatment effeciency height, non-scaling compared to reverse osmosis membrane separation mechanism.
Optionally, referring to Fig. 2, the quantity of aeration zone 210 is two, and two aeration zones 210 connect with pretreatment pool 100
Logical, settling zone 220 is arranged in two aeration zones 210 and communicates therewith.
In this embodiment, aerobe reaction pond 200 includes two aeration zones 210 and a settling zone 220, aeration zone
210 are arranged at 220 both ends of settling zone.The water outlet of pretreatment pool respectively enters two aeration zones 210 while carrying out Air Exposure, with
Aerobe sludge reaction enters back into settling zone 220.The design improves the processing capacity of waste water, improves the processing of waste water
Efficiency.
Optionally, referring to Fig. 2,220 bottom of settling zone is equipped with the slope that the sludge for that will precipitate returns to aeration zone 210
400。
There is a certain distance between 240 lower end of baffle and slope 400, return to aeration zone 210 for sludge and leave channel.Gear
When plate 240 is obliquely installed from aeration zone 210 to 220 direction of settling zone from top to bottom, which is more conducive to aerobe sludge
It is precipitated in settling zone 220, on sunken caves to slope 400.Slope 400 has certain inclination angle, and aerobe sludge is made in gravity
It is moved with the lower inclined-plane along slope 400 and is back to aeration zone 210, it is most of under the action of the aeration mechanism 230 of aeration zone 210
Sludge can rise again to be reacted with waste water, to realize the interior circulation of aerobe sludge.When setting, there are two aeration zones 210
When, slope 400 can have there are two inclined-plane, respectively correspond two aeration zones 210, sludge is back to corresponding aeration zone 210.
Optionally, referring to Fig. 2,210 bottom of aeration zone is equipped with mud discharging mouth.The appropriate spoil disposal when sludge is excessive.
Another aspect of the present invention provides a kind of processing method of lead and zinc dressing wastewater treatment, referring to Fig. 2, including following step
It is rapid:
Lead and zinc dressing waste water is passed through in pretreatment pool 100, pH value is adjusted and generates to precipitating, and supernatant is shifted into most intimate friend
Oxygen biological reaction pool 200.
Enter settling zone 220 after the aerobe sludge reaction that supernatant and aeration zone 210 suspend, aerobe sludge is heavy
It forms sediment and separates, the waste water outflow after precipitating, water outlet COD is lower than 40mg/L.
Waste water after precipitating is handled through sulfate radical removal mechanism 300 reduces sulfate ion concentration, obtains recycle-water, reuse
The sulfate ion concentration of water is lower than 1000mg/L, it is preferable that the sulfate ion concentration of recycle-water is lower than 800mg/L.
Lead and zinc dressing waste water can be entered in pretreatment pool 100 by water inlet, and lead and zinc dressing waste water is usually alkalinity, pre- to locate
Reason pond 100 is by being added acid reagent or being passed through CO2The pH value of gas aerating regulation waste water, so that heavy metal ion forms precipitating
To pass through sedimentation removal.Supernatant is to pass through pretreated waste water.The aerobe that supernatant and aeration zone 210 suspend
Enter settling zone 220 after sludge reaction, aerobe sludge settling separates, and the waste water outflow after precipitating, water outlet COD is lower than
40mg/L。
It is equipped with aeration mechanism 230 in aeration zone 210, air is continually fed into waste water, so that waste water connects with air in pond
Touching oxygenation, and stir waste water and the oxygen of air is accelerated to shift into waste water, and prevent aerobe sludge from sinking, reinforce aerobic
The contact of biology, organic matter and dissolved oxygen carries out oxygenolysis to the organic matter in waste water, reduces what pretreatment pool 100 was discharged
COD value.Waste water and aerobe sludge in aeration zone 210 can enter precipitating under aeration mechanism 230 and self-propagating effect
Area 220, the not set aeration mechanism 230 in settling zone 220.Aerobe sludge sinks down into 220 bottom of settling zone under the effect of gravity,
220 top of settling zone or close to top waste water outflow enter sulfate radical removal mechanism 300.
Waste water after precipitating can fully enter reduction sulfate ion concentration in sulfate radical removal mechanism 300 and obtain reuse
Water, or precipitating after wastewater fraction enter in sulfate radical removal mechanism 300 reduce sulfate ion concentration after, with it is remaining not into
The waste water for entering sulfate radical removal mechanism 300 re-mixes to obtain recycle-water, can such as lead to the waste water after 50%~90% precipitating
Enter after sulfate radical removal mechanism 300 handles, then mixes with remaining waste water.Above two mode no matter which kind of mode recycle-water it is equal
It is required that sulfate ion concentration is lower than 1000mg/L, it is preferable that the sulfate ion concentration of recycle-water is lower than 800mg/L.
Optionally, it is 8.5~10 that pH value is adjusted in pretreatment pool 100, and standing 2~4 hours complete to precipitating.The pH range
For heavy metal lead, zinc precipitate Optimal pH, it is too low or it is excessively high can all cause heavy metal processing not exclusively, lead to subsequent aerobe
The microorganism of reaction tank is poisoned.Time of repose is short, and precipitating can not settle completely, and sedimentation time length will lead to settling zone volume mistake
It is big to influence economic benefit.
Residence time of the supernatant in aerobe reaction pond 200 is 8~12 hours.
Residence time of the supernatant in aerobe reaction pond 200 be aeration zone 210 and settling zone 220 in total
Residence time.Residence time is 8~10 hours, and time span is suitable, and both cocoa effectively guaranteed the removal effect of organic matter, together
When in turn avoid meaningless excess dwell, improve sewage treating efficiency.Preferably 10~12 hours.
Optionally, aerobe sludge is made using acclimation, acclimation are as follows:
1 takes sludge sewage as seed sludge, is added in aerobe reaction pond 200, sludge seeding amount
For SV30: 20%~30%.
The 2 setting 5 stages per stage one day domestications, and waste water load after pretreatment is stepped up, per stage is located in advance
Waste water/clear water volume ratio is respectively 1:5,2:4,3:3,4:2,5:1, waste water after all pretreatments of finally intaking after reason.
Biochemical indicator is SV during 3 domestications30: 20%~30%, dissolved oxygen concentration: 2~4mg/L is discharged COD:< 40mg/
L。
SV30For sludge settling volume.When domestication, point 5 stages are carried out, each one day of each stage.Step up pretreatment
Waste water load afterwards, waste water/clear water volume ratio is respectively 1:5,2:4,3:3,4:2,5:1 after per stage pretreatment, and finally water inlet is complete
Portion is waste water after pretreatment, and tap water can be used in clear water.Biochemical indicator is SV during domestication30: 20%~30%, dissolved oxygen is dense
Degree: 2~4mg/L is discharged COD:< 40mg/L.Under this condition can effective acclimation sludge so that sludge reaches processing waste water
Standard.
Optionally, residence time of the waste water after precipitating in sulfate radical removal mechanism 300 is 0.5~1 hour.
Waste water after precipitating stops 8~10 hours in sulfate radical removal mechanism 300, and time span is suitable, and both cocoa had
The removal effect of the guarantee sulfate radical of effect, while meaningless excess dwell is in turn avoided, improve sewage treating efficiency.
Optionally, sulfate radical removal mechanism 300 is anion exchange resin mechanism, and the processing method of lead and zinc dressing waste water is also
Including being regenerated using 1.1 times of NaOH solutions, the regeneration period is 1 day.
Waste water after precipitating enters anion exchange resin mechanism and elutes from top to bottom.Resin can pass through 1.1 times of NaOH liquid
It is regenerated, regeneration period 1d.
The removal principle of sulfate radical: OH- and sulfate radical (SO in NaOH4 2-) swap.Detailed process is as follows:
Regeneration: ion exchange mechanism, NaOH is added in NaOH solution by the NaOH solution that configuration quality concentration is 4%~5%
In OH- by the SO on resin4 2-It cements out, OH- is by resin adsorption, the Na of generation2SO4Solution output mechanism.
Use: waste water enters ion exchange mechanism, the SO4 in waste water2-OH- on ion and resin is replaced, in waste water
SO4 2-It is removed by resin adsorption.
OH- and SO4 2-It is replaced by 2:1, the amount * 2 of the sulfate radical of removal is needed in theoretical amount, that is, waste water of NaOH, is
Guarantee regeneration effect, usual NaOH are 1.1 times excessive.NaOH liquid is added to be regenerated, cost has been saved.
Beneficiation wastewater used in the embodiment of the present invention and comparative example is from same Pb-Zn deposits dressing plant with primary choosing
Beneficiation wastewater after mine, water inlet pH value are 11.5, COD 430mg/L, sulfate concentration 1400mg/L.
In the processing system of the present embodiment, pretreatment reaction pond is cylindric, is highly 1.5m, outside diameter 1.2m,
Inside diameter is 1.15m, and pretreatment reaction pond material is polyethylene；Water inlet is leaving a mouthful position of reactor bottom 1m high,
Water outlet is leaving a mouthful position of reactor bottom 1.4m high, and water inlet is provided with peristaltic pump.Aerobic aerobe reaction pond
200 be rectangular-shape, and both ends are aeration reaction zone, and centre is settling zone 220, and each segment length's width is 0.8m, high 1.2m.Ion is handed over
Change pillar height 0.8m, diameter 0.3m.The pipe diameter for connecting each reactor Inlet and outlet water is 3cm.
200 sludge acclimatization process of aerobe reaction pond are as follows: take sludge sewage as seed sludge, be added
In biochemical reactor, sludge SV30About 20%；5 days domestications are set, the water volume ratio of daily waste water/originally be respectively 1:5,2:4,
3:3,4:2,5:1, waste water after all pretreatments of finally intaking；Biochemical indicator is SV:20%-30%, dissolved oxygen during domestication
Concentration: 2-4mg/L is discharged COD:< 40mg/L.
Embodiment 1
Pb-Zn deposits beneficiation wastewater is introduced into pretreatment reaction pond, with the stirring of 100r/min revolving speed, while exposing CO2, aeration quantity
For 0.3g/L waste water, 1 μm of aerator aperture, aeration time 1min, pH are adjusted to 9.5；3h is staticly settled, clear liquid enters aerobic life
Object reaction tank 200.
Aerobic biological process reactor sludge loading is 0.5kg CODCr/ (kg MLSSd), air aeration use 8 groupsMicro-hole aerator, service area 0.16m2/, oxygen utilization rate 20%；200 residence time of aerobe reaction pond
10-12h, reactor biochemical indicator with domestication during it is identical, after biological treatment waste water through secondary precipitation later half water enter from
Sub- switch carries out desalination.
Ion interchange unit filler is anion exchange resin, and amount of resin 80L, residence time 30min, bio-chemical effluent is from upper
And lower elution, ion exchange column water outlet are used as ore dressing recycle-water after mixing with water outlet after the other half biochemical treatment.
Embodiment 2
Pretreatment and biological treatment step with embodiment 1,90% water of biological treatment waste water enter ion interchange unit into
Row desalination, ion exchange column water outlet are used as ore dressing recycle-water after mixing with water outlet after remaining 10% biochemical treatment.
Comparative example
With embodiment 1, bio-chemical effluent does not pass through ion-exchange treatment and is directly used as ore dressing for pretreatment and biological treatment step
Recycle-water.
Test example
According to correlation technique specified in " integrated wastewater discharge standard " GB8978-1996 to embodiment 1-2 and comparative example
Indices are discharged after process to be detected.Testing result shows that the lead of embodiment 1-2 and comparative example and Zn content are low
In 0.1mg/L, it is discharged COD and stablizes in 40mg/L hereinafter, water quality reaches first discharge standard.Effluent index testing result is shown in Table
1。
Water outlet after embodiment 1 and comparative example processing is subjected to ore dressing experiment with water as flotation, measures the recycling of ore flotation
Rate and grade, and compared in clear water result.Part index number testing result is shown in Table 2.
1 embodiment of table, 1 effluent quality testing result
2 water quality detection result of table and lead zinc flotation recovery rate and grade
Ore dressing the result shows that, lead and zinc dressing wastewater treatment equipment provided by the invention and processing method are tested for ore dressing
The rate of recovery and grade of middle floatable minerals are close with clear water, meet mill water requirement, illustrate that this method not only can effectively be located
The discharge for managing beneficiation wastewater can also solve the problems, such as the cycling use of water in mineral processing production, drop low water usage cost.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, made any to repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (9)
1. a kind of lead and zinc dressing wastewater treatment equipment, which is characterized in that including the pH value for adjusting lead and zinc dressing waste water with heavy
Drop removes the pretreatment pool (100) of heavy metal ion and the aerobic life of the COD value for reducing the pretreatment tank (100) water outlet
Object reaction tank (200)；Pretreatment pool (100) is equipped with CO2Mechanism is aerated to adjust the pH value of waste water, the pH value of the waste water after adjusting
It is 8.5~10, horizontal sedimentation tank is provided between pretreatment pool (100) and aerobic biological reaction pool (200), in pretreatment pool
(100) after the pH value for adjusting lead and zinc dressing waste water in, waste water, which enters in horizontal sedimentation tank, carries out precipitating removing heavy metal ion；Institute
Stating aerobe reaction pond (200) includes the aeration zone (210) and settling zone (220) to communicate with each other, the aeration zone (210) with
The pretreatment tank (100) connection, and have and be suspended in the aerobic life in the lead and zinc dressing waste water by being aerated mechanism (230)
Object sludge；
The aerobe reaction pond (200) further includes being connected to the settling zone (220) for reducing the settling zone (220)
It is discharged the sulfate radical removal mechanism (300) of sulfate concentration.
2. lead and zinc dressing wastewater treatment equipment according to claim 1, which is characterized in that the sulfate radical removal mechanism
It (300) is anion exchange resin mechanism.
3. lead and zinc dressing wastewater treatment equipment according to claim 1, which is characterized in that the number of the aeration zone (210)
Amount is two, and described two aeration zones (210) are connected to the pretreatment tank (100), and the settling zone (220) is arranged in institute
It states in two aeration zones (210) and communicates therewith.
4. lead and zinc dressing wastewater treatment equipment according to claim 1, which is characterized in that settling zone (220) bottom
The slope (400) of the aeration zone (210) is returned to equipped with the sludge for that will precipitate；Aeration zone (210) bottom is equipped with row
Mud mouth.
5. a kind of processing method of lead and zinc dressing waste water, which comprises the following steps:
Lead and zinc dressing waste water is passed through in pretreatment pool (100), is passed through carbon dioxide gas aerating regulation pH value to 8.5~10,
Waste water is passed through horizontal sedimentation tank and carries out precipitating removing heavy metal ion, and supernatant is transferred to aerobe reaction pond
(200)；
Enter settling zone (220) after the aerobe sludge reaction that supernatant and aeration zone (210) suspend, aerobe sludge is heavy
It forms sediment and separates, the waste water outflow after precipitating, water outlet COD is lower than 40mg/L；
Waste water after the precipitating is handled through sulfate radical removal mechanism (300) reduces sulfate ion concentration, obtains recycle-water, institute
The sulfate ion concentration of recycle-water is stated lower than 1000mg/L.
6. the processing method of lead and zinc dressing waste water according to claim 5, which is characterized in that the pretreatment tank (100)
Interior adjusting pH value is 8.5~10, stands 2~4 hours and extremely precipitates completely；
Residence time of the supernatant in aerobe reaction pond (200) is 8-12 hours.
7. the processing method of lead and zinc dressing waste water according to claim 5, which is characterized in that the aerobe sludge is adopted
It is made with acclimation, the acclimation are as follows:
It takes sludge sewage as seed sludge, is added in the aerobe reaction pond (200), sludge seeding amount
For SV30: 20%~30%；
The domestication in one day per stage of 5 stages is set, and steps up waste water load after pretreatment, is given up after per stage pretreatment
Water/clear water volume ratio is respectively 1:5,2:4,3:3,4:2,5:1, waste water after all pretreatments of finally intaking；
Biochemical indicator is SV during domestication30: 20%~30%, dissolved oxygen concentration: 2~4mg/L is discharged COD:< 40mg/L.
8. the processing method of lead and zinc dressing waste water according to claim 5, which is characterized in that the waste water after the precipitating exists
Residence time in the sulfate radical removal mechanism (300) is 0.5~1 hour.
9. the processing method of lead and zinc dressing waste water according to any one of claim 5~8, which is characterized in that the sulphur
Acid group removal mechanism (300) is anion exchange resin mechanism, and the processing method of the lead and zinc dressing waste water further includes using 1.1
Times NaOH solution is regenerated, and the regeneration period is 1 day.
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| CN105217900A (en) * | 2015-11-17 | 2016-01-06 | 梅庆波 | A kind for the treatment of process of Pb-Zn deposits beneficiation wastewater |
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| CN101941761A (en) * | 2010-08-23 | 2011-01-12 | 四川省工业环境监测研究院 | Biochemical water treatment device and method |
| CN105217900A (en) * | 2015-11-17 | 2016-01-06 | 梅庆波 | A kind for the treatment of process of Pb-Zn deposits beneficiation wastewater |
| CN106242191A (en) * | 2016-08-31 | 2016-12-21 | 广州中环万代环境工程有限公司 | A kind of process technique of Pb-Zn deposits beneficiation wastewater |
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