CN108358387A - A kind of electroplating waste water treatment system and method - Google Patents
A kind of electroplating waste water treatment system and method Download PDFInfo
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- CN108358387A CN108358387A CN201810186447.0A CN201810186447A CN108358387A CN 108358387 A CN108358387 A CN 108358387A CN 201810186447 A CN201810186447 A CN 201810186447A CN 108358387 A CN108358387 A CN 108358387A
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- 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
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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- 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
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- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- 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
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- 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
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- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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
- C02F1/70—Treatment of water, waste water, or sewage by reduction
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/18—Cyanides
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
- C02F2101/22—Chromium or chromium compounds, e.g. chromates
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- 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
- C02F3/005—Combined electrochemical biological processes
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- 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
- C02F3/08—Aerobic processes using moving contact bodies
- C02F3/085—Fluidized beds
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- 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
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
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- 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
- C02F3/28—Anaerobic digestion processes
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- 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
- C02F3/30—Aerobic and anaerobic processes
Abstract
The invention discloses a kind of electroplating waste water treatment system and method, system includes：Pretreatment unit；Coagulative precipitation device comprising broken chromium reaction tank, coagulating sedimentation mechanism and intermediate pool；Biochemical reaction device, including hydrolysis acidification pool and horizontal three phase fluidized bed；Treated sewage reusing device, including membrane bioreactor, reverse osmosis mechanism and evaporation device；Method includes broken cyanide processing and/or oil removal treatment, carries out coagulation, precipitation, anaerobism, Aerobic Process for Treatment, biomembrane, reverse osmosis, evaporation process successively.The present invention will be after electroplating wastewater oil removing, broken cyanide by pretreatment unit, carry out brokenly chromium, coagulating sedimentation successively by coagulative precipitation device, it can remove heavy metal in decontaminated water, and anaerobism, aerobic is carried out by hydrolysis acidification pool, horizontal three phase fluidized bed successively, it can remove the suspended matter in waste water to reach discharge standard, and membrane bioreactor, reverse osmosis mechanism and evaporation device, which is arranged, can carry out waste water tertiary treatment, realize that water resource drinkableization recycles.
Description
Technical field
The present invention relates to sewage disposal technologies, more particularly, to a kind of electroplating waste water treatment system and method.
Background technology
In plating production process, contained drug is complicated in electroplate liquid, and there are many pollutants in the waste water generated, therefore
Multistep treatment need to be carried out when to electroplating wastewater treatment, and existing electroplating waste processing process is complicated, water utilization rate is low.
Invention content
It is an object of the invention to overcome above-mentioned technical deficiency, a kind of electroplating waste water treatment system and method are proposed, solve
The technical problem that electroplating waste processing process is complicated in the prior art and water utilization rate is low.
To reach above-mentioned technical purpose, technical scheme of the present invention provides a kind of electroplating waste water treatment system, including：
Pretreatment unit is used for by the cyanide wastewater broken cyanide and by oily waste water oil removing；
Coagulative precipitation device comprising sequentially connected broken chromium reaction tank, coagulating sedimentation mechanism and intermediate pool, it is described broken
Chromium reaction tank is connect with the pretreatment unit；
Biochemical reaction device comprising sequentially connected hydrolysis acidification pool and horizontal three phase fluidized bed, the hydrolysis acidification
Pond is connect with the intermediate pool；
Treated sewage reusing device comprising sequentially connected membrane bioreactor, reverse osmosis mechanism and evaporation device, the film
The water inlet degree of bioreactor is connect with the horizontal three phase fluidized bed.
Meanwhile the present invention also provides a kind of electroplating effluent treatment method, including the following steps：
(1) by electroplating wastewater cyanide wastewater and oily waste water carry out respectively broken cyanide processing and oil removal treatment after mix；
(2) mixed waste water is broken to stirring, precipitation after coagulant is added after chromium is handled；
(3) waste water after precipitation is subjected to anaerobism, Aerobic Process for Treatment successively；
(4) by step (3), treated that waste water carries out biomembrane, reverse osmosis, evaporation process successively.
Compared with prior art, the present invention passes through coagulating sedimentation by pretreatment unit by after electroplating wastewater oil removing, broken cyanide
Device carries out brokenly chromium, coagulating sedimentation successively, can remove heavy metal in decontaminated water, and pass through hydrolysis acidification pool, horizontal three-phase fluidization
Bed carries out anaerobism, aerobic successively, can remove the suspended matter in waste water to reach discharge standard, and be arranged membrane bioreactor,
Waste water can be carried out tertiary treatment by reverse osmosis mechanism and evaporation device, realize that water resource drinkableization recycles.
Description of the drawings
Fig. 1 is the attachment structure schematic diagram of the electroplating waste water treatment system of the present invention；
Fig. 2 is the attachment structure schematic diagram of the horizontal three phase fluidized bed of the present invention.
Specific implementation mode
In order to make the purpose , technical scheme and advantage of the present invention be clearer, with reference to the accompanying drawings and embodiments, right
The present invention is further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, and
It is not used in the restriction present invention.
Referring to Fig. 1, the present invention provides a kind of electroplating waste water treatment systems comprising pretreatment unit 1, coagulating sedimentation
Device 2, biochemical reaction device 3 and Treated sewage reusing device 4.
During electroplating wastewater processing, electroplating wastewater is divided into three kinds, and cyanide wastewater, oily waste water and Normal wastewater are
Convenient for handling above-mentioned three kinds of waste water, the present embodiment pretreatment unit 1 includes broken cyanide reaction tank 11, broken cyanide regulating reservoir
12, oil separator 13, air supporting 14, inclined plate grease removal tank 15, fuel-displaced regulating reservoir 16 and comprehensive adjustment pond 17, the oil separator 13, air supporting
14, inclined plate grease removal tank 15, fuel-displaced regulating reservoir 16 and comprehensive adjustment pond 17 are sequentially connected, the water inlet end of the broken cyanide regulating reservoir 12 with
The connection of broken cyanide reaction tank 11, water outlet and comprehensive adjustment pond 17 connect.When it carries out electroplating wastewater pretreatment, cyanide wastewater can be into
Enter broken cyanide reaction tank 11, oily waste water is then passed through oil separator 13, and Normal wastewater is then passed directly into comprehensive adjustment pond 17；Into broken cyanide
TLA compound for treatment of electroplating wastes can be added by chemical feed machine in the sewage of reaction tank 11, then put into sodium hydroxide or dilute sulfuric acid, and
It is 8.0~8.5 to control pH value in broken cyanide reaction tank 11, and above-mentioned solution is made fully to be reacted with substance in waste water；Waste water after reaction
Broken cyanide regulating reservoir 12 can be automatically flowed into, blender can be set in broken cyanide regulating reservoir 12, under the high-speed stirred effect of blender, cyanogen
Root is smashed completely, and the waste water handled by broken cyanide can flow into comprehensive adjustment pond 17 and carry out water quality, PH is adjusted；Oily waste water is then
By, by the oily waste degradation in waste water, then passing through fuel-displaced tune after oil separator 13, air supporting 14, the processing successively of inclined plate grease removal tank 15
Pond 16 is saved to carry out in water quality adjustment input comprehensive adjustment pond 17.
The present embodiment coagulative precipitation device 2 includes sequentially connected broken chromium reaction tank 21, coagulating sedimentation mechanism 22 and centre
Pond 23；The coagulating sedimentation mechanism 22 includes sequentially connected first PH regulating reservoirs 221, the first coagulating basin 222, first precipitation
Pond 223, the 2nd PH regulating reservoirs 224, transient response pond 225, middle transition pond 226, the 3rd PH regulating reservoirs 227, the second coagulating basin
228 and second sedimentation basin 229, the first PH regulating reservoirs 221 connect with the broken chromium reaction tank 21, second sedimentation basin
229 connect with the intermediate pool 23；The present embodiment breaks chromium reaction tank 21 and is connect with comprehensive adjustment pond 17, by regulating water quality
Sewage, which enters, breaks chromium reaction tank 21, dilute sulfuric acid is then added into broken chromium reaction tank 21, and control the PH broken in chromium reaction tank 21
Value is 2.5~3.0, while launching reducing agent sodium pyrosulfite, and control the potential value broken in chromium reaction tank 21 be 250~
300mV is conducive to ensure that the hexavalent chrome reduction in sewage is trivalent chromium, and then realizes and break chromium processing；After broken chromium, sewage flows into the
Lye can will be added in the first PH regulating reservoirs 221 in one PH regulating reservoirs 221, and the pH value for controlling waste water is 8~9, then by waste water
It inputs in the first coagulating basin 222, and polyacrylamide solution is added, and addition is 4L/m in waste water3Left and right, may make useless
The waste water for forming a large amount of alumen ustum in water, and being formed with a large amount of alumen ustum can enter the first sedimentation basin 223 and precipitate；Supernatant after precipitation
Liquid enters the 2nd PH regulating reservoirs 224, and TLA compound for treatment of electroplating wastes can be added in the 2nd PH regulating reservoirs 224, can carry out integration ring
Chemical reaction, while can be added lye with adjust waste water pH value be 8.0~8.5, water outlet enter transient response pond 225, mistake
It crosses setting blender in reaction tank 225 and carries out high-speed stirred to promote fully to react, the waste water after reaction enters middle transition pond
226, its flow can be controlled in middle transition pond 226, ensure middle transition pond 226 be pumped into the flows of the 3rd PH regulating reservoirs 227 with
The water flow in comprehensive adjustment pond 17 is identical, is conducive to ensure the stability of water process；It is pumped into the waste water of the 3rd PH regulating reservoirs 227
Can control its pH value is 9~10, and TLA compound for treatment of electroplating wastes is put into the 3rd PH regulating reservoirs 227, is then being made by stirring
It is fully reacted with water, and can be by all precipitation removals of the heavy metal in waste water after above-mentioned processing；3rd PH regulating reservoirs 227
Inside divide waste water that can flow into the second coagulating basin 228 and enter second coagulation processing, polyacrylamide solution (PAM) can be quantitatively adding,
Also suitable polymeric aluminum chlorides solution (PAC) can be added to enhance coagulation effect, the waste water after coagulation is in the second sedimentation basin 229
Mud-water separation is carried out, supernatant can enter intermediate pool 23, for use.
Biochemical reaction device 3 include sequentially connected PH readjustment pond 31, hydrolysis acidification pool 32, horizontal three phase fluidized bed 33 and
Synchronous precipitation pond 34, the water inlet end in PH readjustment pond 31 connect with intermediate pool 23, water outlet and the hydrolysis acidification pool 32
Connection；The sewage of intermediate pool 23 is pumped into PH readjustments pond 31, and dilute sulfuric acid is added into PH readjustments pond 31, its pH value is made to control
Between 6.5~7.5, adjusts the waste water after pH value and flow into progress anaerobic reaction in hydrolysis acidification pool 32, can be driven by blender
Waste water in dynamic hydrolysis acidification pool 32 is uniformly mixed with microorganism so that macromolecule organic acts on acidifying water in anaerobe
Solution, and then form a variety of organic acids, lactic acid, alcohols, carbon dioxide, hydrogen, ammonia, hydrogen sulfide etc.；Waste water after anaerobic reaction
Horizontal three phase fluidized bed 33 is flowed into, existing conventional horizontal three phase fluidized bed can be used, it can be to the dirt after Anaerobic Treatment
Water carries out Aerobic Process for Treatment, and declines above-mentioned small organic molecule in aerobic bacteria effect and aoxidize and remove ammonia nitrogen, aerobic in order to ensure
Treatment effeciency, the dissolved oxygen concentration in horizontal three phase fluidized bed 33 are 3~4mg/L, useless after above-mentioned anaerobism, Aerobic Process for Treatment
Water enters the precipitation of synchronous precipitation pond 34, and oettIed sewage can reach discharge standard.
In practical applications, which easily leads to ammonia dependent on being precisely controlled if control is bad
Nitrogen removal efficiency is low, that is, leads in discharge gas that there are nitrous oxide gas, to aggravate the deterioration of greenhouse effects, in view of
This, the horizontal three phase fluidized bed of an electric pole type can be used in the horizontal three phase fluidized bed of the present embodiment 33, as shown in Figure 2 comprising three-phase
Fluid bed 331, aeration mechanism 332, three-diemsnional electrode 333 and reflux mechanism 334.
The present embodiment three phase fluidized bed 331 includes simultaneous anaerobic treatment pool 331a, Aerobic Process for Treatment pond 331b, mudpan
331c, first partition 331d, second partition 331e and third partition board 331f, the first partition 331d are built in described and anaerobism
Processing pond 331a is simultaneously separated to form anaerobic zone a11 and aerobic area a12, and the second partition 331e is built in the aerobic place
Reason pond 331b is simultaneously separated to form First Transition area b11 and aerobic zone b12, and the third partition board 331f is built in the sludge
Sedimentation basin 331c is simultaneously separated to form the second transition region c11 and settling zone c12, the anaerobic zone a11, aerobic area a12, first
Transition region b11, aerobic zone b12, the second transition region c11 and settling zone c12 are sequentially communicated；Wherein, described in the present embodiment first every
The first gap for being connected to anaerobic zone a11 and aerobic area a12 is formed between plate 331d and the described and bottoms anaerobic treatment pool 331a,
It is formed between the second partition 331e and the Aerobic Process for Treatment pond bottoms 331b and is connected to First Transition area b11 and aerobic zone
The second gap of b12 is formed between the third partition board 331f and the bottoms the mudpan 331c and is connected to the second transition
The third space of area c11 and settling zone c12.Moreover, the water inlet pipe of the present embodiment three phase fluidized bed 331 is connect with anaerobic zone a11,
And aerobic area a12 is then connected to by the first vector separator 331g close to the aerobic area upper ends a12 with First Transition area b11, it is good
Oxygen area b12 and the second transition region c11 then passes through the Second support separator 331h connections close to the aerobic zone upper ends b12, sludge
An effluent weir is arranged far from the Aerobic Process for Treatment pond sides 331b in sedimentation basin 331c, and settling zone c12 can pass through third close to the upper end
Carrier separator 331i is connected to effluent weir 331j.It should be noted that due to the anaerobic zone a11 of the present embodiment, aerobic area
The sewage upper layer of a12, aerobic zone b12 and settling zone c12 are both provided with floating stuffing, therefore the present embodiment is detached using first vector
Device 331g, Second support separator 331h and third carrier separator 331i can avoid the spilling of floating stuffing.
It includes main aeration tube 332a, the first aeration plate group 332b and the second aeration plate group 332c to be aerated mechanism 332, and first exposes
Gas disk group 332b is made of multiple first aeration plates for being evenly arranged the aerobic area bottoms a12, and the second aeration plate group 332c is by uniform
Arrange that multiple second aeration plates of the aerobic zone bottoms b12 are constituted, multiple first aeration plates and the second aeration plate are respectively by passing through
First aeration valve and the second aeration valve are connected to main aeration tube 332a, and the first aeration valve and the second aeration valve are all made of flow valve,
Its controllable aeration quantity controlled respectively in aerobic area a12 and aerobic zone b12.
Three-diemsnional electrode 333 includes anode plate 333a, cathode plate 333b and activated carbon fiber layers 333c, the anode of the present embodiment
Plate 333a and cathode plate 333b is arranged in parallel in the tops the settling zone c12, the specially described anode plate 333a and cathode plate
333b is vertically arranged and is attached at the both sides inner wall setting of the settling zone c12 respectively, and the activated carbon fiber layers 333c is set
It is placed between anode plate 333a and cathode plate 333b, the light electrolysis effect between anode plate 333a and cathode plate 333b can be increased
Fruit, and then improve the removal efficiency of nitrous oxide.It is understood that the present embodiment anode plate 333a and cathode plate 333b also may be used
With horizontal setting up and down, when horizontal setting up and down, anode plate 333a and cathode plate 333b may be configured as porous structure or netted
Structure can from the bottom to top move convenient for sewage, and then ensure that the nitrous oxide in sewage comes into full contact with cathode plate 333b, into
And increase ammonia nitrogen removal effect.And in order to avoid the floating stuffing of settling zone c12 blocks anode plate 333a and cathode plate 333b, this
The anode plate 333a and cathode plate 333b of embodiment are preferably used and are vertically arranged, and in order to promote the light electrolysis of three-diemsnional electrode 333
The floating stuffing of effect, the present embodiment settling zone c12 preferably uses electric polarity carrier filler, such as activated carbon, and anaerobic zone
Electric polarity carrier filler can also be used in a11, aerobic area a12, the floating stuffing in the b12 of aerobic zone.
The reflux mechanism 334 includes a reflux pump 334a, the connection bottoms the second transition region c11 and reflux pump 334a
The first sludge out pipe 334b of water inlet end, the first mud valve 334c being set on the first sludge out pipe 334b, described in connection
Second sludge out pipe 334d of the water inlet end of the settling zone bottoms c12 and reflux pump 334a, on the second sludge out pipe 334d
Second mud valve 334e, the water outlet of the connection reflux pump 334a and the aerobic area bottoms a12 return duct 334f, be set to it is described
Return valve 334g on return duct 334f, the sludge pipe 334h being connect with the water outlet of the reflux pump 334a and it is set to the row
Mud valve 334i on mud pipe 334h；It can realize the reflux of sludge in mudpan 331c by a reflux pump 334a
And discharge, i.e., when needing returned sludge, then return valve 334g conductings, mud valve 334i are closed, and return valve 334g when spoil disposal
It is closed, mud valve 334i conducting, while the first mud valve 334c and the second mud valve 334e can be according to the second transition region c11 and heavy
The spoil disposal of shallow lake area c12 is connected.
When the horizontal three phase fluidized bed 33 of the present embodiment electric pole type carries out sewage disposal, sewage enters anaerobic zone by water inlet pipe
A11 simultaneously carries out anaerobic biochemical reaction, and the sewage of anaerobic zone a11 then enters aerobic area a12 by the first gap, can pass through control the
The oxygen amount of the aeration control aerobic area a12 of one aeration plate group 332b, and then control aerobic area a12 and facultative anaerobic biochemical occurs
Reaction, the sewage after reaction can be entered by first vector separator 331g overflows in First Transition area b11, First Transition area
Sewage in b11 can be flowed by the second gap in the b12 of aerobic zone, and the aeration quantity of the second aeration plate group 332c of control can be passed through
The oxygen amount of aerobic zone b12 is controlled, and then controls aerobic zone b12 and aerobic biochemical reaction, the sewage after aerobic reaction occurs
The second transition region c11 can be entered by Second support separator 331h, and settling zone c12 is flowed by third space, it can will be dirty
Sludge in water is precipitated；Sewage and sludge in mudpan 331c can be back to anaerobic zone by the mechanism 334 that flows back
A11 can flow into aerobic area a12 and carry out anti-nitration reaction to remove ammonia nitrogen；And treated that sewage can pass through by settling zone c12
It in three carrier separator 331i overflows to effluent weir 331j, can be handled by subsequent processing, can also be discharged；After processing
Sewage when being moved from bottom to top in settling zone c12, since settling zone c12 is provided with three-diemsnional electrode 333 close to top, lead to
Light electrolysis is generated after electricity, unreacted nitrous oxide in sewage can be reduced into nitrogen discharge, can avoid by cathode plate 333b
Nitrous oxide also avoids the aggravation of greenhouse efficiency by being overflowed in the sewage that is discharged.
Treated sewage reusing device 4 includes sequentially connected membrane bioreactor 41, reverse osmosis mechanism 42 and evaporation device 43, institute
The water inlet degree for stating membrane bioreactor 41 is connect with the synchronous precipitation pond 34, the supernatant after synchronous precipitation pond 34 is precipitated
In still contain a certain amount of COD and ammonia nitrogen, and the present embodiment can thoroughly be removed it by membrane bioreactor 41, and be passed through
Reverse osmosis mechanism 42 and evaporation device 43 carry out reverse osmosis and evaporation process successively, and then by water resource reuse therein.
The reverse osmosis mechanism 42 includes sequentially connected sand filtration mechanism 421, cartridge filter 422, first-stage reverse osmosis device
423, two-pass reverse osmosis device 424, electric Fenton device 425, nanofilter 426, three-level counter-osmosis device 427, the sand filtration mechanism 421
It connect, the sewage that membrane bioreactor 41 is handled can be filtered successively, reverse osmosis place with the membrane bioreactor 41
Reason, specially sand filtration are gone out large granular impurity in waste water, and cartridge filter 422 can remove wherein fine particle impurity, level-one
Treated that fresh water can be utilized directly for counter-osmosis device 423, and concentrated water can be handled by 424 after-treatment of two-pass reverse osmosis device
Concentrated water can by electric Fenton device 425 with by moieties therein removal, precipitation, then pass through nanofilter 426 filter
Afterwards, it is handled by three-level counter-osmosis device 427, the concentration of the concentration of the processing of three-level counter-osmosis device 427 is higher, can pass through evaporation device
43 are evaporated processing, and the evaporation device 43 includes evaporator 431 and condenser 432, the water inlet end of the evaporator 431 with
The connection of concentrated water end, outlet side and the condenser 432 of three-level counter-osmosis device 427 connect, and can be carried out concentrated water by evaporator 431
Evaporation process, the vapor after evaporation can be condensed into distilled water reuse by condenser 432, evaporate the crystallization of formation and above-mentioned heavy
The sludge in shallow lake can make dangerous material collection processing.
Water resource in electroplating wastewater can be carried out potability recycling profit by the present embodiment by the processing successively of above-mentioned technique
With also avoiding environmental pollution.
The specific implementation mode of present invention described above, is not intended to limit the scope of the present invention..Any basis
The various other corresponding changes and deformation that the technical concept of the present invention is made, should be included in the guarantor of the claims in the present invention
It protects in range.
Claims (10)
1. a kind of electroplating waste water treatment system, which is characterized in that including：
Pretreatment unit is used for by the cyanide wastewater broken cyanide and by oily waste water oil removing；
Coagulative precipitation device comprising sequentially connected broken chromium reaction tank, coagulating sedimentation mechanism and intermediate pool, the broken chromium are anti-
Pretreatment unit described in Ying Chiyu connects；
Biochemical reaction device comprising sequentially connected hydrolysis acidification pool and horizontal three phase fluidized bed, the hydrolysis acidification pool with
The intermediate pool connection；
Treated sewage reusing device comprising sequentially connected membrane bioreactor, reverse osmosis mechanism and evaporation device, the film biology
The water inlet degree of reactor is connect with the horizontal three phase fluidized bed.
2. electroplating waste water treatment system according to claim 1, which is characterized in that the pretreatment unit includes that broken cyanide is anti-
Ying Chi, broken cyanide regulating reservoir, oil separator, air supporting, inclined plate grease removal tank, fuel-displaced regulating reservoir and comprehensive adjustment pond, the oil separator, gas
Floating, inclined plate grease removal tank, fuel-displaced regulating reservoir and comprehensive adjustment pond are sequentially connected, and the water inlet end of the broken cyanide regulating reservoir is reacted with broken cyanide
Pond connection, water outlet and comprehensive adjustment pond connect.
3. electroplating waste water treatment system according to claim 2, which is characterized in that the coagulating sedimentation mechanism includes successively
Connection the first PH regulating reservoirs, the first coagulating basin, the first sedimentation basin, the 2nd PH regulating reservoirs, transient response pond, middle transition pond,
3rd PH regulating reservoirs, the second coagulating basin and the second sedimentation basin, the first PH regulating reservoirs are connect with the broken chromium reaction tank, described
Second sedimentation basin is connect with the intermediate pool.
4. electroplating waste water treatment system according to claim 3, which is characterized in that the biochemical reaction device further includes PH
It adjusts back pond and one synchronizes sedimentation basin, the water inlet end in PH readjustment pond connect with intermediate pool, water outlet and the hydrolysis acidification
Pond connects, and the synchronous precipitation pond is set between horizontal three phase fluidized bed and membrane bioreactor.
5. electroplating waste water treatment system according to claim 4, which is characterized in that the reverse osmosis mechanism includes connecting successively
Sand filtration mechanism, cartridge filter, first-stage reverse osmosis device, two-pass reverse osmosis device, electric Fenton device, nanofilter, the three-level connect is anti-
Permeator, the sand filtration mechanism are connect with the membrane bioreactor.
6. electroplating waste water treatment system according to claim 5, which is characterized in that the evaporation device include evaporator and
Condenser, the water inlet end of the evaporator is connect with the concentrated water end of three-level counter-osmosis device, outlet side and condenser connect.
7. a kind of electroplating effluent treatment method, which is characterized in that include the following steps：
(1) by electroplating wastewater cyanide wastewater and oily waste water carry out respectively broken cyanide processing and oil removal treatment after mix；
(2) mixed waste water is broken to stirring, precipitation after coagulant is added after chromium is handled；
(3) waste water after precipitation is subjected to anaerobism, Aerobic Process for Treatment successively；
(4) by step (3), treated that waste water carries out biomembrane, reverse osmosis, evaporation process successively.
8. electroplating effluent treatment method according to claim 7, which is characterized in that the broken chromium-treated pH value is 2.5
~3.0, the broken chromium agent being added is sodium pyrosulfite, and the potential value that the waste water of sodium pyrosulfite is added is 250~300mV.
9. electroplating effluent treatment method according to claim 7, which is characterized in that the coagulation being added in the step (2)
Agent is polyacrylamide.
10. electroplating effluent treatment method according to claim 7, which is characterized in that in the step (3) when aerobic reaction
Dissolved oxygen concentration is 3~4mg/L in waste water.
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