CN105254139A - Treating method for high-salinity pharmaceutical wastewater - Google Patents
Treating method for high-salinity pharmaceutical wastewater Download PDFInfo
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Abstract
The invention provides a treating method for high-salinity pharmaceutical wastewater. According to the treating method, the steps of materialization pretreatment, desulfuration biological treatment, materialization deep treatment, settlement and drainage and the like are adopted for treating the pharmaceutical wastewater which is high in COD concentration and high in sulfate radical concentration and contains medical intermediates and antibiotic residues. The treating method is fit for characteristics of the pharmaceutical wastewater, such as high concentration, refractory and strong biotoxicity. According to the invention, the technical combination is reasonable and the standard emission is ensured.
Description
Technical field
The invention belongs to waste water treatment field, be specifically related to a kind for the treatment of process of high salt pharmacy waste water.
Background technology
In pharmaceutical manufacturing process, often use plurality of raw materials and solvent, complex manufacturing, Production Flow Chart is long, reaction is complicated, and by product is many, and thus waste water composition is very complicated, Pollutants in Wastewater content is high, COD concentration is large and fluctuation is large, colourity is dark, SS concentration is high, and containing difficult for biological degradation and toxicant many.As the waste water of the microbiotic medicine intermediates such as production clarithromycin, Ciprofloxacin, the semi-synthetic Intermediate Wastewater of medicines such as synthesis Cephalexin Monohydrate Micro/Compacted, Cephradine and S 578 etc., and to produce antibiotic fermentation waste water etc. be exactly typical difficult degradation, high salt, virose waste water.This kind of waste water contains the material of not easily degrading in a large number and the material suppressing microbial process, sulfate radical containing higher concentration, ammonia nitrogen, containing a small amount of unreacted raw material and synthetic intermediate, these materials have restraining effect and toxic action to bacterium, as sulfate radical reduzate hydrogen sulfide to the methanogen in anaerobic system, acid-producing bacteria even sulphate reducing bacteria all have restraining effect.The soluble inorganic salt of Coal Gas Washing Cycling Water and the toxic organic compound of difficult degradation can cause serious environmental pollution, damage soil and surface water, underground water.Harm humans is healthy, and havoc water body, soil and ecotope, cause unthinkable consequence.
Various countries scientist pays much attention to the degraded of pharmacy waste water and the research for the treatment of process, sum up nothing more than physico-chemical process, biological process, materialization-bio combined method, but the feature of high salt pharmacy waste water makes traditional treatment process be difficult to gather effect, and processing cost is high.Therefore, how effectively to utilize existing water pollutions treatment technology, and to reasonably carrying out process combination, introduce new technology simultaneously, Optimization Technology technical parameter becomes the key of pharmaceutical wastewater treatment process success or failure.
Summary of the invention
In order to solve the deficiency of existing high salt pharmacy waste water technique, reduce sulfate concentration in pharmacy waste water, make it effectively to be processed and qualified discharge, the present invention adopts step process height COD concentration, the high sulfate concentrations such as physico-chemical pretreatment, desulfurization biological treatment, materialization advanced treatment, whole mattress sinking water, and the pharmacy waste water containing medicine intermediate and antibiotic remains, be adapted to the features such as pharmacy waste water high density, difficult degradation, bio-toxicity are strong, process combination is reasonable, ensures qualified discharge.
In order to realize foregoing invention object, the present invention adopts following combination process to process high salt pharmacy waste water:
1) physico-chemical pretreatment;
2) desulfurization biological treatment;
3) materialization advanced treatment;
4) whole mattress sinking water.
Preferably, the treatment process of described high salt pharmacy waste water, it comprises the following steps:
1) physico-chemical pretreatment: catalysis and micro-electrolysis, lime desulfurization precipitation, pH value adjustment;
2) desulfurization biological treatment: anoxic biological treatment, molysite desulfurization process, anaerobic biological treatment, Aerobic biological process;
3) materialization advanced treatment: pH value adjustment, strengthening Fenton oxidation, flocculation sediment;
4) whole mattress sinking water: heavy, draining eventually.
Preferably, the treatment process of described high salt pharmacy waste water, it comprises the following steps:
1) physico-chemical pretreatment: high salt pharmacy waste water enters catalysis and micro-electrolysis pond, catalysis and micro-electrolysis system is made up of iron-carbon-metal-oxygen, catalyzed oxidation Recalcitrant chemicals, improve wastewater biodegradability, then desulfurization pond I is entered, add lime according to sulfate concentration in water and carry out desulfurization, water outlet enters settling tank and precipitates, and enters next workshop section after supernatant liquor adjustment pH;
2) desulfurization biological treatment: upper workshop section's water enters anoxic biological treatment tank, the organic macromolecule fast hydrolyzings such as protein, fat, starch are the small molecules such as amino acid, lipid acid, glycerine, monose by acidication bacterium, and sulfate reduction is sulfide by sulphate reducing bacteria; The water outlet of anoxic biological treatment tank enters desulfurization pond II, adds ferrous salt and is stirred, precipitated sulfur compound; The water outlet of desulfurization pond enters anaerobic biological treatment pond, and the organic molecule that methanogen utilizes acidication to produce produces clean energy biogas; The water outlet of anaerobic biological treatment pond enters aerobic treatment biological tank, under aerobic environment, remove the organic pollutants such as most COD, and water outlet enters next workshop section;
3) materialization advanced treatment: enter strengthening Fenton oxidation reaction tank after a upper workshop section water adjustment pH, strengthening Fenton oxidation reaction system is made up of ferrous sulfate-hydrogen peroxide-Zero-valent Iron-oxygen, the pollutent such as medicine intermediate, microbiotic residual in exhaustive oxidation Decomposition Wastewater, Zero-valent Iron reuses, and enters next workshop section after the flocculation of water outlet alkali tune;
4) whole mattress sinking water: upper workshop section's water enters final deposition pool, discharge supernatant liquor, high salt pharmacy waste water is disposed.
Further preferably, the treatment process of described high salt pharmacy waste water, it comprises the following steps:
1) physico-chemical pretreatment: high salt pharmacy waste water enters catalysis and micro-electrolysis pond, in catalysis and micro-electrolysis system, the mass ratio of iron-carbon-metal is (5-20): (1-5): (2-8), wherein said metal is one in aluminium, copper, zinc or its combination, dissolved oxygen concentration is 0.5-2.0mg/L, and the reaction times is 60-120min; Then waste water enters desulfurization pond I, and in lime adding amount and water, the mol ratio of sulfate radical is (1-5): 1, and water outlet enters settling tank and precipitates, and enters next workshop section after supernatant liquor adjustment pH to 6-8;
2) desulfurization biological treatment: upper workshop section's water enters anoxic biological tank, adds photosynthetic bacterium bacteria suspension according to wastewater volume, and dosage is 2.0 ‰ ~ 10 ‰, and dissolved oxygen concentration is 0.1-0.3mg/L, and the residence time is 8-12 hour; The water outlet of anoxic biological tank enters desulfurization pond II, and wherein the mol ratio of ferrous salt and Sulfide in water is (0.5-2): 1, and ferrous salt is one in ferrous sulfate, iron protochloride or its combination; The water outlet of desulfurization pond enters anaerobe pond, and the residence time is 6-8 hour; The water outlet of anaerobe pond enters aerobe pond, and dissolved oxygen concentration is 3-5mg/L, and the residence time is 6-10 hour, and water outlet enters next workshop section;
3) materialization advanced treatment: enter strengthening Fenton oxidation reaction tank after a upper workshop section water adjustment pH to 3-5, the wherein preferred iron vitriol of ferrous sulfate, in its add-on and water, the mass ratio of COD is 1:(5-20), the mass ratio of iron vitriol-hydrogen peroxide-Zero-valent Iron is (1-5): (2-10): (8-20), dissolved oxygen concentration is 0.5-2.0mg/L, reaction times is 20-30min, wherein said Zero-valent Iron is iron plane flower, one in waste iron filing or its combination, Zero-valent Iron reuses, water outlet alkali tune pH to 7-8 enters next workshop section after flocculating,
4) whole mattress sinking water: upper workshop section's water enters final deposition pool, discharge supernatant liquor, high salt pharmacy waste water is disposed.
Select most scheme as of the present invention, following parameter limited:
1) in physico-chemical pretreatment workshop section, catalysis and micro-electrolysis system, the mass ratio of iron-carbon-metal is (10-15): (2-4): (3-5); In lime adding amount and water, the mol ratio of sulfate radical is (2-3): 1.
2), in desulfurization biological treatment workshop section, photosynthetic bacterium is 5.0 ‰ ~ 7.0 ‰ with the dosage of wastewater volume ratio, and photosynthetic bacterium bacteria suspension is photosynthetic bacterium bacteria suspension that is commercially available or that cultivate voluntarily, and wherein the concentration of photosynthetic bacterium is greater than 109/milliliter; The mol ratio of ferrous salt and Sulfide in water is (0.8-1): 1.
3) in materialization advanced treatment workshop section, in the add-on of iron vitriol and water, the mass ratio of COD is 1:(10-15), the mass ratio of iron vitriol-hydrogen peroxide-Zero-valent Iron is (2-4): (6-8): (12-15).
4) pH adjusting agent is for adjusting and reducing agent or acidity regulator, and wherein adjusting and reducing agent is one in sodium hydroxide, calcium hydroxide or its combination, and acidity regulator is one in sulfuric acid, hydrochloric acid or its combination.
5) anoxic biological treatment is acidication technique; Anaerobic treatment technique is the one in UASB, IC technique, and aerobic biological treatment process is the one in SBR, CASS, A/O; Described dissolved oxygen generator is the one in perforated pipe aerating regulation, disc type aeration.
High salt pharmacy wastewater treatment combination process of the present invention is adapted to process the high salt pharmacy waste water with following feature: COD≤8000mg/l, Liu Suan Gen≤3000mg/l, and containing medicine intermediate and antibiotic remains.
Compare with existing method of wastewater treatment, high salt pharmacy wastewater treatment method tool of the present invention has the following advantages:
1) present invention process combination is reasonable, technical data is reliable, adapts to high salt pharmacy waste water water quality requirement, and the waste water quality after process is stablized, and meets the requirement of " integrated wastewater discharge standard " (GB8978-1996) first discharge standard.
2) in conventional light electrolysis system, add the metal composition iron-carbon-metal-oxygen multiple catalyzing light electrolysis systems such as aluminium, copper, zinc, Recalcitrant chemicals in catalyzed oxidation waste water, improve wastewater biodegradability, effectively reduce organic loading and the toxicity inhibition of biological treatment.
3) utilize cheap lime as pretreated primary desulfurization, running cost is low, makes most of sulfate radical in waste water be precipitated removal.
4) in conventional diphasic anaerobic technique, set up ferrous salt desulfurization workshop section, precipitated sulfur compound, effectively reduce the restraining effect of sulfide to methanogen, and provide good influent quality for aerobic biosystem.
5) in conventional anoxic process, photosynthetic bacterium is added, the advantages such as photosynthetic bacterium has resistance to high organic loading, resistance to high salinity, oxygen requirement is little, temperature influence is little, Co metabolism system is formed with floras such as acidication bacterium, sulphate reducing bacterias, being the small molecules such as amino acid, lipid acid by the macromole such as protein, fat fast hydrolyzing, is sulfide by sulfate reduction.
6) in conventional Fenton oxidation system, add Zero-valent Iron form iron vitriol-hydrogen peroxide-Zero-valent Iron-oxygen boosting Fenton oxidation system, Zero-valent Iron progressively separates out ferrous ion in acid condition, avoid the disposable problem adding ferrous salt and cause part iron ion excessive, meanwhile, the metal ion such as Zero-valent Iron and its nickel contained, manganese plays the effect of catalysis to Fenton oxidation.
7) height salt pharmacy waste water combined treatment process of the present invention can make hardly degraded organic substance in waste water, residual intermediate and the open loop of microbiotic scission of link, eliminate bio-toxicity, exhaustive oxidation is CO2 and H2O, COD Nong Du≤8000mg/l can be adapted to, the process of the high salt pharmacy waste water of Liu Suan Gen≤3000mg/l.
Embodiment
It should be noted that and understand, when not departing from the spirit and scope of the present invention required by accompanying claim, various amendment and improvement can be made to the present invention.Therefore, the scope of claimed technical scheme is not by the restriction of given any specific exemplary teachings.
Embodiment 1:
Certain pharmaceutical factory mainly produces chemical synthesis pharmaceutical, medicine intermediate, semisynthetic antibiotics, its waste water produced be mainly derived from extraction, centrifugal, filter, distillation and salt the production link such as to wash, pollutant kind complexity, COD concentration, sulfate concentration are high.Water-quality guideline is in table one.Adopt treatment process of the present invention to process, operate as follows:
High salt pharmacy waste water enters catalysis and micro-electrolysis pond, and the mass ratio of iron-carbon-metal is 12:3:4, and wherein metal is aluminium and copper is the composition of 1:1 in mass ratio, and dissolved oxygen concentration is 1.0mg/L, and the reaction times is 90min; Waste water enters desulfurization pond I after completion of the reaction, and in lime adding amount and water, the mol ratio of sulfate radical is 2:1, and water outlet enters settling tank and precipitates; Enter anoxic biological tank after supernatant liquor adjustment pH to 7, add photosynthetic bacterium bacteria suspension 6.0 ‰ according to wastewater volume, dissolved oxygen concentration is 0.2mg/L, and the residence time is 10 hours; The water outlet of anoxic biological tank enters desulfurization pond II, is that 1:1 adds ferrous sulfate according to the mol ratio of ferrous salt and Sulfide in water; The water outlet of desulfurization pond enters anaerobe pond, and the residence time is 8 hours; The water outlet of anaerobe pond enters aerobe pond, and dissolved oxygen concentration is 4g/L, and the residence time is 8 hours; Strengthening Fenton oxidation reaction tank is entered after water outlet adjustment pH to 4.0, be that 1:12 adds iron vitriol according to the mass ratio of COD in iron vitriol and water, according to the mass ratio of iron vitriol-hydrogen peroxide-Zero-valent Iron be 3:7:15 add hydrogen peroxide and iron plane flower, dissolved oxygen concentration is 0.5mg/L, reaction times is 30min, water outlet alkali tune pH to 8 enters final deposition pool after flocculating, and discharge supernatant liquor, high salt pharmacy waste water is disposed.
Each unit water quality situation is in table one.
Table one, influent quality and each processing unit effluent quality
Embodiment 2:
Certain pharmaceutical factory mainly produces microbiotic, antitumor class medicine, its waste water produced be mainly derived from extraction, centrifugal, filter, distillation and salt the production link such as to wash, pollutant kind complexity, COD concentration, sulfate concentration are high.Water-quality guideline is in table two.Adopt treatment process of the present invention to process, operate as follows:
High salt pharmacy waste water enters catalysis and micro-electrolysis pond, and the mass ratio of iron-carbon-metal is 15:7:8, and wherein metal is aluminum and zinc copper is the composition of 1:1 in mass ratio, and dissolved oxygen concentration is 1.5mg/L, and the reaction times is 120min; Waste water enters desulfurization pond I after completion of the reaction, and in lime adding amount and water, the mol ratio of sulfate radical is 4:1, and water outlet enters settling tank and precipitates; Enter anoxic biological tank after supernatant liquor adjustment pH to 6, add photosynthetic bacterium bacteria suspension 8 ‰ according to wastewater volume, dissolved oxygen concentration is 0.2mg/L, and the residence time is 8 hours; The water outlet of anoxic biological tank enters desulfurization pond II, is that 2:1 adds ferrous sulfate according to the mol ratio of ferrous salt and Sulfide in water; The water outlet of desulfurization pond enters anaerobe pond, and the residence time is 7 hours; The water outlet of anaerobe pond enters aerobe pond, and dissolved oxygen concentration is 3mg/L, and the residence time is 10 hours; Strengthening Fenton oxidation reaction tank is entered after water outlet adjustment pH to 4.0, be that 1:16 adds iron vitriol according to the mass ratio of COD in iron vitriol and water, be that 5:9:16 adds hydrogen peroxide and waste iron filing according to the mass ratio of iron vitriol-hydrogen peroxide-Zero-valent Iron, dissolved oxygen concentration is 1.0mg/L, reaction times is 30min, water outlet alkali tune pH to 8 enters final deposition pool after flocculating, and discharge supernatant liquor, high salt pharmacy waste water is disposed.
Each unit water quality situation is in table two.
Table two, influent quality and each processing unit effluent quality
As can be seen from embodiment 1 and embodiment 2, adopt combined treatment process process for producing chemosynthesis pharmacy of the present invention, during the processing wastewater of the medicines such as medicine intermediate, semisynthetic antibiotics, microbiotic, antitumor class, physico-chemical pretreatment workshop section and desulfurization biological treatment workshop section high to total salt quantity removal efficiency, be greater than 60% and be greater than 70% respectively, desulfurization biological treatment workshop section and materialization advanced treatment workshop section high to COD clearance, be greater than 94% and be greater than 69.5% respectively, and the removal mainly desulfurization biological treatment workshop section to NH3-N, clearance is greater than 95%.After process, water outlet meets the requirement of " integrated wastewater discharge standard " (GB8978-1996) first discharge standard.
Claims (10)
1. a treatment process for high salt pharmacy waste water, it is characterized in that, it comprises the following steps:
1) physico-chemical pretreatment;
2) desulfurization biological treatment;
3) materialization advanced treatment;
4) whole mattress sinking water.
2. the treatment process of high salt pharmacy waste water as claimed in claim 1, it is characterized in that, it comprises the following steps:
1) physico-chemical pretreatment: catalysis and micro-electrolysis, lime desulfurization precipitation, pH value adjustment;
2) desulfurization biological treatment: anoxic biological treatment, molysite desulfurization process, anaerobic biological treatment, Aerobic biological process;
3) materialization advanced treatment: pH value adjustment, strengthening Fenton oxidation, flocculation sediment;
4) whole mattress sinking water: heavy, draining eventually.
3. the treatment process of high salt pharmacy waste water as claimed in claim 2, its feature exists, and it comprises the following steps:
1) physico-chemical pretreatment: high salt pharmacy waste water enters catalysis and micro-electrolysis pond, catalysis and micro-electrolysis system is made up of iron-carbon-metal-oxygen, catalyzed oxidation Recalcitrant chemicals, improve wastewater biodegradability, then desulfurization pond I is entered, add lime according to sulfate concentration in water and carry out desulfurization, water outlet enters settling tank and precipitates, and enters next workshop section after supernatant liquor adjustment pH;
2) desulfurization biological treatment: upper workshop section's water enters anoxic biological treatment tank, the organic macromolecule fast hydrolyzings such as protein, fat, starch are the small molecules such as amino acid, lipid acid, glycerine, monose by acidication bacterium, and sulfate reduction is sulfide by sulphate reducing bacteria; The water outlet of anoxic biological treatment tank enters desulfurization pond II, adds ferrous salt and is stirred, precipitated sulfur compound; The water outlet of desulfurization pond enters anaerobic biological treatment pond, and the organic molecule that methanogen utilizes acidication to produce produces clean energy biogas; The water outlet of anaerobic biological treatment pond enters aerobic treatment biological tank, under aerobic environment, remove the organic pollutants such as most COD, and water outlet enters next workshop section;
3) materialization advanced treatment: enter strengthening Fenton oxidation reaction tank after a upper workshop section water adjustment pH, strengthening Fenton oxidation reaction system is made up of ferrous sulfate-hydrogen peroxide-Zero-valent Iron-oxygen, the pollutent such as medicine intermediate, microbiotic residual in exhaustive oxidation Decomposition Wastewater, Zero-valent Iron reuses, and enters next workshop section after the flocculation of water outlet alkali tune;
4) whole mattress sinking water: upper workshop section's water enters final deposition pool, discharge supernatant liquor, high salt pharmacy waste water is disposed.
4. the treatment process of high salt pharmacy waste water as claimed in claim 3, it is characterized in that, it comprises the following steps:
1) physico-chemical pretreatment: high salt pharmacy waste water enters catalysis and micro-electrolysis pond, in catalysis and micro-electrolysis system, the mass ratio of iron-carbon-metal is (5-20): (1-5): (2-8), wherein said metal is one in aluminium, copper, zinc or its combination, dissolved oxygen concentration is 0.5-2.0mg/L, and the reaction times is 60-120min; Then waste water enters desulfurization pond I, and in lime adding amount and water, the mol ratio of sulfate radical is (1-5): 1, and water outlet enters settling tank and precipitates, and enters next workshop section after supernatant liquor adjustment pH to 6-8;
2) desulfurization biological treatment: upper workshop section's water enters anoxic biological tank, adds photosynthetic bacterium bacteria suspension according to wastewater volume, and dosage is 2.0 ‰ ~ 10 ‰, and dissolved oxygen concentration is 0.1-0.3mg/L, and the residence time is 8-12 hour; The water outlet of anoxic biological tank enters desulfurization pond II, and wherein the mol ratio of ferrous salt and Sulfide in water is (0.5-2): 1, and ferrous salt is one in ferrous sulfate, iron protochloride or its combination; The water outlet of desulfurization pond enters anaerobe pond, and the residence time is 6-8 hour; The water outlet of anaerobe pond enters aerobe pond, and dissolved oxygen concentration is 3-5mg/L, and the residence time is 6-10 hour, and water outlet enters next workshop section;
3) materialization advanced treatment: enter strengthening Fenton oxidation reaction tank after a upper workshop section water adjustment pH to 3-5, the wherein preferred iron vitriol of ferrous sulfate, in its add-on and water, the mass ratio of COD is 1:(5-20), the mass ratio of iron vitriol-hydrogen peroxide-Zero-valent Iron is (1-5): (2-10): (8-20), dissolved oxygen concentration is 0.5-2.0mg/L, reaction times is 20-30min, wherein said Zero-valent Iron is iron plane flower, one in waste iron filing or its combination, Zero-valent Iron reuses, water outlet alkali tune pH to 7-8 enters next workshop section after flocculating,
4) whole mattress sinking water: upper workshop section's water enters final deposition pool, discharge supernatant liquor, high salt pharmacy waste water is disposed.
5. the treatment process of high salt pharmacy waste water as claimed in claim 4, is characterized in that, in physico-chemical pretreatment workshop section, and catalysis and micro-electrolysis system, the mass ratio of iron-carbon-metal is (10-15): (2-4): (3-5); In lime adding amount and water, the mol ratio of sulfate radical is (2-3): 1.
6. the treatment process of high salt pharmacy waste water as claimed in claim 4, it is characterized in that, in desulfurization biological treatment workshop section, photosynthetic bacterium is 5.0 ‰ ~ 7.0 ‰ with the dosage of wastewater volume ratio, photosynthetic bacterium bacteria suspension is photosynthetic bacterium bacteria suspension that is commercially available or that cultivate voluntarily, and wherein the concentration of photosynthetic bacterium is greater than 10
9individual/milliliter; The mol ratio of ferrous salt and Sulfide in water is (0.8-1): 1.
7. the treatment process of high salt pharmacy waste water as claimed in claim 4, it is characterized in that, in materialization advanced treatment workshop section, in the add-on of iron vitriol and water, the mass ratio of COD is 1:(10-15), the mass ratio of iron vitriol-hydrogen peroxide-Zero-valent Iron is (2-4): (6-8): (12-15).
8. the treatment process of the high salt pharmacy waste water as described in as arbitrary in claim 2-4, it is characterized in that, described pH adjusting agent is for adjusting and reducing agent or acidity regulator, and wherein adjusting and reducing agent is one in sodium hydroxide, calcium hydroxide or its combination, and acidity regulator is one in sulfuric acid, hydrochloric acid or its combination.
9. the treatment process of the high salt pharmacy waste water as described in as arbitrary in claim 2-7, it is characterized in that, described anoxic biological treatment is acidication technique; Anaerobic treatment technique is the one in UASB, IC technique, and aerobic biological treatment process is the one in SBR, CASS, A/O; Described dissolved oxygen generator is the one in perforated pipe aerating regulation, disc type aeration.
10. the treatment process of high salt pharmacy waste water as claimed in claim 1, is characterized in that described high salt pharmacy waste water has following feature: COD≤8000mg/L, Liu Suan Gen≤3000mg/L, and containing medicine intermediate and antibiotic remains.
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| CN108046427A (en) * | 2018-01-09 | 2018-05-18 | 衢州学院 | Low C/S is than the anaerobic bio-treated method of sulfate-containing organic wastewater under room temperature |
| CN108298699A (en) * | 2018-03-02 | 2018-07-20 | 云南龙帜环境工程有限公司 | A kind of pharmaceutical wastewater integrated processing technique |
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| CN108046427A (en) * | 2018-01-09 | 2018-05-18 | 衢州学院 | Low C/S is than the anaerobic bio-treated method of sulfate-containing organic wastewater under room temperature |
| CN108298699A (en) * | 2018-03-02 | 2018-07-20 | 云南龙帜环境工程有限公司 | A kind of pharmaceutical wastewater integrated processing technique |
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| CN112744981A (en) * | 2020-12-25 | 2021-05-04 | 新疆水处理工程技术研究中心有限公司 | High-sulfur and high-COD wastewater treatment system and treatment method |
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