CN110498562A - Treatment method of high-concentration stripping liquid wastewater - Google Patents
Treatment method of high-concentration stripping liquid wastewater Download PDFInfo
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- CN110498562A CN110498562A CN201910728367.8A CN201910728367A CN110498562A CN 110498562 A CN110498562 A CN 110498562A CN 201910728367 A CN201910728367 A CN 201910728367A CN 110498562 A CN110498562 A CN 110498562A
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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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- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
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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
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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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
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
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- Hydrology & Water Resources (AREA)
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- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a method for treating stripping liquid wastewater, wherein the stripping liquid wastewater contains dimethyl sulfoxide and ethanolamine, and the method comprises the following steps: 1) adjusting the pH value of the wastewater to 8.5-10.0; 2) introducing the treated wastewater into a moving bed biomembrane reaction tank containing the rhizogenes and the thiobacillus for treatment, and controlling the pH value of the system in the treatment process to be 7-8; 3) introducing the treated wastewater into an anoxic tank for denitrification treatment; 4) introducing the treated wastewater into an anaerobic tank for ammoniation treatment to obtain NH containing free ammonia3And ammonium ion NH4 +The wastewater of (4); 5) introducing the treated wastewater into an aerobic tank for nitration reaction, controlling the pH value of a system in the treatment process to be 7-8, and making part of the wastewater in the aerobic tank flow back to an anoxic tank; 6) carrying out mud-water separation on the treated wastewater; the invention can effectively and efficiently treat stripping liquid wastewater with large capacity and high organic wastewater concentration。
Description
Technical field
The invention belongs to the processing of technical field of waste water processing more particularly to stripper waste water, and in particular to a kind of highly concentrated
Spend the processing method of stripper waste water.
Background technique
Currently, the strength of domestic especially liquid crystal display panel manufacturer, panel vendor constantly enhances, production capacity is significantly promoted,
Wherein will use positivity and/or negative photoresist stripper etc. during producing panel, these strippers generally in
Strong basicity, pH value is substantially 10 or more, and the major pollutants of these strippers are dimethyl sulfoxide (DMSO) and ethanol amine at present
(MEA), the intermediate product of DMSO such as (dimethyl disulfide) DMS can generate inhibition to microorganism, suppress growth of microorganism, MEA
It will lead to high COD concentration and high-concentration ammonia-nitrogen.When production capacity is less in the past, handled using physico-chemical process, it can barely
Reach lower discharge standard, but treatment effeciency is still lower and at high cost；And with the continuous promotion of production capacity, used by
Stripper dosage is equally significantly promoted, then the waste water accordingly generated also gradually increases, and the organic wastewater in waste water is dense because of its
Degree is high, has inhibition, is difficult to biodegrade, suffers from serious harm for ecological environment and human health, use is existing
Physico-chemical process has been difficult to this high concentration and the big stripper waste water of amount carries out effectively and efficient processing.
Summary of the invention
Based on the above issues, a kind of new the technical problem to be solved by the present invention is to overcome the deficiencies of the prior art and provide
Processing stripper waste water method, can be realized the stripper that efficiently and effectively treating capacity is big and organic wastewater concentration is high
Waste water.
In order to solve the above technical problems, the present invention adopts the following technical scheme:
A kind of processing method of stripper waste water, the stripper waste water include dimethyl sulfoxide and ethanol amine, the place
Reason method includes the following steps:
(1) pH value of the stripper waste water is adjusted to 8.5-10.0；
(2) by step (1), treated that stripper waste water is passed through the moving bed biological containing Hyphomicrobium and Thiobacillus
Film reaction pond is handled, and controls the pH value of system in treatment process in 7-8；
(3) by step (2) treated stripper waste water is passed through progress denitrification processing in anoxic pond；
(4) by step (3), treated that stripper waste water is passed through in anaerobic pond carries out ammoniated treatment, obtains containing free ammonia
NH3With ammonium ion NH4 +Stripper waste water；
(5) by step (4), treated that stripper waste water is passed through in aerobic tank carries out nitration reaction, controls in treatment process
The pH value of system makes to be partially stripped liquid return of waste water into the anoxic pond in the aerobic tank in 7-8；
(6) step (5) treated stripper waste water is subjected to mud-water separation.
In terms of more according to the present invention specific and preferred, in step (1), stripper waste water is adjusted using addition acid solution
PH value, the acid solution includes aqueous sulfuric acid.
Some preferred aspects according to the present invention, in step (2), treated that stripper waste water is moving for rate-determining steps (1)
The residence time is preferably greater than to be equal to 15h more than or equal to 10h, be more preferably higher than equal in dynamic bed biomembrane reaction pond
20h is further preferably greater than equal to for 24 hours.
It is raw to the moving bed during processing in step (2) in terms of more according to the present invention preferred and specific
Object film reaction pond is aerated.
It is more according to the present invention preferably and specific aspect, in step (4), microorganism fungus kind that the anaerobic pond contains
For anaerobic ammonia oxidizing bacteria.
Some preferred aspects according to the present invention, in step (4), the ORP of rate-determining steps (4) treated stripper waste water
Numerical value is in -500-300mv.
In terms of more according to the present invention preferred and specific, in step (5), dissolved oxygen numerical value in the aerobic tank is controlled
In 2-6mg/L.
In terms of more according to the present invention specific and preferred, in step (5), control the aerobic tank and be back to described lack
Stripper wastewater flow rate in oxygen pond and the stripper wastewater flow rate entered in the anoxic pond from the moving-bed biofilm reaction tank
Ratio be 1-2.5.
More according to the present invention specific and preferred aspect, in step (6), the mud-water separation in secondary settling tank into
Row, and the sludge being partially separated out is back to respectively in the moving-bed biofilm reaction tank and the anoxic pond, sludge returns
The ratio of flow and the stripper wastewater flow rate entered in secondary settling tank is 0.5-1.
More according to the present invention specific and preferred aspect, the processing method using stripper waste water treatment system into
Row wastewater treatment, the stripper waste water treatment system include the stripper wastewater equalization pond being sequentially communicated, stripper wastewater pH
It is worth conditioning tank, moving-bed biofilm reaction tank, anoxic pond, anaerobic pond, aerobic tank, secondary settling tank and outer blowoff basin；Wherein, described good
Oxygen pond is connected to the anoxic pond by the first return pipe, and the secondary settling tank and the moving-bed biofilm reaction tank pass through second
Return pipe connection, the anoxic pond are connected to by third return pipe with second return pipe.
Some specific aspects according to the present invention, the stripper waste water treatment system further include acid solution storage tank, lye storage
Slot, air blast blower, the acid solution storage tank are connected to the stripper pH value of waste water conditioning tank, the lye storage tank respectively with it is described
Stripper pH value of waste water conditioning tank, the moving-bed biofilm reaction tank are connected to the aerobic tank, and the air blast blower goes out
Air port is connected to the moving-bed biofilm reaction tank, the aerobic tank respectively.
Due to the adoption of the above technical solution, the invention has the following advantages over the prior art:
The present invention is matched by each treatment process of particular order, can not only to high concentration, containing there is inhibition
And the organic wastewater (especially including the stripper waste water of dimethyl sulfoxide and ethanol amine) for being difficult to degradable chemical realizes have
It imitates and efficiently handles, while treating capacity can greatly increase, fully meet after panel vendor's production capacity is promoted for wastewater treatment
High standards；Present invention process is simple simultaneously, and easy to operate, operating cost is lower, and producer is acceptant, answers convenient for promoting
With.
Detailed description of the invention
Fig. 1 is the process flow diagram of the processing method of high concentration stripper waste water of the invention；
Fig. 2 is the structural schematic diagram of secondary settling tank employed in the processing method of high concentration stripper waste water of the invention；
Wherein；1, stripper wastewater equalization pond；2, stripper pH value of waste water conditioning tank；3, moving-bed biofilm reaction tank；
4, anoxic pond；5, anaerobic pond；6, aerobic tank；7, secondary settling tank；71, first slope；72, the second slope；73, stirring system；731,
Driving mechanism；732, drive shaft；733, agitating paddle；7331, connector；7332, the first agitating plate；7333, the second agitating plate；
74, sludge outlet；8, outer blowoff basin；9, acid solution storage tank；10, lye storage tank；11, roots blower；12, organic sludge concentration basin；
A, the first return pipe；B, the second return pipe；C, third return pipe；D, agitating device.
Specific embodiment
COD is writing a Chinese character in simplified form for Chemical Oxygen Demand, refers to COD, refers to and handles water sample with strong oxidizer
When, consumed oxidant content, it is an index for indicating reducing substances are how many in water, and the reducing substances in water are main
Refer to organic matter, therefore, COD is to measure the how many index of Organic substance in water matter content, and COD value is bigger, illustrates water body by organic matter
Pollution it is more serious, the measuring method of COD can use potassium dichromate standard method, and principle is: being added in water sample a certain amount of
Potassium bichromate and catalyst sulfuric acid silver, are heated to reflux, part potassium bichromate is by oxidizable substance in water sample in strong acid medium
Reduction titrates remaining potassium bichromate with iron ammonium sulfate, and the value of COD is calculated according to the amount of consumption potassium bichromate, is denoted as
CODCr, COD is higher, means that the organic pollution of water is more serious.
NH3N refers in water with free ammonia (NH3) and ammonium ion (NH4+) nitrogen existing for form, detection method usually has Na Shi
Colorimetric method, phenol-hypochlorite (or salicylic acid-hypochlorite) colorimetric method and electrode method etc., the ammonia nitrogen in water can be certain
Under the conditions of be converted to nitrite, if long-term drinking, nitrite in water will combine with protein and form nitrosamine, this is
A kind of strong carcinogen, totally unfavorable to human health, ammonia nitrogen plays the mainly free ammonia of damaging effect, toxicity to aquatic organism
It is more several ten times larger than ammonium salt, and increase with the enhancing of alkalinity.Below with reference to specific embodiment to technical solution of the present invention and
Its advantage is described in detail.
Embodiment 1-6
This little embodiment provides a kind of processing method of stripper waste water, the stripper waste water include dimethyl sulfoxide and
Ethanol amine the treating method comprises following steps:
(1) pH value of the stripper waste water is adjusted by the way of adding aqueous sulfuric acid to 9 ± 0.2；
(2) by step (1), treated that stripper waste water is passed through the moving bed biological containing Hyphomicrobium and Thiobacillus
Film reaction pond is handled for 24 hours, carries out Air Exposure simultaneously in the process, controls the pH value of system in treatment process 7.5
± 0.2 (pH value that system can be maintained by adding sodium hydrate aqueous solution) is, it can be achieved that be converted into sulphur for dimethyl sulfoxide
Acid group；
(3) by step (2), treated that stripper waste water is passed through carries out denitrification processing in anoxic pond and (can occur as next
A little reactions: NO2 -+3H→0.5N2+H2O+OH-、NO3 -+5H→0.5N2+2H2O+OH-)；
(4) by step (3) treated stripper waste water is passed through containing microorganism fungus kind be detesting for anaerobic ammonia oxidizing bacteria
Ammoniated treatment is carried out in oxygen pond, is obtained containing free ammonia NH3With ammonium ion NH4 +Stripper waste water, control treated removing
The ORP numerical value of liquid waste water is in 100 ± 50mv；
(5) by step (4), treated that stripper waste water is passed through carries out nitration reaction in aerobic tank and (can occur following anti-
It answers: NH4 ++2O2→NO3 -+H2O+2H+), the pH value of system in treatment process is controlled 7.5 ± 0.2, and is made in the aerobic tank
Be partially stripped liquid return of waste water into the anoxic pond (control aerobic tank be back to stripper wastewater flow rate in anoxic pond with from
The ratio that moving-bed biofilm reaction tank enters the stripper wastewater flow rate in anoxic pond is 2), to control dissolved oxygen numerical value in aerobic tank
In 4 ± 1mg/L；
(6) step (5) treated stripper waste water is subjected to mud-water separation, supernatant qualified discharge, the muddy water point
Carried out from secondary settling tank, and by the sludge being partially separated out be back to respectively the moving-bed biofilm reaction tank and it is described lack
In oxygen pond, the ratio of sludge reflux amount and the stripper wastewater flow rate entered in secondary settling tank is 0.8.
Wherein, above-mentioned processing method is specifically operated using following stripper waste water treatment system: as shown in Figs. 1-2,
Stripper waste water treatment system includes the stripper wastewater equalization pond 1 being sequentially communicated (can be by all stripper waste water of collection
Mixed to obtain the waste water of relatively stable pH value), stripper pH value of waste water conditioning tank 2, moving-bed biofilm reaction tank
(pond MBBR) 3, anoxic pond 4, anaerobic pond 5, aerobic tank 6, secondary settling tank 7 and outer blowoff basin 8；Wherein, aerobic tank 6 and anoxic pond 4 are logical
The first return pipe a connection is crossed, secondary settling tank 7 is connected to moving-bed biofilm reaction tank 3 by the second return pipe b, and anoxic pond 4 passes through
Third return pipe c is connected to the second return pipe b.
In this example, stripper waste water treatment system further includes acid solution storage tank 9, lye storage tank 10, air blast blower, acid solution storage tank
9 are connected to stripper pH value of waste water conditioning tank 2, lye storage tank 10 respectively with stripper pH value of waste water conditioning tank 2, moving bed biological
Film reaction pond 3 is connected to aerobic tank 6, and the wind outlet of air blast blower is connected to moving-bed biofilm reaction tank 3, aerobic tank 6 respectively.
Specifically, the air blast blower of this example is roots blower 11, and for storing aqueous sulfuric acid, lye storage tank 10 is used for acid solution storage tank 9
Sodium hydrate aqueous solution is stored, air blast blower into moving-bed biofilm reaction tank 3, aerobic tank 6 for being aerated.
In this example, anoxic pond 4, aerobic tank 6 respectively include agitating device d, and agitating device d includes support carriers and support
The support rod that support is detachably connected and vertically extends, and setting are used to drive stripper useless in support rod lower end
The rabbling mechanism that water moves in the horizontal direction.Specifically, rabbling mechanism is located at the bottom of anoxic pond 4 or aerobic tank 6；Wherein, it stirs
Mixing mechanism includes the motor for capableing of underwater operation and the impeller with the output end transmission connection of motor, the Plane of rotation of impeller
It for vertical plane, and then may be implemented that stripper waste water is pushed to move in the horizontal direction, be conducive to muddy water mixing.
In this example, stripper waste water treatment system further includes organic sludge concentration basin 12, organic sludge concentration basin 12 and two
Heavy pond 7 is connected to, for storing the sludge of discharge.
In this example, the top of stripper pH value of waste water conditioning tank 2, the top of moving-bed biofilm reaction tank 3, anoxic pond 4
Top, the top of anaerobic pond 5, the top of aerobic tank 6 and secondary settling tank 7 top offer overflow port, stripper waste water respectively
PH value conditioning tank 2 is connected to moving-bed biofilm reaction tank 3 by the overflow port of stripper pH value of waste water conditioning tank 2, moving bed
Biomembrane reaction pond 3 is connected to anoxic pond 4 by the overflow port of moving-bed biofilm reaction tank 3, and anoxic pond 4 and anaerobic pond 5 are logical
The overflow port connection of anoxic pond 4 is crossed, anaerobic pond 5 is connected to aerobic tank 6 by the overflow port of anaerobic pond 5, aerobic tank 6 and secondary settling tank
7 are connected to by the overflow port of aerobic tank 6, and secondary settling tank 7 is connected with outer blowoff basin 8 by the overflow port of secondary settling tank 7.Above-mentioned setting
Enable and circulate in stripper waste water in the present invention overflow port possessed by respective and next processing station for abutting,
The defects of can blocking caused by Pipeline transport to avoid long range.
In this example, the bottom of secondary settling tank 7 is provided with first slope 71 and the second slope 72, first slope 71 and the second slope
72 composition angles are the V-type at obtuse angle, and the bottom connection on the bottom of first slope 71 and the second slope 72 is formed with sludge and goes out
Mouth 74, is conducive to the outflow of sludge；Further, secondary settling tank 7 further includes stirring system 73, and stirring system 73 includes being arranged two
The driving mechanism 731 of heavy 7 upper end of pond, the drive shaft 732 being mutually sequentially connected with the output end of driving mechanism 731, and with drive
The detachably connected agitating paddle 733 of moving axis 732；Wherein drive shaft 732 vertically extends, and agitating paddle 733 includes multiple
The connector 7331 mutually detachably connected with the lower part of drive shaft 732 respectively, and respectively and in multiple connectors 7331
Part the first agitating plate 7332 and the second agitating plate 7333 that are fixedly connected, the extending direction and first of the first agitating plate 7332
Slope 71 is identical, and the extending direction of the second agitating plate 7333 is identical as the second slope 72, the first agitating plate 7332 and the second stirring
Plate 7333 constitutes angle and is the V-type at obtuse angle, to realize the phase interworking of stirring system 73 with first slope 71, the second slope 72
It closes, can either sufficiently stir evenly internal mud mixture, and can be convenient the outflow of sludge.
To the organic wastewater of Fujian panel enterprise (major pollutants are dimethyl sulfoxide (DMSO) and ethanol amine (MEA))
It is handled, sampled analysis, produce the fundamental property of waste water: CODcr:800-2500mg/L, pH are 10~12, NH3N is
100-400mg/L, waste water yield are 1800m3/d。
After the processing of above-mentioned processing method, as a result as shown in the table (in following, each embodiment represents 1 actual measurement work
Condition):
As can be seen from the above table, the stripper waste water generated in faceplate manufacturing process is in strong basicity, and big containing toxicity, difficult
With biodegrade, after the adjusted pH value of the waste water to suitable range, after being handled by the above method, COD removal rate is 95%
More than, NH3N removal rate is discharged 90% or more up to national grade one discharge standard.The present invention has high treating effect, processing
Advantage at low cost can be widely applied to the processing of panel factory stripper organic wastewater, and treated, and waste water can direct row up to standard
It puts, can also be used as the preprocess method of the organic wastewater of high concentration.
The above embodiments merely illustrate the technical concept and features of the present invention, and its object is to allow person skilled in the art
Scholar cans understand the content of the present invention and implement it accordingly, and it is not intended to limit the scope of the present invention, it is all according to the present invention
Equivalent change or modification made by Spirit Essence, should be covered by the protection scope of the present invention.
Claims (10)
1. a kind of processing method of stripper waste water, the stripper waste water includes dimethyl sulfoxide and ethanol amine, and feature exists
In the treating method comprises following steps:
(1) pH value of the stripper waste water is adjusted to 8.5-10.0；
(2) by step (1), treated that stripper waste water is passed through the moving-bed biofilm containing Hyphomicrobium and Thiobacillus is anti-
It answers pond to be handled, controls the pH value of system in treatment process in 7-8；
(3) by step (2) treated stripper waste water is passed through progress denitrification processing in anoxic pond；
(4) by step (3), treated that stripper waste water is passed through in anaerobic pond carries out ammoniated treatment, obtains containing free ammonia NH3With
Ammonium ion NH4 +Stripper waste water；
(5) by step (4), treated that stripper waste water is passed through in aerobic tank carries out nitration reaction, controls system in treatment process
PH value in 7-8, and make to be partially stripped liquid return of waste water into the anoxic pond in the aerobic tank；
(6) step (5) treated stripper waste water is subjected to mud-water separation.
2. the processing method of stripper waste water according to claim 1, which is characterized in that in step (1), using addition acid
Liquid adjusts the pH value of stripper waste water, and the acid solution includes aqueous sulfuric acid.
3. the processing method of stripper waste water according to claim 1, which is characterized in that in step (2), rate-determining steps
(1) treated the stripper waste water residence time in moving-bed biofilm reaction tank is more than or equal to 10h, preferably greater than etc.
In 15h, more preferably higher than it is equal to 20h, is further preferably greater than equal to for 24 hours；And/or in step (2), in treatment process
In the moving-bed biofilm reaction tank is aerated.
4. the processing method of stripper waste water according to claim 1, which is characterized in that in step (4), the anaerobic pond
The microorganism fungus kind contained is anaerobic ammonia oxidizing bacteria.
5. the processing method of stripper waste water according to claim 1, which is characterized in that in step (4), rate-determining steps
(4) the ORP numerical value of treated stripper waste water is in -500-300mv.
6. the processing method of stripper waste water according to claim 1, which is characterized in that in step (5), it is described good to control
Dissolved oxygen numerical value is in 2-6mg/L in oxygen pond.
7. the processing method of stripper waste water according to claim 1, which is characterized in that in step (5), it is described good to control
Oxygen pond is back to the stripper wastewater flow rate in the anoxic pond and enters the anoxic pond with from the moving-bed biofilm reaction tank
In stripper wastewater flow rate ratio be 1-2.5.
8. the processing method of stripper waste water according to claim 1, which is characterized in that in step (6), the muddy water point
Carried out from secondary settling tank, and by the sludge being partially separated out be back to respectively the moving-bed biofilm reaction tank and it is described lack
In oxygen pond, the ratio of sludge reflux amount and the stripper wastewater flow rate entered in secondary settling tank is 0.5-1.
9. the processing method of stripper waste water described in any one of -8 claims according to claim 1, which is characterized in that institute
It states processing method and wastewater treatment is carried out using stripper waste water treatment system, the stripper waste water treatment system includes successively connecting
It is logical stripper wastewater equalization pond, stripper pH value of waste water conditioning tank, moving-bed biofilm reaction tank, anoxic pond, anaerobic pond, good
Oxygen pond, secondary settling tank and outer blowoff basin；Wherein, the aerobic tank is connected to the anoxic pond by the first return pipe, and described two is heavy
Pond is connected to the moving-bed biofilm reaction tank by the second return pipe, and the anoxic pond passes through third return pipe and described the
The connection of two return pipes.
10. the processing method of stripper waste water according to claim 9, which is characterized in that the stripper wastewater treatment
System further includes acid solution storage tank, lye storage tank, air blast blower, and the acid solution storage tank and the stripper pH value of waste water conditioning tank connect
It is logical, the lye storage tank respectively with the stripper pH value of waste water conditioning tank, the moving-bed biofilm reaction tank and described good
The connection of oxygen pond, the air outlet of the air blast blower are connected to the moving-bed biofilm reaction tank, the aerobic tank respectively.
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