CN101973662B - Method and system for treating industrial wastewater of photovoltaic solar cell plates - Google Patents
Method and system for treating industrial wastewater of photovoltaic solar cell plates Download PDFInfo
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- CN101973662B CN101973662B CN2010102860714A CN201010286071A CN101973662B CN 101973662 B CN101973662 B CN 101973662B CN 2010102860714 A CN2010102860714 A CN 2010102860714A CN 201010286071 A CN201010286071 A CN 201010286071A CN 101973662 B CN101973662 B CN 101973662B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/20—Controlling water pollution; Waste water treatment
- Y02A20/208—Off-grid powered water treatment
- Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
The invention discloses a process for treating industrial wastewater of photovoltaic solar cell plates. The process comprises the following steps of: collecting wastewater, namely collecting acid wastewater and alkaline wastewater respectively; regulating pH, namely adding strong acid or strong base into the acid wastewater, alkaline wastewater or acid-alkaline mixed wastewater mixed by the acid wastewater and the alkaline wastewater, and regulating the pH value to be between 8.0 and 8.5 to form conditioning fluid; defluorinating the conditioning fluid and/or removing chemical oxygen demand (COD) from the conditioning fluid, wherein the defluorinating step means throwing calcium salt into the conditioning fluid so as to remove fluorion from the wastewater, and the COD removing step means performing incomplete anaerobic reaction on the conditioning fluid; performing aerobic biological treatment; and sequentially completing the steps to discharge the wastewater meeting the discharge standard. The invention provides a treatment process aiming at the water quality characteristics of the industrial wastewater of the photovoltaic solar cell plates and main design operational parameters. By a treatment system, the fluorion can be effectively removed, the fluorion concentration of effluent can be reduced to be below 10mg/L, and the wastewater CODCr is below 300mg/L and meets the discharge standard. Meanwhile, the invention also provides a system for treating the industrial wastewater of the photovoltaic solar cell plates.
Description
Technical field
The present invention relates to waste water treatment process, relate to particularly a kind for the treatment of process and applied Waste Water Treatment of the method for photovoltaic solar cell sheet factory effluent.
Background technology
Under the pressure of global energy crisis and climate warming, the development of renewable New Energy Industry more and more receives publicity.The inexhaustible clean energy that utilizes the Nature to give such as development sun power, can not only solve the problem of future source of energy shortage, and can solve for a long time the environmental problem that the fossil oil of mankind's dependence causes.
Under the promotion of policy, rules and the action plan of government, the production of solar cell is just with the looks rapid growth of a sunrise industry.In in the past 15 years, global photovoltaic industry is with 25% average annual rate increase, and the average annual compound rate of growth of global photovoltaic system installation was up to 49.1% in 2000～2009.In China, government also pays much attention to the development of solar energy industry.Hu Jintao secretary's once important written instructions in " about supporting the suggestion of China's sun power autonomous innovation gordian technique " report are pointed out: sun power is one of important renewable energy source, advance scientific and technical innovation, solving the expensive problem of solar electrical energy generation is the key that large-scale develops and utilizes sun power.China's solar cell production high speed development from 2002, average growth rate per annum reaches 180%.The solar product manufacturing enterprise of China is above 500 at present.
Yet as the sunrise industry of producing clean energy, the manufacture of solar cells process is also unclean.In the processes such as cutting, corrosion and rinsing that crystalline silicon is produced, can produce high pollution waste water.Also can produce waste water in the processes such as making herbs into wool, etching, rinsing and evaporation of the solar battery sheet course of processing, these manufacture of solar cells waste water have following characteristics:
1) the waste water acid-basicity is extremely strong;
2) fluorinion concentration is high, and fluorinion concentration is often at several thousand even several ten thousand ppm;
3) total dissolved solidss content is large, owing to adopting a large amount of strong acid and strong bases in the manufacture of solar cells, brings a large amount of mineral ions in the waste discharge into, causes total dissolved salt content high;
4) adopt organic solvent to cause the chemical oxygen demand (COD) that contains higher concentration in the waste discharge in the manufacture of solar cells.
The These characteristics of the waste water that produces for the production process of following this solar cell, for the production wastewater treatment of photovoltaic solar cell has been brought following difficult point:
1) pH regulator consumption acids alkali number is large;
2) content of fluoride ion is high, needs to select reasonable medicament and treatment process just can reach the following emission standard of 10mg/L;
3) total dissolved salt is high, and owing to adding a large amount of medicaments in the removal fluorion process, cause the total salt amount of waste water high, and hardness is high, and the traditional biological treatment system is caused inhibition, and the COD removal effect is undesirable.
Be regarded as green sunrise industry in China's manufacture of solar cells at present.And the environmental pollution that its factory effluent causes is not sufficiently paid attention to.Existing many enterprises only adopt simple flocculation sediment, add methods adjusting pH and the removal part fluorine such as carbide slag or lime for this waste water, fluorine content still exceeds standard in its waste discharge, bring serious secondary pollution into, and the COD that large amount of organic causes does not remove; Simultaneously, also have Some Enterprises to adopt the traditional biological treatment system, but because manufacture of solar cells waste water acid-basicity is extremely strong, need to add a large amount of medicaments before entering biological treatment, cause in the waste water saltiness up to more than 2%, waste water hardness is high, like this, the simple inhibition of adopting the traditional biological treatment system to tend to be subject to high salt and high rigidity, the biological treatment effect extreme difference, COD removes undesirable, discharge of wastewater is not up to standard, directly discharging then causes serious problem of environmental pollution, enters city planting ductwork and then the downstream Sewage Plant is brought larger impact load, even affect its normal operation.
Although the development trend of this sunrise industry of manufacture of solar cells is had an optimistic view of in the many areas of China at present, because the environmental protection pressure in the manufacture of solar cells forces many manufacture of solar cells projects to have to halt or shelve.
Therefore, be badly in need of the strong acid-base that discharges for this photovoltaic solar cell production, high saliferous, high fluorine and the efficient cheap treatment technology of high COD trade effluent exploitation, satisfy qualified discharge or regeneration requirement.
Summary of the invention
The objective of the invention is provides a kind for the treatment of process and system of photovoltaic solar cell sheet factory effluent for above-mentioned photovoltaic solar cell sheet factory effluent characteristics and difficulty in treatment.The method flow process is simple, and working cost is lower, and level of automation is high, can solve the difficult problem of the current photovoltaic solar industry of puzzlement wastewater treatment.
For this reason, the invention provides a kind of photovoltaic solar cell sheet production wastewater treatment technique, technique may further comprise the steps: wastewater collection, collect respectively acid waste water and alkaline waste water; PH regulator, oxytropism waste water, alkaline waste water or mixed in the soda acid composite waste that forms by acid waste water and alkaline waste water add strong acid or highly basic, regulate pH value to 8.0～8.5, the formation treatment solution; Treatment solution is carried out defluorination and/or removes the COD step; The defluorination step is to drop into calcium salt in treatment solution, to remove the fluorion in the waste water; Except the COD step is that treatment solution is carried out incomplete anaerobic reaction; Carrying out aerobe processes again; Finish successively above-mentioned steps, the waste water that will reach emission standard effluxes.
According to further improvement of the present invention, the wastewater collection process further comprises: collect respectively acid waste water and alkaline waste water, hydraulic detention time is greater than 8h.
According to further improvement of the present invention, the defluorination process further comprises: the one-level defluorination, drop into calcium salt in the waste water that regulates the pH value, the input amount of calcium salt and the mass ratio of fluorion are 4: 1～5: 1, stirring reaction 20～30min, precipitation 1～2h, scavenger precipitation chemical sludge.
According to further improvement of the present invention, the defluorination process further comprises: the secondary defluorination, drop into calcium salt again in the waste water through one-level defluorination process, the input amount of calcium salt is 500～1000mg/L, stirring reaction 20～30min, precipitation 2h, scavenger precipitation chemical sludge.
According to further improvement of the present invention, further comprise in the secondary defluorination process: when dropping into calcium salt, add 100～200mg/L flocculation agent, and the coagulant aids of 3～8mg/L.
According to further improvement of the present invention, the defluorination process further comprises: carry out concentration to precipitating the chemical sludge that produces in the defluorination process, outward transport landfill after the thickened sludge dehydration is disposed or is carried out the advanced treatment of the resource recovery of fluorine, concentrating filtrate turns back to the pH regulator step, continues to process.
According to further improvement of the present invention, aerobe is processed and is further comprised: the biochemical sludge part of discharging in the aerobe treating processes is applied in the aerobe treating processes again; Excess sludge is carried out concentration, and the biochemical sludge after concentrating is transported outward after processed or compost is disposed, and concentrating filtrate turns back to incomplete anaerobic reaction step, continues to process.
According to further improvement of the present invention, employed calcium salt is CaCl in the above-mentioned technique
2Flocculation agent is Al
2(SO
4)
3, polyaluminium sulfate; Coagulant aids is polyacrylamide.
According to further improvement of the present invention, except in the COD step, not exclusively the time of anaerobic reaction is 8～12h.
According to further improvement of the present invention, except in the COD step, the hydraulic detention time of aerobe treating processes is greater than 20h, and sludge concentration is 3000～4000mg/L, reaction postprecipitation 1～2h.
Simultaneously, a kind of Waste Water Treatment also is provided in the present invention, and the waste water for the treatment of producing in the photovoltaic solar cell sheet production process comprises: the wastewater collection pond, comprise acid waste water pond and alkaline waste water pond, be used for collecting respectively acid waste water and alkaline waste water; The pH regulator pond is connected respectively with acid waste water pond and alkaline waste water pond, and the pH regulator pond is provided with the soda acid dog-house, is used for adding strong acid or the highly basic of regulating waste water ph; The defluorination unit, in order to remove the fluorion in the waste water, the defluorination unit comprises reaction tank and settling tank, and pH regulator pond, reaction tank and settling tank sequentially connect, and reaction tank is provided with dog-house; Settling tank is provided with chemical sludge relief outlet and water outlet; Not exclusively anaerobic reation pool links to each other with water outlet and the pH regulator pond of settling tank in the defluorination unit respectively, is used for carrying out incomplete anaerobic reaction; The aerobe reaction member, being used for carrying out aerobe processes, comprise aerobe reaction tank and biochemical sedimentation basin, not exclusively anaerobic reation pool, aerobe reaction tank and biochemical sedimentation basin sequentially connect, and biochemical sedimentation basin is provided with waste water and effluxes mouth and biochemical sludge relief outlet.
According to the present invention, comprise two defluorination unit that sequentially connect, the first defluorination unit: comprise the first reaction tank and the first settling tank, be used for finishing the one-level defluorination; The second defluorination unit: comprise the second reaction tank and the second settling tank; Finish the secondary defluorination; The second reaction tank is connected with the water outlet of the first settling tank; The first reaction tank in the first defluorination unit is connected with the pH regulator pond, and the water outlet of the second settling tank in the second defluorination unit is connected with incomplete anaerobic reation pool.
According to further improvement of the present invention, also comprise sludge thickener, sludge thickener comprises: the chemical sludge concentration basin, and the chemical sludge that is used for the defluorination unit is produced carries out concentration, and the chemical sludge concentration basin is connected with the chemical sludge relief outlet of each settling tank in the defluorination unit.The biochemical sludge concentration basin, the biochemical sludge that is used for the aerobe treating processes is discharged carries out concentration, and the biochemical sludge concentration basin links to each other with the biochemical sludge relief outlet of biochemical sedimentation basin.
According to further improvement of the present invention, all be provided with whipping appts in each reaction tank in pH regulator pond and the defluorination unit.
According to further improvement of the present invention, be provided with online pH monitor in the pH regulator pond, be used for pH value in the measuring cell.
Beneficial effect of the present invention is: the invention provides treatment process and main design and operation parameter for photovoltaic solar factory effluent water quality characteristics, adopt this treatment system, can effectively remove fluorion, the water outlet fluorinion concentration is reduced to below the 10mg/L, simultaneity factor has been eliminated the restraining effect of high saliferous and hardly degraded organic substance, guarantee that biochemical system can normally move, process waste discharge COD
Cr(chemical oxygen demand that adopts potassium bichromate to determine as oxygenant) is below the 300mg/L.Waste water can directly discharge or reach and receive pipe standards and enter downstream sewage centralized treatment plant after treatment.
Description of drawings
Accompanying drawing consist of this specification sheets a part, be used for further understanding the present invention, accompanying drawing shows the preferred embodiments of the present invention, and is used for illustrating principle of the present invention with specification sheets.Among the figure:
Fig. 1 shows the schema of a kind for the treatment of process of photovoltaic solar cell sheet factory effluent according to the present invention.
Embodiment
Be noted that following detailed description all is exemplary, is intended to the invention provides further instruction.Unless otherwise, all technology used herein and scientific terminology have the identical meanings of usually understanding with the general technical staff of the technical field of the invention.
As shown in Figure 1, a kind of schema for the treatment of process of photovoltaic solar cell sheet factory effluent has been shown according to the present invention among Fig. 1.Wherein the step of solid line connection is explained the sewage disposal step, and the step that dotted line connects represents the sludge treatment step.
In a kind of typical embodiment of the present invention, a kind of photovoltaic solar cell sheet production wastewater treatment technique may further comprise the steps: collect respectively acid waste water and alkaline waste water in acid waste water pond and alkaline waste water pond; Oxytropism waste water, alkaline waste water or mixed in the soda acid composite waste that forms by acid waste water and alkaline waste water add strong acid or highly basic, regulate pH value to 8.0～8.5, the formation treatment solution.Treatment solution is carried out defluorination and/or removes the COD step; Wherein, the defluorination step is to drop into calcium salt in treatment solution, to remove the fluorion in the waste water; Except the COD step is that treatment solution is carried out incomplete anaerobic reaction; Carrying out aerobe processes again; Finish successively above-mentioned steps, the waste water that will reach emission standard effluxes.
In the photovoltaic solar cell sheet production wastewater treatment technique of the present invention, acid waste water and alkaline waste water can individual curing, also can mix aftertreatment.According to the kind of handled waste water in the pH regulator process, those skilled in the art are easy to judge in the subsequent processes and should carry out defluorination and/or remove the COD step treatment solution; As adding highly basic adjusting pH to 8.0～8.5 for being treated in the acid waste water of collecting of separate acid wastewater, form treatment solution, treatment solution is transported to the defluorination unit, in treatment solution, drop into calcium salt in the defluorination unit, with the fluorion in the Transformatin liquid; Make fluorinion concentration less than 10mg/L, satisfy the backward outer discharging of emission standard.Add strong acid for adjusting pH to 8.0～8.5 for being treated in the alkaline waste water of collecting of alkaline waste water, form treatment solution, treatment solution is carried out incomplete anaerobic reaction; Carrying out aerobe processes again; Make treatment solution COD
CrLess than 300mg/L, satisfy the backward outer discharging of emission standard.For the soda acid composite waste, can utilize the spent acid salkali waste to regulate mutually pH, part realizes the treatment of wastes with processes of wastes against one another, reduces the input amount of strong acid and strong base.The soda acid composite waste is regulated pH to 8.0～8.5 in the pH regulator pond by adding strong acid or highly basic, forms treatment solution, and treatment solution is transported to the defluorination unit, drops into calcium salt in the defluorination unit in treatment solution, with the fluorion in the Transformatin liquid; The treatment solution of finishing the defluorination step is carried out incomplete anaerobic reaction; Carry out again aerobe and process removal COD.After finishing above-mentioned steps successively, the waste water that will reach emission standard effluxes.
Preferably, in the above-mentioned waste water treatment process, acid waste water and alkaline waste water respectively the hydraulic detention time in acid waste water pond and alkaline waste water pond all greater than 8h.
Preferably, in the pH regulator pond, carry out the pH regulator hydraulic detention time in the above-mentioned waste water treatment process and be not less than 30min.
Preferably, in a kind of preferred implementation of the present invention, the defluorination process of above-mentioned waste water treatment process further comprises: the one-level defluorination, in the waste water that regulates the pH value, drop into calcium salt, the input amount of calcium salt and the mass ratio of fluorion are 4: 1～5: 1, stirring reaction 20～30min, precipitation 1～2h regularly discharges precipitating sludge to the chemical sludge concentration basin.More preferably, above-mentioned defluorination process further comprises: the secondary defluorination, drop into calcium salt again in the waste water through one-level defluorination process, the input amount of calcium salt is 500～1000mg/L, stirring reaction 20～30min, precipitation 2h regularly discharges precipitating sludge to the chemical sludge concentration basin.More preferably further comprise in the secondary defluorination process: when dropping into calcium salt, add 100～200mg/L flocculation agent, and the coagulant aids of 3～8mg/L.Operable calcium salt includes but not limited to CaCl in the present invention
2Operable flocculation agent includes but not limited to Al in the present invention
2(SO
4)
3, polyaluminium sulfate; Operable coagulant aids includes but not limited to polyacrylamide in the present invention; Step through secondary defluorination among the present invention can be reduced to the fluorinion concentration in the waste water below the 10mg/L, but reaches the emission standard of fluorinion in waste water.
Preferably, in the above-mentioned waste water treatment process, the hydraulic detention time of waste water in incomplete anaerobic reation pool is controlled at 8～12h in the process of removal COD.
Preferably, in the above-mentioned waste water treatment process, remove in the process of COD, the hydraulic detention time of waste water in the aerobe reaction tank is greater than 20h, and sludge concentration is 3000～4000mg/L, reaction postprecipitation 1～2h.
In a kind of preferably embodiment of the present invention, in order to improve resource utilization, also in order to reduce pollution, defluorination process in waste water treatment process of the present invention further comprises: the chemical sludge that produces in the defluorination process is carried out concentration, the resource recovery of fluorine be disposed or be carried out to chemical sludge after concentrated can by the outward transport landfill after dehydration, concentrating filtrate turns back to the pH regulator step, continues to process.Simultaneously, further comprise in the aerobe treating processes: the sludge part of discharging in the aerobe treating processes is applied in the aerobe treating processes again, excess sludge is carried out concentration, biochemical sludge after concentrated is transported outward after processed or compost is disposed, concentrating filtrate turns back to incomplete anaerobic reaction step, continues to process.
Simultaneously, in order to realize above-mentioned waste water treatment process by efficiently and effectively, a kind of Waste Water Treatment also is provided in the present invention, for the treatment of the waste water that produces in the photovoltaic solar cell sheet production process, this system comprises: wastewater collection pond, pH regulator pond, defluorination unit, incomplete anaerobic reation pool, aerobe reaction member.The wastewater collection pond comprises acid waste water pond and alkaline waste water pond, is used for collecting respectively acid waste water and alkaline waste water.The pH regulator pond is connected respectively with acid waste water pond and alkaline waste water pond, and the pH regulator pond is provided with the soda acid dog-house, is used for adding strong acid or the highly basic of regulating waste water ph.The defluorination unit, in order to remove the fluorion in the waste water, this defluorination unit comprises reaction tank and settling tank, wherein pH regulator pond, reaction tank and settling tank sequentially connect.Be provided with dog-house at reaction tank, be used for dropping into calcium salt and the flocculation agent that to remove fluorinion in waste water, coagulant aids etc.The first settling tank is provided with chemical sludge relief outlet and water outlet.Finishing the liquid of separate acid wastewater treating processes can directly get rid of by water outlet.Not exclusively water port and the pH regulator pond of settling tank links to each other respectively in anaerobic reation pool and the defluorination unit, for carrying out incomplete anaerobic reaction; The aerobe reaction member is used for carrying out aerobe to be processed, comprise aerobe reaction tank and biochemical sedimentation basin, not exclusively anaerobic reation pool, aerobe reaction tank and biochemical sedimentation basin sequentially connect, and wherein, biochemical sedimentation basin is provided with waste water and effluxes mouth and biochemical sludge relief outlet.
Preferably, this Waste Water Treatment, comprise two defluorination unit that connect successively, the first defluorination unit comprises the first reaction tank and the first settling tank, be used for finishing the one-level defluorination, the second defluorination unit comprises, the second reaction tank and the second settling tank, be used for finishing the secondary defluorination, the second reaction tank is connected with the water outlet of the first precipitation.The first reaction tank in the first defluorination unit is connected with the pH regulator pond, and the water outlet of the second settling tank in the second defluorination unit is connected with incomplete anaerobic reation pool.
Preferably, in pH regulator pond and each reaction tank in the defluorination unit, all be provided with whipping appts, be used for the liquid in the reaction process stirred vessel, more preferably, be provided with online pH monitor in the pH pond, be used for pH value in the measuring cell.
Preferably, in order to handle better chemical sludge and the biochemical sludge that produces in the wastewater treatment process well, at this Waste Water Treatment, also comprise sludge thickener, this sludge thickener comprises chemical sludge concentration basin and biochemical sludge concentration basin.The chemical sludge concentration basin, the chemical sludge that is used for the defluorination unit is produced carries out concentration, and this chemical sludge concentration basin is connected with the chemical sludge relief outlet of each settling tank in the defluorination unit.Subsequent disposal at the chemical sludge concentration basin partly connects dewatering system, and dewatering system carries out processed to chemical sludge, and the chemical sludge concentrating filtrate that produces need turn back to the pH regulator pond and process.The biochemical sludge concentration basin, the biochemical sludge that is used for the aerobe treating processes is discharged carries out concentration, and the biochemical sludge concentration basin links to each other with the biochemical sludge relief outlet of biochemical sedimentation basin.At the subsequent disposal part connection outlet dewatering system of biochemical sludge concentration basin, dewatering system carries out processed to biochemical sludge, and the biochemical sludge concentrating filtrate that produces turns back to incomplete anaerobic reation pool and processes.
Preferably, the problem that in the practical application of this Waste Water Treatment, may have elevation, at this moment, can in this Waste Water Treatment, add an intermediate pool, and sewage pump is set in intermediate pool, in order to lay according to the engineering real system, lifting sewage satisfies waterpower elevation demand to the subsequent reactions pond.
The invention provides a kind for the treatment of process of photovoltaic solar cell sheet factory effluent, adopt the thing treatment technology of delivering a child behind the multistage defluorination to process photovoltaic solar cell sheet factory effluent, processed waste water reaches direct emission standard or enters downstream sewage work receives pipe standards.
Embodiment one
A photovoltaic solar cell sheet manufacturer, collect respectively the acid waste water and the alkaline waste water that produce in the production process, acid waste water and alkaline waste water are tested, wherein the pH value of acid waste water is 1.5, content of fluoride ion is 4700mg/L; The pH value of alkaline waste water is 13.1, COD
CrConcentration value is 5800mg/L.
Acid waste water pond and the alkaline waste water tank waterpower residence time be about 8h respectively, being promoted to the pH regulator pond through lift pump mixes, the built-in stirrer in pH regulator pond, the rotating speed of stirrer is 160 rev/mins (RPM) in the mixing process, the pH value was 4.9 after the online pH instrument demonstration that arranges in the pond mixed, utilize online pH instrument control to add alkali pump, utilize volume pump to add NaOH solution and regulate between composite waste pH to 8.0～8.5 pH regulator tank waterpower residence time 30min.
The composite waste gravity flow enters the first reaction tank removal fluorion of follow-up the first defluorination unit behind the adjusting pH, utilizes volume pump to add CaCl
2About 8.84g/L, stirring reaction time 20min under the built-in stirrer effect of reaction tank, the rotating speed of stirrer is 160RPM, the waste water gravity flow enters the first settling tank precipitation, settling tank hydraulic detention time 1.5h after the reaction.The waste water gravity flow enters the second reaction tank of the second defluorination unit behind the one-level defluorination, carries out the reaction of secondary defluorination, utilizes volume pump to add CaCl
2About 500mg/L, reaction tank arranges stirrer, and rotating speed 88RPM utilizes volume pump to add Al simultaneously
2(SO4)
3Flocculation agent 150mg/L and PAM coagulant aids 5mg/L, reaction times 30min, gravity flow enters the second settling tank, hydraulic detention time 2h after the reaction.Hydraulic detention time 1h is flow automatically into intermediate pool in the precipitation water outlet.
Intermediate pool waste water is promoted to incomplete anaerobic reation pool through lift pump, hydraulic detention time 8h, and reaction tank adopts pulse water distribution.Not exclusively anaerobic reaction water outlet gravity flow enters follow-up aerobic biochemical pool, hydraulic detention time 20h.Gas-water ratio 30: 1 adopts the microporous diaphragm aeration tube.Sludge concentration 3000mg/L, the biochemistry pool water outlet flows into follow-up biochemical sedimentation basin, settling tank residence time 2h.
The priority pollutant index is as shown in table 1 in the biochemical sedimentation basin water outlet.
The principal pollutant index of water outlet after table 1 is processed
These parameters all adopts this area method test gained commonly used.By data in the table 1 as can be known, the waste water of discharging through waste water treatment process of the present invention meets China's discharge of wastewater respective standard, can enter the downstream and concentrate sewage work.
The precipitation discharging contains CaF in above-mentioned one-level and secondary defluorination process
2Chemical sludge, gravitational discharge is collected in the chemical sludge concentration basin, mud discharging is manually controlled, concentrating chemical mud is transported outward landfill after the mud spiral pump is promoted to plate-and-frame filter press dehydration, the sludge dewatering filtrate turns back to the pH regulator pond.The biochemical sedimentation basin precipitating sludge is partly refluxed to aerobic biochemical pool, reflux ratio 50%, all the other excess sludge gravitational discharges are collected in the biochemical sludge concentration basin, mud discharging is manually controlled, concentrated biological sludge is transported outward disposal after processed, biochemical sludge dehydration filtrate turns back to incomplete anaerobic reation pool.
In this Practical Project example, this system arranges programmable logic controller (PLC) system, is used for according to liquid level control lift pump start and stop in the pond, according to control dosing volume pump start and stop such as pH and fluorinion concentrations, also regulating fan operation time and the air quantity that is used for the biochemical treatment unit.
Embodiment two
Discharging alkaline waste water COD in the solar battery sheet production process
Cr5000mg/L, pH12.3, acid waste water pH 1.2, fluorinion concentration 5800mg/L.Adopt acid waste water, alkaline waste water shunting to process.Acid waste water tank waterpower residence time 10h, alkaline waste water tank waterpower residence time 8h.
Acid waste water is promoted to the pH regulator pond, adds NaOH solution and regulates pH to 8.0～8.5, and the water outlet gravity flow enters the first reaction tank of the first defluorination unit, adds CaCl
2Approximately 29g/L reacts 30min, and the waste water gravity flow enters the first settling tank, hydraulic detention time 2h after the reaction.The water outlet gravity flow enters the second reaction tank, adds CaCl
21000mg/L adds Al simultaneously
2(SO
4)
3Flocculation agent 200mg/L and PAM coagulant aids 8mg/L, reaction times 30min, gravity flow enters the second settling region, hydraulic detention time 2h after the reaction.Precipitation water outlet pH approximately about 8.0, fluorinion concentration 8mg/L, directly standard discharge.Defluorination settling tank discharging chemical sludge is regularly beaten to the mud and sewage unit after the chemical sludge concentration basin is concentrated, and the dehydrated sludge outward transport is as reclaiming purification fluorite raw material.
Alkaline waste water is promoted to another pH regulator pond, adds sulphur acid for adjusting pH to 8.0～8.5.The water outlet gravity flow enters incomplete anaerobic reation pool after regulating, hydraulic detention time 12h, and water outlet enters follow-up aerobic biochemical reaction tank, hydraulic detention time 28h, sludge concentration is 4000mg/L approximately, water outlet COD after the biochemistry precipitation
CrAbout 280mg/L, pH 7.5～8.0, can standard discharge.Biochemical sedimentation basin mud dewaters after concentration and transports outward landfill.
The above is the preferred embodiments of the present invention only, is not limited to the present invention, and for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. a photovoltaic solar cell sheet production wastewater treatment technique is characterized in that, described technique may further comprise the steps:
Acid waste water and alkaline waste water are collected respectively in wastewater collection;
PH regulator to being mixed by described acid waste water and alkaline waste water, in the soda acid composite waste of formation, adds strong acid or highly basic, regulates pH value to 8.0～8.5, forms treatment solution;
Described treatment solution is carried out the defluorination step: in described treatment solution, drop into CaCl
2, to remove the fluorion in the waste water;
The described treatment solution of finishing the defluorination step is removed the COD step: treatment solution is carried out incomplete anaerobic reaction; Carrying out aerobe processes again;
Finish successively above-mentioned steps, the waste water that will reach emission standard effluxes.
2. waste water treatment process according to claim 1 is characterized in that, described wastewater collection process further comprises:
Collect respectively acid waste water and alkaline waste water, hydraulic detention time is greater than 8h.
3. waste water treatment process according to claim 1 is characterized in that, described defluorination process further comprises:
The one-level defluorination drops into CaCl in the waste water that regulates the pH value
2, the input amount of described calcium salt and the mass ratio of fluorion are 4: 1～5: 1, stirring reaction 20～30min, precipitation 1～2h, scavenger precipitation chemical sludge.
4. waste water treatment process according to claim 3 is characterized in that, described defluorination process further comprises:
The secondary defluorination drops into CaCl again in the waste water through one-level defluorination process
2, the input amount of described calcium salt is 500～1000mg/L, stirring reaction 20～30min, precipitation 2h, scavenger precipitation chemical sludge.
5. waste water treatment process according to claim 4 is characterized in that, further comprises in the described secondary defluorination process:
Drop into CaCl
2The time add 100～200mg/L flocculation agent, and the coagulant aids of 3～8mg/L.
6. each described waste water treatment process is characterized in that according to claim 1-5, and described defluorination process further comprises:
Carry out concentration to precipitating the chemical sludge that produces in the defluorination process, outward transport landfill after the thickened sludge dehydration is disposed or carried out the advanced treatment of the resource recovery of fluorine, concentrating filtrate turns back to the pH regulator step, continues to process.
7. waste water treatment process according to claim 1 is characterized in that, described aerobe is processed and further comprised:
The biochemical sludge part of discharging in the aerobe treating processes is applied in the described aerobe treating processes again; Excess sludge is carried out concentration, and the biochemical sludge after concentrating is transported outward after processed or compost is disposed, and concentrating filtrate turns back to incomplete anaerobic reaction step, continues to process.
8. waste water treatment process according to claim 5 is characterized in that,
Described flocculation agent is Al
2(SO
4)
3, polyaluminium sulfate;
Described coagulant aids is polyacrylamide.
9. waste water treatment process according to claim 1 is characterized in that, except in the COD step, not exclusively the time of anaerobic reaction is 8～12h.
10. waste water treatment process according to claim 1 is characterized in that, except in the COD step, the hydraulic detention time of aerobe treating processes is greater than 20h, and sludge concentration is 3000～4000mg/L, reaction postprecipitation 1～2h.
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| TW201236983A (en) * | 2011-03-03 | 2012-09-16 | Chiou-Mei Chen | Treatment method for waste water in process of preparing silicon chip |
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| CN103011453B (en) * | 2012-12-08 | 2014-01-22 | 北京国环清华环境工程设计研究院有限公司 | Processing method for fluoride waste water in production of solar cells |
| CN103102027B (en) * | 2013-02-26 | 2015-07-01 | 宏大中源太阳能股份有限公司 | Sewage treatment system and method for solar cell production |
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| CN103708679B (en) * | 2013-12-26 | 2015-05-20 | 浙江工商大学 | Treatment process for fluorine chemical wastewater |
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| CN108249706B (en) * | 2018-02-14 | 2020-11-20 | 南京大学 | Treatment method for denitrification, defluorination and recycling of wastewater in silicon industry |
| CN108249707B (en) * | 2018-02-14 | 2020-10-30 | 南京大学 | Treatment system and treatment method for fluorine-containing nitrate nitrogen-containing industrial wastewater |
| CN110510822A (en) * | 2019-09-09 | 2019-11-29 | 山东大海新能源发展有限公司 | A kind of polycrystalline silicon industry wastewater treatment recovery method |
| CN111547885B (en) * | 2020-05-14 | 2022-07-01 | 浙江艾摩柯斯环境科技有限公司 | Process for removing fluorine, controlling salt and recovering fluorine from silicon solar cell production wastewater |
| CN111977911A (en) * | 2020-08-28 | 2020-11-24 | 贵州中车绿色环保有限公司 | Method for treating leachate wastewater in electrolytic aluminum slag yard |
| CN112174439A (en) * | 2020-10-14 | 2021-01-05 | 上海三邦水处理技术有限公司 | LED chip manufacturing industry wastewater treatment engineering process |
| CN115959750A (en) * | 2022-12-26 | 2023-04-14 | 伊沃环境科技(南京)有限公司 | Efficient polycrystalline silicon waste water defluorination system |
| CN117105382B (en) * | 2023-09-23 | 2024-03-19 | 广东水清环保科技有限公司 | Industrial garden heavy metal wastewater treatment method, device, equipment and storage medium |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101811792A (en) * | 2009-02-24 | 2010-08-25 | 宝山钢铁股份有限公司 | Processing method of stainless steel cold rolling pickling wastewater |
-
2010
- 2010-09-17 CN CN2010102860714A patent/CN101973662B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101811792A (en) * | 2009-02-24 | 2010-08-25 | 宝山钢铁股份有限公司 | Processing method of stainless steel cold rolling pickling wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 周建民等.光伏电池单晶硅生产废水处理工程实例.《水处理技术》.2009,第35卷(第4期), * |
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