CN104003581A - Treatment process of high-concentration degradation-resistant organic wastewater - Google Patents
Treatment process of high-concentration degradation-resistant organic wastewater Download PDFInfo
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Abstract
The invention discloses a treatment process of high-concentration degradation-resistant organic wastewater; the treatment process is high in efficiency, good in effect, low in cost, very environment-friendly and capable of effectively treating the high-concentration degradation-resistant organic wastewater and comprises the steps of introducing wastewater in an anaerobic reactor, regulating pH value, resisting halobacteriumsp reaction, adsorbing, separating, denitrifying, cooling and filtering; and the ultrasonic wave is used in the denitrifying step to enhance the denitrifying efficiency.
Description
Technical field
The present invention relates to a kind for the treatment of process of organic waste water.
Background technology
Nitrogenous and organic content is very high, be difficult to biological degradation in the waste water producing in the industry production processes such as chemical industry, food-processing, semi-conductor, be one of the difficult point of wastewater treatment both at home and abroad at present and focus.
For example, in chemical materials production process, will produce a large amount of high concentration hard-degraded organic waste waters, its COD is high, is generally greater than 10000mg/L, saltiness is high, and approximately 3%～5%, total nitrogen is high and be organonitrogen.A kind of method of processing this waste water is to adopt iron-carbon micro-electrolysis+Fenton to carry out the methyl compound in degrading waste water, but its treatment effect is undesirable, and processing cost is higher.
In the trade effluents such as medication chemistry, printing dye, also contain in addition difficult for biological degradation, poisonous composition, while processing this waste water, directly adopt biochemical process poor effect, generally before biochemical process, by the micro-electrolysis of iron charcoal, catalytic oxidation etc., it is carried out to pre-treatment, but the micro-electrolysis of iron charcoal is easily lumpd, and catalytic oxidation running cost is higher.To environment, more disadvantageously, also have a lot of chemical enterprises to utilize some clear water by carrying out again biochemical treatment after above-mentioned wastewater dilution, not only cause the waste of water resources, also increased treatment facility scale.
For better protection of the environment; on the one hand; people adopt the eco-friendly and green methods such as chemical synthesis route from source and fundamentally reduce and pollute, and on the other hand, people also attempt to set up more efficient, economic, clean, to remove up hill and dale water pollutant novel method.
At present, treatment technology for pollutents such as the heavy metal in water, suspended solid, bio-degradable organic pollutant, nitrogen, phosphorus is gradually improved, but be difficult to biodegradable organic waste water for polluted-water middle and high concentration, also lack at present highly effective method and technology, therefore need the treatment process of the more effective highly difficult organic wastewater with difficult degradation thereby of research and development badly.
Summary of the invention
The invention discloses a kind for the treatment of process of high concentration hard-degraded organic waste water, this art breading efficiency is high, effective, cost is low, more environmental protection, can effectively process the organic waste water of high-concentration hardly-degradable.
The treatment process of high concentration hard-degraded organic waste water of the present invention, comprises the following steps:
(1) organic waste water is passed into anaerobic reactor, adopt pH regulator reagent by its pH regulator to 7.5～8.5, control 25～30 ℃ of temperature, add Facultative Halophiles to carry out two-stage anaerobic biochemical reaction, every order reaction 36～40h, the add-on of Facultative Halophiles is 8%～15% of anaerobic reactor useful volume;
(2) wastewater pH of processing through step (1) is adjusted to and is more than or equal to 11, enter ammonia-nitrogen stripping tower and carry out ammonia-nitrogen desorption and be not less than 10 to pH, and no longer decline;
(3) waste water of step (2) being processed imports aerobic reactor pH regulator to 7～9, adds Facultative Halophiles to carry out aerobic reaction, and the add-on of Facultative Halophiles is 8%～15% of aerobic reactor useful volume, and the aerobic reaction time is 20～30h;
(4) adopting gac is sorbent material, and the waste water that step (3) was processed carries out extracting and enriching processing, after charcoal absorption is saturated, carries out natural gravity draining, adopts aqueous acetone solution to carry out outer circulation desorption-ozone Oxidation Treatment;
(5) waste water after step (4) processing is entered into reverse osmosis membrane system and carry out separation, isolate two portions water outlet after described reverse osmosis membrane system, a part is for producing water, and another part is dense water;
(6) the product water after step (5) processing is entered into exchange resin tower, by ion exchange resin, remove wherein residual Nitrogen element pollutent; The operating capacity of exchange resin tower is 60～70meq/g, and regeneration exchange capacity is 80～90mep/g; Ion exchange resin is macroporous ion-exchange resin, and its true density is 1.15～1.24g/ml; Inside at exchange resin tower is provided with ultrasonic generator, and hyperacoustic frequency is 30～60KHz;
(7) waste water after step (6) is processed, after grid is crossed the thick dirt of elimination, enters again in another water cooler and continues to be cooled to 0～10 ℃ after supercooler is cooling, then filters;
(8) waste water filtering out in step (7) is entered to neutralization tank and regulate its pH value for entering the cooling waste water entering through grid in another water cooler after neutrality by acid-base neutralisation device, then enter in vaporizer and be concentrated 6～12 times;
(9) waste water after concentrated in step (8) is filtered, filtrate enters sink drainage after mixing with phlegma out from vaporizer and carries out biochemical treatment.
Wherein, in step (6), hyperacoustic calibration is 40～45KHz; Ion exchange resin is preferably acrylic resin;
Wherein, Facultative Halophiles is in step (1): lactobacillus fermentum, short lactobacillus, Pseudomonas alcaligenes, to cause golden pseudomonas, greenery pseudomonas, nitrate reductase pseudomonas, riboflavin pseudomonas or above-mentioned multiple bacterial classification compound.
Wherein, in step (1), pH regulator reagent is sulfuric acid, nitric acid, hydrochloric acid, carbonic acid, sodium hydroxide, calcium hydroxide, potassium hydroxide, calcium oxide, sodium carbonate, calcium carbonate or Calcium hydrogen carbonate.
Wherein, in step (4), operating weight percentage concentration is as desorption liquid lower than 50% aqueous acetone solution.
Wherein, in step (4), ozone contacts with adsorbing saturated gac with aqueous acetone solution simultaneously, forms water/solid-liquid three-phase system, and aeration and desorption carry out simultaneously, and aeration-desorption time is 20～30min, and the ozone oxidation reaction time is 20～30min.
Wherein, in step (5), described reverse osmosis membrane system adopts crosslinked aromatic polymeric amide anti-pollution reverse osmosis membrane, and its ratio of desalinization is greater than 98%.
Wherein, in step (7), water cooler is dividing wall type water cooler, water drip cooler.
Wherein, in step (8), vaporizer is single-effect evaporator, multiple-effect evaporator, rotary evaporator.
Embodiment
In order to make those skilled in the art more clearly understand waste water treatment process of the present invention, specifically describe its embodiment and embodiment below.
The treatment process of high concentration hard-degraded organic waste water of the present invention, comprises the following steps:
(1) organic waste water is passed into anaerobic reactor pH regulator to 7.5～8.5, control 20～25 ℃ of temperature, add Facultative Halophiles to carry out two-stage anaerobic biochemical reaction, every order reaction 36～40h, the add-on of Facultative Halophiles is 10%～15% of anaerobic reactor useful volume, the COD≤10000mg/L of wherein said organic waste water, NH
3-N≤150mg/L, TN≤700mg/L;
(2) wastewater pH of processing through step (1) is adjusted to and is more than or equal to 11, enter ammonia-nitrogen stripping tower and carry out ammonia-nitrogen desorption and be not less than 10 to pH, and no longer decline;
(3) waste water of step (2) being processed imports aerobic reactor pH regulator to 7～9, adds Facultative Halophiles to carry out aerobic reaction, and the add-on of Facultative Halophiles is 8%～15% of aerobic reactor useful volume, and the aerobic reaction time is 20～30h.
Wherein, described salt-durable microbe is: lactobacillus fermentum, short lactobacillus, Pseudomonas alcaligenes, to cause golden pseudomonas, greenery pseudomonas, nitrate reductase pseudomonas, riboflavin pseudomonas or above-mentioned multiple bacterial classification compound.
Wherein, the reagent of described adjusting pH is sulfuric acid, nitric acid, hydrochloric acid, carbonic acid, sodium hydroxide, calcium hydroxide, potassium hydroxide, calcium oxide, sodium carbonate, calcium carbonate or Calcium hydrogen carbonate.
(4) adopt the waste water after gac is processed step (3) to adsorb-trap oxybenzene compound, after charcoal absorption is saturated, replaceable new activated carbon column proceeds to adsorb wastewater treatment, adsorb after saturated gac natural gravity draining, adopting aqueous acetone solution to carry out outer circulation mode desorption processes, in desorption process, pass into ozone simultaneously, form water/solid-liquid three-phase system, aeration and desorption carry out simultaneously, oxybenzene compound carries out ozone oxidation degraded at aqueous acetone solution or activated carbon surface, general aeration-desorption time is 40～60min, the ozone oxidation reaction time is generally 40～60min.
(5) waste water after step (4) processing is entered into reverse osmosis membrane system and carry out separation, isolate two portions water outlet after described reverse osmosis membrane system, a part is for producing water, and another part is dense water, and producing water ratio is 65%～70%.
Wherein, described reverse osmosis membrane system adopts crosslinked aromatic polymeric amide anti-pollution reverse osmosis membrane, and its ratio of desalinization is greater than 98%.
Wherein, the producing water ratio of described reverse osmosis membrane system is 68%～70%.
(6) the product water after step (5) processing is entered into exchange resin tower, ion exchange resin is macroporous ion-exchange resin, is preferably acrylic resin; Its true density is 1.15～1.24g/ml, by process waste water in exchange resin tower, can remove wherein residual Nitrogen element pollutent; The operating capacity of exchange resin tower is 60～70meq/g, and regeneration exchange capacity is 80～90mep/g;
Inside at exchange resin tower is provided with ultrasonic generator, and preferably, hyperacoustic frequency is 30～60KHz, preferred, and hyperacoustic frequency is 40～45KHz.The discovery that we are pleasantly surprised, in the product water of exchange resin tower, the content of test Nitrogen element pollutent, adopts ultrasonic wave generating apparatus than not adopting ultrasonic wave generating apparatus to reduce by 25～35%.We know, in the prior art, also once had the report that adopts ultrasonic generator, but the method are completely different from the application in method of wastewater treatment, and it is in degradation process, utilize hyperacoustic cavatition to strengthen the organic degradation capability of degradation bacteria; And the reason that the application can strengthen desorption ability is analyzed according to us and is, adopt ultrasonic wave in ion exchange process, can expand the contact efficiency of ion exchange resin, shorten the distance of ion-exchange, increase active centre, thereby improve ion-exchange capacity.
(7) waste water after step (6) is processed, after grid is crossed the thick dirt of elimination, enters again in the second water cooler and continues to be cooled to 0～10 ℃ after the first water cooler is cooling, then filters; Wherein, water cooler is dividing wall type water cooler, water drip cooler etc.
(8) waste water filtering out in step (7) is entered to neutralization tank and regulate its pH value for entering the cooling waste water entering through grid in water cooler after neutrality by acid-base neutralisation device, then enter in vaporizer and be concentrated 6～12 times; Wherein, vaporizer is single-effect evaporator, multiple-effect evaporator, rotary evaporator etc.
(9) waste water after concentrated in step (8) is filtered, filtrate enters sink drainage after mixing with phlegma out from vaporizer and carries out biochemical treatment.Wherein, the equipment of filtration is whizzer, suction filtration tank or pressure filter etc.
Embodiment 1
By waste water (COD:6428mg/L, TN:684mg/L, NH
3-N:83mg/L, salinity: 2.6%) pass into anaerobic reactor pH regulator to 8.5, control 25 ℃ of temperature, add flour, ammonium sulfate, dipotassium hydrogen phosphate, regulate COD: N: P=240: 5: 1, add halo micrococci to carry out two-stage anaerobic biochemical reaction, every order reaction 36h; To regulate 12 through the wastewater pH of step process, and enter ammonia-nitrogen stripping tower and carry out ammonia-nitrogen desorption and be not less than 10 to pH, and no longer decline; Waste water is continued to import aerobic reactor pH regulator to 8.5, add Pseudomonas alcaligenes to carry out aerobic reaction, the reaction times is 30h.It is that 220mg/L, TN are 45.5mg/L, NH that water outlet detects COD
3-N is 13.6mg/L.
Use conventional active carbon adsorption column (or tower), its device connects solvent desorption system.The processed organic waste water water yield is lower than 20m
3/ d, concentration is below 100mg/L, ozonizer is 5.0g/h.In active carbon adsorption column, Pyrogentisinic Acid's compound carries out adsorption treatment, intermittently to adsorbing saturated gac, carries out desorption/ozone oxidation.Adsorb after saturated gac natural gravity draining, adopt aqueous acetone solution (to contain acetone below 50%, volume ratio) outer circulation desorption/ozone oxidation is processed simultaneously, oxidation time is 20～30min, stop desorption/ozone oxidation, aqueous acetone solution returns in container for storing liquid, adds the activated carbon column just entering in adsorption treatment containing the tail gas of residual ozone before by pump, after adsorbing completely-decomposing, enter atmosphere.Aqueous acetone solution and gac recycle.Oxybenzene compound clearance can reach more than 90%.
Waste water is entered into reverse osmosis membrane system and carry out separation, isolate two portions water outlet after described reverse osmosis membrane system, a part is for producing water, and another part is dense water, and producing water ratio is 65%～70%.Then enter into exchange resin tower, by ion exchange resin, remove wherein residual Nitrogen element pollutent.The operating capacity of exchange resin tower is 60meq/g, and regeneration exchange capacity is 80mep/g; Ion exchange resin acrylic resin, its true density is 1.19g/ml; Inside at exchange resin tower is provided with ultrasonic generator, and hyperacoustic frequency is 40KHz.
By removing waste water after nitrogen element, after grid is crossed the thick dirt of elimination, enter successively after being cooled to 5 ℃ in spiral-plate exchanger, brine cooler and filter with tripod pendulum type batch centrifugal; The filtrate filtering out enters neutralization tank, and by acid-base neutralisation device, to regulate its pH value be to enter after neutrality coolingly in spiral-plate exchanger through grid, to enter the alkaline hydrolysis waste water in spiral-plate exchanger, then enters successively in multiple-effect evaporator and be concentrated 10 times; Alkaline hydrolysis waste water after being concentrated is filtered with suction filtration tank, and filtrate enters sink drainage after mixing with phlegma out from multiple-effect evaporator and carries out biochemical treatment.
Waste water after processing: effluent COD concentration <50mg/l; MARS technology: water outlet phenol content <500ppm; Rejection >90%; Coefficient of oxygen utilization >=90%, without sludge creation; Salt tolerant scope: 1%～10%.
Embodiment 2:
By waste water (COD:5040mg/L, TN:612mg/L, NH
3-N:71mg/L, salinity: 2.45%) pass into anaerobic reactor pH regulator to 8, control 26 ℃ of temperature, add glucose, urea, potassium primary phosphate, regulate COD: N: P=180: 5: 1, add short lactobacillus to carry out two-stage anaerobic biochemical reaction, every order reaction 38h; To regulate 11.5 through the wastewater pH of step process, and enter ammonia-nitrogen stripping tower and carry out ammonia-nitrogen desorption and be not less than 10 to pH, and no longer decline; Waste water is continued to import aerobic reactor pH regulator to 8, add micrococcus luteus to carry out aerobic reaction, the reaction times is 24h.It is that 250mg/L, TN are that 36.5mg/L, NH3-N are 11.2mg/L that water outlet detects COD.
Use common active carbon adsorption column (or tower), its device connects solvent desorption system.The processed organic waste water water yield is greater than 20m
3/ d, concentration is below 100mg/L, ozonizer is 8.0g/h.In active carbon adsorption column, it is carried out to adsorption treatment, by changing activated carbon column method, continuously waste water is carried out to adsorption treatment, intermittently to adsorbing saturated gac, carry out desorption/ozone oxidation.Adsorb after saturated gac natural gravity draining, adopt aqueous acetone solution (to contain acetone below 50%, volume ratio) outer circulation desorption/ozone oxidation is processed simultaneously, oxidation time is 20～30min, stop desorption/ozone oxidation, aqueous acetone solution returns in container for storing liquid, adds the activated carbon column just entering in adsorption treatment containing the tail gas of residual ozone before by pump, after adsorbing completely-decomposing, enter atmosphere.Aqueous acetone solution and gac recycle.Oxybenzene compound clearance can reach more than 93%.
Waste water after processing is entered into reverse osmosis membrane system and carry out separation, isolate two portions water outlet after described reverse osmosis membrane system, a part is for producing water, and another part is dense water, and producing water ratio is 65%～70%.Waste water after processing is entered into exchange resin tower, by ion exchange resin, remove wherein residual Nitrogen element pollutent.The operating capacity of exchange resin tower is 70meq/g, and regeneration exchange capacity is 90mep/g; Ion exchange resin acrylic resin, its true density is 1.19g/ml; Inside at exchange resin tower is provided with ultrasonic generator, and hyperacoustic frequency is 45KHz.
Through above-mentioned wastewater temperature, be 20 ℃, after grid is crossed the thick dirt of elimination, enter successively after being cooled to 0 ℃ in spiral-plate exchanger, brine cooler and filter with tripod pendulum type batch centrifugal; The filtrate filtering out is entered to neutralization tank, and by acid-base neutralisation device, to regulate its pH value be to enter after neutrality coolingly in spiral-plate exchanger through grid, to enter the alkaline hydrolysis waste water in spiral-plate exchanger, then enters successively in multiple-effect evaporator, scraped film evaporator and be concentrated 12 times; Alkaline hydrolysis waste water is filtered with suction filtration tank, and filtrate enters sink drainage after mixing with phlegma out from multiple-effect evaporator and carries out biochemical treatment; .
Waste water after processing: effluent COD concentration <50mg/l; MARS technology: water outlet phenol content <500ppm; Rejection >90%; Coefficient of oxygen utilization >=90%, without sludge creation; Salt tolerant scope: 1%～10%.
The present invention, by above-mentioned treatment process organic combination, brings into play the synergy of each technique, and the hardly degraded organic substance in waste water and other organic pollutants significantly reduce the most at last, finally realizes the process water of waste water recycling in producing and the object of wastewater zero discharge.Its usage range is wide, and technique is simple, simple to operate, and working cost is lower.
The present invention is directed to the feature of organic waster-water in the course of processing, first adopt anaerobic biological to destroy the structure of DMAC in waste water, the organism of degraded part, the ammonification of simultaneously carrying out, organonitrogen is converted into ammonia nitrogen, the ammonia nitrogen transforming is realized and being reclaimed by follow-up stripping and absorption unit, thereby realizes the removal of Determination of Total Nitrogen in Waste Water and ammonia nitrogen, and the waste water after stripping passes through aerobic biochemical degradation of organic substances again.Owing to introducing microorganism, process, a whole set of method, when processing waste water, can be saved very large energy consumption, has greatly saved treatment cost.
The present invention is by the method for ozone Quick Oxidation degradation of phenol compound waste water, under equal conditions, compare with traditional water/gas two-phase ozone oxidation reaction system, ozone dosage reduces more than 1/2, reaction times shortens more than 2/3, the total clearance of toxic organic compound reaches more than 90%, and stable effluent quality.
Anaerobic reactor, adjusting pH value, Facultative Halophiles reaction, absorption, separation, denitrogenation, cooling and filtration
In method of the present invention, between the order of each step, also have a beneficial effect, waste water first passes through oxidation pre-treatment denitrogenation, more further by aerobic/anaerobic biological treatment, carries out biochemical denitrification, reduces processing cost.The present invention is by absorption, separated that the materials such as the particulate matter in waste water, inorganic salt, organism, hardness ions, bacterium is separated with water.Filtering, evaporation, the step such as cooling can make full use of the efficiency of the equipment such as vaporizer, material can be in lower temperature evaporation, meet the concentrated requirement of heat-sensitive material, the integrated impact that is not subject to saltiness height of evaporative crystallization, and can not introduce new pollutent in water.
Waste water technology index after processing by the present invention: effluent COD concentration <50mg/l; MARS technology: water outlet phenol content <500ppm; Rejection >90%, raffinate can be directly as fuel combustion; Biomass mean calorie >33MJ/kg; Coefficient of oxygen utilization >=90%, without sludge creation.Facultative Halophiles is processed high salt chemical engineering waste water salt tolerant scope 1%～10%.
The present invention also can have other various embodiments; in the situation that not deviating from spirit of the present invention and essence thereof; those of ordinary skill in the art are when making according to the present invention various corresponding changes and distortion, but these corresponding changes and distortion all should belong to the protection domain of the appended claim of the present invention.
Claims (10)
1. a treatment process for high concentration hard-degraded organic waste water, comprises the following steps:
(1) organic waste water is passed into anaerobic reactor, adopt pH regulator reagent by its pH regulator to 7.5～8.5, control 20～25 ℃ of temperature, add Facultative Halophiles to carry out two-stage anaerobic biochemical reaction, every order reaction 36～40h, the add-on of Facultative Halophiles is 10%～15% of anaerobic reactor useful volume;
(2) wastewater pH of processing through step (1) is adjusted to and is more than or equal to 11, enter ammonia-nitrogen stripping tower and carry out ammonia-nitrogen desorption and be not less than 10 to pH, and no longer decline;
(3) waste water of step (2) being processed imports aerobic reactor pH regulator to 7～9, adds Facultative Halophiles to carry out aerobic reaction, and the add-on of Facultative Halophiles is 8%～15% of aerobic reactor useful volume, and the aerobic reaction time is 20～30h;
(4) adopting gac is sorbent material, and the waste water that step (3) was processed carries out extracting and enriching processing, after charcoal absorption is saturated, carries out natural gravity draining, adopts aqueous acetone solution to carry out outer circulation desorption-ozone Oxidation Treatment;
(5) waste water after step (4) processing is entered into reverse osmosis membrane system and carry out separation, isolate two portions water outlet after described reverse osmosis membrane system, a part is for producing water, and another part is dense water;
(6) the product water after step (5) processing is entered into exchange resin tower, by ion exchange resin, remove wherein residual Nitrogen element pollutent; The operating capacity of exchange resin tower is 60～70meq/g, and regeneration exchange capacity is 80～90mep/g; Ion exchange resin is macroporous ion-exchange resin, and its true density is 1.15～1.24g/ml; Inside at exchange resin tower is provided with ultrasonic generator, and hyperacoustic frequency is 30～60KHz;
(7) waste water after step (6) is processed, after grid is crossed the thick dirt of elimination, enters again in another water cooler and continues to be cooled to 0～10 ℃ after supercooler is cooling, then filters;
(8) waste water filtering out in step (7) is entered to neutralization tank and regulate its pH value for entering the cooling waste water entering through grid in another water cooler after neutrality by acid-base neutralisation device, then enter in vaporizer and be concentrated 6～12 times;
(9) waste water after concentrated in step (8) is filtered, filtrate enters sink drainage after mixing with phlegma out from vaporizer and carries out biochemical treatment.
2. technique as claimed in claim 1, is characterized in that, in step (6), hyperacoustic frequency is 40～45KHz.
3. technique as claimed in claim 1, is characterized in that, in step (6), ion exchange resin is acrylic resin.
4. technique as claimed in claim 1, it is characterized in that, Facultative Halophiles is in step (1): lactobacillus fermentum, short lactobacillus, Pseudomonas alcaligenes, to cause golden pseudomonas, greenery pseudomonas, nitrate reductase pseudomonas, riboflavin pseudomonas or above-mentioned multiple bacterial classification compound.
5. technique as claimed in claim 1, is characterized in that, in step (1), pH regulator reagent is sulfuric acid, nitric acid, hydrochloric acid, carbonic acid, sodium hydroxide, calcium hydroxide, potassium hydroxide, calcium oxide, sodium carbonate, calcium carbonate or Calcium hydrogen carbonate.
6. technique as claimed in claim 1, is characterized in that, in step (4), operating weight percentage concentration is as desorption liquid lower than 50% aqueous acetone solution.
7. technique as claimed in claim 1, it is characterized in that, in step (4), ozone contacts with the aqueous acetone solution while gac saturated with absorption, form water/solid-liquid three-phase system, aeration and desorption carry out simultaneously, and aeration-desorption time is 20～30min, and the ozone oxidation reaction time is 20～30min.
8. technique as claimed in claim 1, is characterized in that, in step (5), described reverse osmosis membrane system adopts crosslinked aromatic polymeric amide anti-pollution reverse osmosis membrane, and its ratio of desalinization is greater than 98%.
9. technique as claimed in claim 1, is characterized in that, in step (7), water cooler is dividing wall type water cooler, water drip cooler.
10. technique as claimed in claim 1, is characterized in that, in step (8), vaporizer is single-effect evaporator, multiple-effect evaporator, rotary evaporator.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105776747A (en) * | 2016-04-06 | 2016-07-20 | 大连理工大学 | Method for promoting azo dye wastewater decoloring with lignite |
| CN106007078A (en) * | 2016-07-05 | 2016-10-12 | 双良节能系统股份有限公司 | Intermittent adsorption-catalytic oxidation treatment method for removing organic matters of coal chemical high-salt water |
| CN107686218A (en) * | 2017-10-17 | 2018-02-13 | 爱环吴世（苏州）环保股份有限公司 | The handling process of high-concentration waste water |
| CN108840497A (en) * | 2018-06-04 | 2018-11-20 | 宿迁新亚科技有限公司 | A method of sewage middle and high concentration ammonia nitrogen is removed with large aperture synthetic resin |
| CN110564605A (en) * | 2019-09-17 | 2019-12-13 | 山东昱泰环保工程有限公司 | Semi-open type microbial fermentation equipment and method for high-salinity wastewater treatment |
| CN115231775A (en) * | 2022-07-26 | 2022-10-25 | 山东鲁抗中和环保科技有限公司 | Method for treating pharmaceutical chemical high-salinity wastewater |
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2014
- 2014-06-09 CN CN201410249933.4A patent/CN104003581A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105776747A (en) * | 2016-04-06 | 2016-07-20 | 大连理工大学 | Method for promoting azo dye wastewater decoloring with lignite |
| CN105776747B (en) * | 2016-04-06 | 2018-07-06 | 大连理工大学 | A kind of method for promoting decolorizing azo dye waste water using lignite |
| CN106007078A (en) * | 2016-07-05 | 2016-10-12 | 双良节能系统股份有限公司 | Intermittent adsorption-catalytic oxidation treatment method for removing organic matters of coal chemical high-salt water |
| CN107686218A (en) * | 2017-10-17 | 2018-02-13 | 爱环吴世（苏州）环保股份有限公司 | The handling process of high-concentration waste water |
| CN108840497A (en) * | 2018-06-04 | 2018-11-20 | 宿迁新亚科技有限公司 | A method of sewage middle and high concentration ammonia nitrogen is removed with large aperture synthetic resin |
| CN110564605A (en) * | 2019-09-17 | 2019-12-13 | 山东昱泰环保工程有限公司 | Semi-open type microbial fermentation equipment and method for high-salinity wastewater treatment |
| CN115231775A (en) * | 2022-07-26 | 2022-10-25 | 山东鲁抗中和环保科技有限公司 | Method for treating pharmaceutical chemical high-salinity wastewater |
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Application publication date: 20140827 |