CN107265738A - Pharmacy wastewater treatment system and processing method - Google Patents
Pharmacy wastewater treatment system and processing method Download PDFInfo
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- CN107265738A CN107265738A CN201710697122.4A CN201710697122A CN107265738A CN 107265738 A CN107265738 A CN 107265738A CN 201710697122 A CN201710697122 A CN 201710697122A CN 107265738 A CN107265738 A CN 107265738A
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- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 41
- 238000003672 processing method Methods 0.000 title abstract description 8
- 239000002351 wastewater Substances 0.000 claims abstract description 198
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 57
- -1 iron-carbon Chemical compound 0.000 claims abstract description 36
- 239000006228 supernatant Substances 0.000 claims abstract description 20
- 230000003197 catalytic Effects 0.000 claims abstract description 14
- 238000006385 ozonation reaction Methods 0.000 claims abstract description 11
- 238000002425 crystallisation Methods 0.000 claims abstract description 8
- 230000005712 crystallization Effects 0.000 claims abstract description 8
- 239000000047 product Substances 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 238000004064 recycling Methods 0.000 claims abstract description 5
- 230000001105 regulatory Effects 0.000 claims description 79
- 238000003860 storage Methods 0.000 claims description 29
- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 27
- 239000010802 sludge Substances 0.000 claims description 22
- 238000001914 filtration Methods 0.000 claims description 19
- 238000004062 sedimentation Methods 0.000 claims description 15
- 238000005189 flocculation Methods 0.000 claims description 12
- 230000016615 flocculation Effects 0.000 claims description 12
- 239000003513 alkali Substances 0.000 claims description 11
- 238000001556 precipitation Methods 0.000 claims description 10
- 239000003795 chemical substances by application Substances 0.000 claims 1
- 230000005611 electricity Effects 0.000 claims 1
- 238000001704 evaporation Methods 0.000 abstract description 22
- 238000000034 method Methods 0.000 abstract description 16
- 230000000694 effects Effects 0.000 abstract description 13
- 241000276438 Gadus morhua Species 0.000 description 18
- 235000019516 cod Nutrition 0.000 description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 239000003814 drug Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 10
- 239000003344 environmental pollutant Substances 0.000 description 9
- 231100000719 pollutant Toxicity 0.000 description 9
- 239000000126 substance Substances 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 238000000354 decomposition reaction Methods 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 150000001780 cephalosporins Chemical class 0.000 description 4
- 238000004332 deodorization Methods 0.000 description 4
- SOCTUWSJJQCPFX-UHFFFAOYSA-N dichromate(2-) Chemical compound [O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O SOCTUWSJJQCPFX-UHFFFAOYSA-N 0.000 description 4
- 238000006460 hydrolysis reaction Methods 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 229920002401 polyacrylamide Polymers 0.000 description 4
- 238000004448 titration Methods 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 238000003556 assay method Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 238000007792 addition Methods 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000004059 degradation Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 229940079593 drugs Drugs 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- JEXVQSWXXUJEMA-UHFFFAOYSA-N pyrazol-3-one Chemical compound O=C1C=CN=N1 JEXVQSWXXUJEMA-UHFFFAOYSA-N 0.000 description 2
- 241000894007 species Species 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 229910017112 Fe—C Inorganic materials 0.000 description 1
- KJFMBFZCATUALV-UHFFFAOYSA-N Phenolphthalein Chemical compound C1=CC(O)=CC=C1C1(C=2C=CC(O)=CC=2)C2=CC=CC=C2C(=O)O1 KJFMBFZCATUALV-UHFFFAOYSA-N 0.000 description 1
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound [N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 239000001166 ammonium sulphate Substances 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-O azanium;sulfuric acid Chemical compound [NH4+].OS(O)(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-O 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 230000003115 biocidal Effects 0.000 description 1
- 229960000074 biopharmaceuticals Drugs 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking Effects 0.000 description 1
- 210000004027 cells Anatomy 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- XKUUMWKWUZRRPD-UHFFFAOYSA-N heptan-2-amine;sulfuric acid Chemical compound [O-]S([O-])(=O)=O.CCCCCC(C)[NH3+].CCCCCC(C)[NH3+] XKUUMWKWUZRRPD-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 238000005020 pharmaceutical industry Methods 0.000 description 1
- 238000001226 reprecipitation Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 210000004215 spores Anatomy 0.000 description 1
- 230000001954 sterilising Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water, or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46176—Galvanic cells
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/02—Odour removal or prevention of malodour
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
Abstract
The present invention relates to a kind of pharmacy wastewater treatment system and processing method.The processing method of the pharmacy waste water comprises the following steps：Collect pharmacy waste water, pH value is adjusted, iron-carbon micro-electrolysis is carried out and obtains electrolysis wastewater, it is 7~12 to adjust pH value, add flocculant, supernatant waste water is precipitated to obtain, catalytic ozonation processing is carried out to supernatant waste water, oxidized waste water is obtained, it is 1~10 to adjust pH value, it is transferred in evaporator and is evaporated concentration, crystallization, collects product, and collect condensate liquid recycling.The technical process of the pharmacy wastewater treatment method and the pharmacy wastewater treatment system, the organic pollution in pharmacy waste water can effectively be removed, the line clogging problem in evaporator evaporation processing can be effectively prevented from the whole, and to the high treating effect of pharmacy waste water, and the biodegradability of pharmacy waste water can be effectively improved.
Description
Technical field
The present invention relates to pharmacy wastewater treatment field, more particularly to a kind of pharmacy wastewater treatment system and processing method.
Background technology
Pharmaceutical industry mainly includes chemical pharmacy, bio-pharmaceuticals, Chinese patent drug, agricultural chemicals etc., and pharmaceuticals industry waste water mainly includes
Washings in antibiotic production wastewater, synthetic drug production waste water, Chinese patent medicine production wastewater and all kinds of formulation manufacturing processes
With several major classes such as flushing waste water.The characteristics of pharmacy waste water is that composition is complicated, and organic pollution content is very high, it is more difficult to handle.Pharmacy
COD COD (Chemical Oxygen Demand, abbreviation COD) value of waste water is very high and fluctuates larger, life on the five
Change oxygen demand BOD5(five days'Biochemical Oxygen Demand：BOD5) content differs.BOD5/CODCrValue difference is different
Larger, some pharmacy waste waters also have the ammonia nitrogen or other high concentration inorganic salts of higher concentration, and biodegradability is poor.Generally
Think BOD5/CODCr>0.3 wastewater biodegradability is preferable, BOD5/CODCr<0.3 waste water is considered as hardly possible by biochemical treatment.
Because pharmaceutical factory generally uses Batch Process, the species of product is changed greatly, and causes water quality, the water of pharmacy waste water
Amount and the species of pollutant are changed greatly.Organic contamination concentration in usual pharmacy waste water is high and causes colourity deep, and toxicity is big, Gu
Body suspension (SS) concentration is also high.
At present, pharmacy industry for water content is relatively fewer and waste water that pollutant concentration is higher, both economical feasible place
Reason method includes evaporation, combustion method and supercritical oxidation process etc..
Wherein, evaporation is typically what is carried out in the evaporative component comprising evaporator, in evaporation process, pharmacy waste water
In nonvolatile matter gradually concentrated, concentration to a certain extent after, concentrate can be centrifuged, crystallized
Deng, according to crystallization obtain solid matter difference handled accordingly.Evaporating obtained condensate according to circumstances can be direct
Carry out reuse or carry out other processing again.The waste water containing high-concentration sulfuric acid ammonium is often produced in cephalosporins medicine production,
The COD of this kind of waste waterCrValue is generally more than tens thousand of milligrams per liter, and color is deeper, because ammonium sulphate content is high and causes such to give up
Water does not have the possibility of direct biochemical treatment.
High boiling point organic compound in pharmacy waste water is easy to condense on the inner-walls of duct of evaporator in evaporation process, knot
Tab phenolphthaleinum induced evaporation device line clogging.It is always several big encountered in evaporation Pharmaceutical Wastewater Treatment process that evaporator pipeline, which is blocked,
One of problem.
The content of the invention
Based on this, it is necessary to can prevent evaporator from blocking and the system good to pharmacy wastewater treatment effect for offer is a kind of
Medicine Waste Water Treatment and processing method.
A kind of pharmacy wastewater treatment system, including wastewater collection pond, the first pH regulating reservoirs, iron-carbon micro-electrolysis device, second
PH regulating reservoirs, sedimentation basin, ozone treatment apparatus, the 3rd pH regulating reservoirs and evaporator；
The wastewater collection pond is used to collect pharmacy waste water；
The first pH regulating reservoirs are connected with the wastewater collection pond and the iron-carbon micro-electrolysis device respectively, and described
One pH regulating reservoirs are used for the pH value for adjusting the pharmacy waste water being transferred to from the wastewater collection pond；
The 2nd pH regulating reservoirs are connected with the iron-carbon micro-electrolysis device and the sedimentation basin respectively, the 2nd pH
Regulating reservoir is used to the electrolysis wastewater being transferred to from the iron-carbon micro-electrolysis device being adjusted to alkalescence, the sedimentation basin also with it is described smelly
Oxygen processing unit is connected；
The 3rd pH regulating reservoirs are connected with the ozone treatment apparatus, and the 3rd pH regulating reservoirs are used for will be from the ozone
The oxidized waste water that processing unit is transferred to is adjusted to acidity；
The evaporator is connected by pipeline with the 3rd pH regulating reservoirs.
In one of the embodiments, the pharmacy wastewater treatment system also includes sludge filter press, the sludge press filtration
Machine is connected with the sedimentation basin and the ozone treatment apparatus respectively.
In one of the embodiments, the pharmacy wastewater treatment system also includes the sour storage pool, the acid storage
Pond is connected with the first pH regulating reservoirs and/or the 3rd pH regulating reservoirs.
In one of the embodiments, the pharmacy wastewater treatment system also includes alkali storage pool and flocculant storage pool,
The alkali storage pool is connected by pipeline with the 2nd pH regulating reservoirs, and the flocculant storage pool is used for the 2nd pH
Regulating reservoir supplies flocculant.
In one of the embodiments, the first pH regulating reservoirs, the 2nd pH regulating reservoirs described in the pharmacy wastewater treatment system
PH meter and agitating device are equipped with the 3rd pH regulating reservoirs.
A kind of pharmacy wastewater treatment method, using above-mentioned pharmacy wastewater treatment system, comprises the following steps：
S1, collects pharmacy waste water；
S2,1~12 is adjusted to by the pH value of the pharmacy waste water, is carried out iron-carbon micro-electrolysis, is obtained electrolysis wastewater；
S3,7~12 are adjusted to by the pH value of the step S2 electrolysis wastewaters obtained, add flocculant, and precipitation obtains upper waste cleaning
Water；
S4, carries out catalytic ozonation processing to the supernatant waste water obtained in step S3, obtains oxidized waste water；
S5,1~10 is adjusted to by the oxidized waste water pH value that step S4 is obtained, and is transferred in evaporator and is evaporated concentration, knot
Crystalline substance, collects product, and collect condensate liquid recycling.
In one of the embodiments, in step s 4, in addition to by the first sludge obtained in step S3 press filtration is carried out
Processing, obtains the second sludge and press filtration waste water, and the press filtration waste water and the upper waste cleaning are hydrated simultaneously, carries out the ozone catalytic
Oxidation processes, obtain the oxidized waste water.
In one of the embodiments, in step s 2, the pH value of the pharmacy waste water is adjusted to 3~5；
In step s3, the pH value of the electrolysis wastewater is adjusted to 8~10；And/or
In step s 5, the pH value of the oxidized waste water is adjusted to 3~6.
In one of the embodiments, in step s 2, the time of the iron-carbon micro-electrolysis is 1~30h；And/or
In step s3, the time of the precipitation is 1~10h.
In one of the embodiments, in step s 2, the time of the iron-carbon micro-electrolysis is 2.5~4h；And/or
In step s3, the time of the precipitation is 1.5~4h.
Above-mentioned pharmacy wastewater treatment system includes wastewater collection pond, the first pH regulating reservoirs, iron-carbon micro-electrolysis device, the 2nd pH
Regulating reservoir, sedimentation basin, ozone treatment apparatus, the 3rd pH regulating reservoirs and evaporator, wherein wastewater collection pond give up for collecting pharmacy
Water, the first pH regulating reservoirs are mainly used in the pH value for the pharmacy waste water that regulation is transferred to from the wastewater collection pond to meet iron
PH value requirement of the carbon micro-electrolysis device to pharmacy waste water, the 2nd pH regulating reservoirs are used to be transferred to from the iron-carbon micro-electrolysis device
Electrolysis wastewater be adjusted to alkalescence with reprecipitation pond precipitate obtain supernatant waste water, ozone treatment apparatus be used for one is entered to supernatant waste water
Step sterilization, decolouring and deodorization, evaporator are used to evaporate the oxidized waste water handled by the 3rd pH regulating reservoirs, receive evaporation product.
It disclosure satisfy that the technical process requirement of pharmacy wastewater treatment method on the whole using above-mentioned pharmacy wastewater treatment system, effectively keep away
Exempt from the line clogging problem in evaporator evaporation process, and to the high treating effect of pharmacy waste water, and pharmacy can be effectively improved
The biodegradability of waste water.
Above-mentioned pharmacy wastewater treatment method comprises the following steps：Pharmacy waste water is collected, the pH value of pharmacy waste water is adjusted to 1~
12, to meet the pH requirements of iron-carbon micro-electrolysis, carry out iron-carbon micro-electrolysis and obtain electrolysis wastewater, then the pH value of electrolysis wastewater is adjusted to 7~
12, flocculant is added, supernatant waste water is precipitated to obtain, catalytic ozonation processing is carried out to supernatant waste water, oxidized waste water is obtained, will aoxidize
PH value of waste water is adjusted to 1~10, is transferred in evaporator and is evaporated concentration, crystallization, collects product, and collects condensate liquid and reclaims profit
With.Wherein, it is to meet the pH requirements of iron-carbon micro-electrolysis the pH value of pharmacy waste water to be adjusted into 1~12 purpose；Pass through iron-carbon micro-electrolysis
Pollutant in pharmacy waste water is degraded, while metal ion also has the effect of hydrolysis flocculation, difficult biochemical can be made high
The biodegradability of concentration pharmacy waste water is improved；Substantial amounts of pollution impurity is removed by flocculation sediment again；It will be obtained again in precipitation process
The supernatant waste water obtained is further sterilized by catalytic ozonation, decolourized and deodorization, and effectively reduces COD value, is further improved
Biodegradability, and the line clogging problem being prevented effectively from evaporator evaporation processing.The technique of above-mentioned pharmacy wastewater treatment method
Process, can effectively remove the organic pollution in pharmacy waste water, can be effectively prevented from the whole in evaporator evaporation processing
Line clogging problem, and to the high treating effect of pharmacy waste water, and the biodegradability of pharmacy waste water can be effectively improved.
Brief description of the drawings
Fig. 1 is the step flow chart of the pharmacy wastewater treatment method of an embodiment；
Fig. 2 is the structure of the pharmacy wastewater treatment system of the pharmacy wastewater treatment method being used in Fig. 1 of an embodiment
Composition schematic diagram.
Embodiment
For the ease of understanding the present invention, the present invention is described more fully below with reference to relevant drawings.In accompanying drawing
Give presently preferred embodiments of the present invention.But, the present invention can be realized in many different forms, however it is not limited to this paper institutes
The embodiment of description.On the contrary, the purpose for providing these embodiments is to make the understanding to the disclosure more thorough
Comprehensively.
Unless otherwise defined, all of technologies and scientific terms used here by the article is with belonging to technical field of the invention
The implication that technical staff is generally understood that is identical.Term used in the description of the invention herein is intended merely to description tool
The purpose of the embodiment of body, it is not intended that in the limitation present invention.Term as used herein " and/or " include one or more phases
The arbitrary and all combination of the Listed Items of pass.
Incorporated by reference to Fig. 1, the pharmacy wastewater treatment method 10 of an embodiment comprises the following steps：
S1, collects pharmacy waste water.
S2,1~12 is adjusted to by the pH value of pharmacy waste water, is carried out iron-carbon micro-electrolysis, is obtained electrolysis wastewater.Adjust pharmacy waste water
The purpose of pH value is to meet the electrolytic condition requirement of iron-carbon micro-electrolysis.Wherein, Fe-C micro electrolysis is utilized in Process of Metallic Corrosion
Middle formation galvanic cell produces redox, produces chemical action to the pollutant in pharmacy waste water, carries out contaminant degradation.
Meanwhile, corrode the metal ion due to hydrolysis flocculation.
Preferably, the time of iron-carbon micro-electrolysis can be 1~30h.
Further, in this step, the pH value of pharmacy waste water is adjusted to 3~5, the time of iron-carbon micro-electrolysis can be
2.5~4h, to carry out chemical action to the pollutant in pharmacy waste water, and is further improved to the pollutant of iron-carbon micro-electrolysis
Degradation effect and hydrolysis flocculation.
S3,7~12 are adjusted to by the pH value of the step S2 electrolysis wastewaters obtained, add flocculant, and precipitation obtains supernatant waste water.
Preferably, in this step, the time of precipitation is 1~10h.
Further, in this step, the pH value of Decomposition Wastewater is adjusted to 8~10, time of precipitation can for 1.5~
4h, reaches preferable flocculation sediment effect.
Further, in this step, press filtration processing in addition to by the first sludge obtained in step S3 is carried out, second is obtained
Sludge and press filtration waste water, and press filtration waste water and upper waste cleaning are hydrated simultaneously, follow-up catalytic ozonation processing is carried out, must be aoxidized useless
Water.First sludge or the second sludge can otherwise processeds.
S4, catalytic ozonation processing is carried out to the pollutant in the supernatant waste water and press filtration waste water that are obtained in step S3,
Obtain oxidized waste water.
The process route that iron-carbon micro-electrolysis is engaged with catalytic ozonation, can be carried out to high concentration pharmacy organic wastewater
Deodorization, decolouring etc. are pre-processed, and can effectively reduce the COD value of pharmacy waste water, while improving the biodegradability of pharmacy waste water.
S5,1~10 is adjusted to by the oxidized waste water pH value that step S4 is obtained, be transferred in evaporator 800 be evaporated concentration,
Crystallization, collects product, and collect condensate liquid recycling.Preferably, in this step, the pH value of oxidized waste water is adjusted to 3~
4。
The pharmacy wastewater treatment method 10 of present embodiment, by carrying out iron after the pH value of pharmacy waste water is adjusted into 1~12
Carbon micro-electrolysis, while metal ion also has the effect of hydrolysis flocculation, can be made with being degraded to the pollutant in pharmacy waste water
The biodegradability of difficult biochemical high concentration medical wastewater is improved；Substantial amounts of pollution impurity is removed by flocculation sediment again；Again will be heavy
The supernatant waste water obtained during shallow lake is further sterilized by catalytic ozonation, decolourized and deodorization, and effectively reduces COD value,
Biodegradability is further improved, the line clogging problem during evaporator evaporation can be prevented effectively from after above-mentioned processing.On
The technical process of pharmacy wastewater treatment method is stated, the organic pollution in pharmacy waste water can be effectively removed, it is higher
The organic pollution of boiling point, the line clogging problem in the evaporation process of evaporator 800 can be effectively prevented from the whole, and to system
The high treating effect of medicine waste water, and the biodegradability of pharmacy waste water can be effectively improved.
Please further combined with Fig. 2, a kind of pharmacy wastewater treatment system 20, including wastewater collection pond 100, the first pH regulating reservoirs
200th, sour storage pool 210, iron-carbon micro-electrolysis device 300, the 2nd pH regulating reservoirs 400, alkali storage pool 410, flocculant storage pool
420th, sedimentation basin 500, ozone treatment apparatus 600, the 3rd pH regulating reservoirs 700 and evaporator 800.
In the present embodiment, wastewater collection pond 100 is used for the pharmacy waste water for collecting specified quantitative, for example, collect 50-
1000m3Pharmacy waste water once focused on.
In the present embodiment, the first pH regulating reservoirs 200 are provided with pH meter and agitating device.First pH regulating reservoirs 200 pass through
Pump and pipeline are connected with wastewater collection pond 100, and the first pH regulating reservoirs 200 are used to adjust what is be transferred to from wastewater collection pond 100
The pH value of pharmacy waste water.Preferably, the first pH regulating reservoirs 200 can be stored acid by pump by being connected with sour storage pool 210
Acid in pond 210 is pumped into the first pH regulating reservoirs 200, and startup agitating device is stirred to pharmacy waste water simultaneously, uses pH
Meter monitors to obtain the pharmacy waste water of certain ph scope in real time.
In the present embodiment, iron-carbon micro-electrolysis device 300 is connected by pipeline with the first pH regulating reservoirs 200, is used for
The pharmacy waste water adjusted in first pH regulating reservoirs 200 is pumped into and carries out iron-carbon micro-electrolysis, further by electrochemical action and
Flocculation removes the pollutant in pharmacy waste water, obtains Decomposition Wastewater.
In the present embodiment, the 2nd pH regulating reservoirs 400 are provided with pH meter and agitating device.2nd pH regulating reservoirs 400 pass through
Pipeline is connected with iron-carbon micro-electrolysis device 300, for the electrolysis wastewater being transferred to from iron-carbon micro-electrolysis device 300 to be adjusted into alkali
Property.
Preferably, the 2nd pH regulating reservoirs 400 also pass through pipeline and alkali storage pool 410.By pump by alkali storage pool 410
Alkali is pumped into the 2nd pH regulating reservoirs 400, and startup agitating device is stirred to Decomposition Wastewater simultaneously, is monitored in real time with pH meter
To obtain the Decomposition Wastewater of certain ph scope, adjust after pH, then the flocculant in flocculant storage pool 420 is pumped into
In two pH regulating reservoirs 400, it is uniformly mixed by agitating device, to improve the effect of flocculation sediment removal of impurities.
In the present embodiment, sedimentation basin 500 is connected by pipeline with the 2nd pH regulating reservoirs 400.When the 2nd pH regulations
After Decomposition Wastewater in pond 400 is adjusted through pH and mixed with flocculant, immediately by be pumped into carried out into sedimentation basin 500 it is quiet
Put, precipitate, obtain the first sludge and supernatant waste water.Preferably, the first sludge is pumped into sludge filter press 900 and further pressed
Squeeze, to obtain the second sludge and press filtration waste water.Press filtration waste water can be mixed with supernatant waste water.Second sludge can otherwise processed.
In the present embodiment, ozone treatment apparatus 600 is connected by pipeline with sedimentation basin 500, for that will precipitate
Supernatant waste water in pond 500 is drawn into row ozone treatment apparatus 600 by the pollution in the ozone and waste water of high oxidation activity
Thing carries out catalytic ozonation, and the secondary pollution such as no solid waste is produced.
In the present embodiment, the 3rd pH regulating reservoirs 700 are provided with pH meter and agitating device.3rd pH regulating reservoirs 700 pass through
Pipeline is connected with ozone treatment apparatus 600, for the oxidized waste water being transferred to from ozone treatment apparatus 600 to be adjusted into acidity.The
Three pH regulating reservoirs 700 are used for the pH value for adjusting the oxidized waste water being transferred to from ozone treatment apparatus 600.
Preferably, the 3rd pH regulating reservoirs 700 can be by being connected, by pump by sour storage pool 210 with sour storage pool 210
Acid be pumped into the 3rd pH regulating reservoirs 700, and simultaneously start agitating device pharmacy waste water is stirred, supervised in real time with pH meter
Survey to obtain the oxidized waste water of certain ph scope.
In the present embodiment, evaporator 800 is shifted the oxidized waste water in the 3rd pH regulating reservoirs 700 by pump and pipeline
Concentration, crystallization are evaporated into evaporator 800, product is collected, and collect condensate liquid recycling.
The pharmacy wastewater treatment method 10 of present embodiment can be carried out using pharmacy wastewater treatment system 20 to pharmacy waste water
Processing, can effectively remove the organic pollution in pharmacy waste water, more high boiling organic pollution can be overall
On be effectively prevented from line clogging problem in the evaporation process of evaporator 800, and to the high treating effect of pharmacy waste water, and can
Effectively improve the biodegradability of pharmacy waste water.
The present invention is explained with reference to specific embodiment.
Embodiment 1
The present embodiment provides a kind of processing method of cephalosporin wastewater, comprises the following steps：
(1) it is 700m using dischargeable capacity3Wastewater collection pond collect 650m3Cephalosporin wastewater, and test the head
The initial COD of spore class pharmacy waste waterCrContent.
(2) cephalosporin wastewater collected in wastewater collection pond is pumped into the first pH regulating reservoirs, opens agitating device and enter
Row stirring, while the sulfuric acid in sour storage pool is pumped into the first pH value regulating reservoir, between regulation pH value to 4~5, has been transferred to
Effect volume is 700m3Iron-carbon micro-electrolysis device carry out iron-carbon micro-electrolysis, time 3h, obtain electrolysis wastewater.
(3) electrolysis wastewater in step (2) is pumped into the 2nd pH regulating reservoirs, opens agitating device and be stirred, simultaneously
Ammoniacal liquor in alkali storage pool is pumped into the second pH value regulating reservoir, between regulation pH value to 9~10, then from flocculant storage pool
PAM (polyacrylamide) transfer input into the second pH value regulating reservoir, be well mixed.
(4) Decomposition Wastewater handled through step (3) is transferred to progress standing 3h in sedimentation basin, flocculation sediment obtains supernatant
Waste water and the first sludge.First sludge is subjected to press filtration processing, the second sludge and press filtration waste water is obtained, and by press filtration waste water and supernatant
Waste water merges, and is pumped into ozone treatment apparatus, opens ozone generator and carries out ozone processing, and controls the addition of ozone to be
1kg/t (ton), the catalytic oxidation time is 1h, obtains oxidized waste water.
(5) oxidized waste water for obtaining step (4) is pumped into the 3rd pH regulating reservoirs, is opened agitating device and is stirred, together
When sulfuric acid in sour storage pool is pumped into the 3rd pH value regulating reservoir, between regulation pH value to 3~4, after regulation terminates, be discharged into steaming
Concentrated, crystallized in hair device.COD before the evaporation in the 3rd pH value regulating reservoir is determined simultaneouslyCrContent.
After above-mentioned processing, the COD of the pharmacy waste water in the present embodimentCrValue changes are as follows：Made in wastewater collection pond
The initial COD of medicine waste waterCrValue is the COD of waste water in 23461mg/L, the 3rd pH value regulating reservoirCrValue is 8437mg/L.Measure side
Method：The measure dichromate titration (GB11914-89) of water chemical oxygen demand.
In the processing mode of cephalosporin wastewater in the present embodiment, without blockage problem in evaporator pipeline, and steam
The hair obtained ammonium sulfate color of crystallization is close to colourless, it is possible to increase its price.Meanwhile, COD before evaporationCrContent is reduced, and is evaporated
The BOD of the condensate arrived5/CODCrValue by it is untreated when 0.06 bring up to processing after 0.41 (assay method：Water quality life on the five
Change oxygen demand (BOD5) measure dilution with inocalation method (HJ505-2009), the measure dichromate titration of water chemical oxygen demand
(GB11914-89)).Due to BOD5/CODCrValue increases, thus improves the biodegradability of pharmacy waste water, for evaporating
Condensation waste water, its biochemical treatment difficulty can be reduced.
Embodiment 2
The present embodiment provides a kind of processing method of pyrazolone pharmacy waste water, comprises the following steps：
(1) it is 100m using dischargeable capacity3Wastewater collection pond collect 80m3Pyrazolone pharmacy waste water, and test the system
The initial COD of medicine waste waterCrContent.
(2) pharmacy waste water collected in wastewater collection pond is pumped into the first pH regulating reservoirs, opens agitating device and be stirred,
The sulfuric acid in sour storage pool is pumped into the first pH value regulating reservoir simultaneously, between regulation pH value to 3~4, dischargeable capacity is transferred to
For 100m3Iron-carbon micro-electrolysis device carry out iron-carbon micro-electrolysis, time 3h, obtain electrolysis wastewater.
(3) electrolysis wastewater in step (2) is pumped into the 2nd pH regulating reservoirs, opens agitating device and be stirred, simultaneously
Ammoniacal liquor in alkali storage pool is pumped into the second pH value regulating reservoir, between regulation pH value to 8~9, then from flocculant storage pool
PAM (polyacrylamide) transfer input into the second pH value regulating reservoir, be well mixed.
(4) Decomposition Wastewater handled through step (3) is transferred to progress standing 2h in sedimentation basin, flocculation sediment obtains supernatant
Waste water and the first sludge.First sludge is subjected to press filtration processing, the second sludge and press filtration waste water is obtained, and by press filtration waste water and supernatant
Waste water merges, and is pumped into ozone treatment apparatus, opens ozone generator and carries out ozone processing, and controls the addition of ozone to be
2kg/t (ton), the catalytic oxidation time is 3h, obtains oxidized waste water.
(5) oxidized waste water for obtaining step (4) is pumped into the 3rd pH regulating reservoirs, is opened agitating device and is stirred, together
When sulfuric acid in sour storage pool is pumped into the 3rd pH value regulating reservoir, between regulation pH value to 5~6, after regulation terminates, be discharged into steaming
Concentrated, crystallized in hair device.COD before the evaporation in the 3rd pH value regulating reservoir is determined simultaneouslyCrContent.
After above-mentioned processing, the COD of the pharmacy waste water in the present embodimentCrValue changes are as follows：Made in wastewater collection pond
The initial COD of medicine waste waterCrValue is the COD of waste water in 745mg/L, the 3rd pH value regulating reservoirCrValue is 150mg/L.Assay method：
The measure dichromate titration (GB11914-89) of water chemical oxygen demand.
In the processing mode of pharmacy waste water in the present embodiment, without blockage problem in evaporator pipeline, and evaporative crystallization
Obtained ammonium sulfate color is close to colourless, it is possible to increase its price.Meanwhile, COD before evaporationCrContent is reduced, and it is solidifying that evaporation is obtained
The BOD born water5/CODCrValue by it is untreated when 0.1 brought up to processing after 0.38 (assay method：Water quality biochemistry on the five is needed
Oxygen amount (BOD5) measure dilution with inocalation method (HJ505-2009), the measure dichromate titration of water chemical oxygen demand
(GB11914-89)).Due to BOD5/CODCrRaising has been worth to, thus has improved the biodegradability of pharmacy waste water, for evaporation
The condensation waste water gone out, can reduce its biochemical treatment difficulty.
Each technical characteristic of embodiment described above can be combined arbitrarily, to make description succinct, not to above-mentioned reality
Apply all possible combination of each technical characteristic in example to be all described, as long as however, the combination of these technical characteristics is not deposited
In contradiction, the scope of this specification record is all considered to be.
Embodiment described above only expresses the several embodiments of the present invention, and it describes more specific and detailed, but simultaneously
Can not therefore it be construed as limiting the scope of the patent.It should be pointed out that coming for one of ordinary skill in the art
Say, without departing from the inventive concept of the premise, various modifications and improvements can be made, these belong to the protection of the present invention
Scope.Therefore, the protection domain of patent of the present invention should be determined by the appended claims.
Claims (10)
1. a kind of pharmacy wastewater treatment system, it is characterised in that including wastewater collection pond, the first pH regulating reservoirs, iron-carbon micro-electrolysis
Device, the 2nd pH regulating reservoirs, sedimentation basin, ozone treatment apparatus, the 3rd pH regulating reservoirs and evaporator；
The wastewater collection pond is used to collect pharmacy waste water；
The first pH regulating reservoirs are connected with the wastewater collection pond and the iron-carbon micro-electrolysis device respectively, the first pH
Regulating reservoir is used for the pH value for adjusting the pharmacy waste water being transferred to from the wastewater collection pond；
The 2nd pH regulating reservoirs are connected with the iron-carbon micro-electrolysis device and the sedimentation basin respectively, the 2nd pH regulations
Pond is used to the electrolysis wastewater being transferred to from the iron-carbon micro-electrolysis device being adjusted to alkalescence, the sedimentation basin also with the ozone
Reason device is connected；
The 3rd pH regulating reservoirs are connected with the ozone treatment apparatus, and the 3rd pH regulating reservoirs are used to handle from the ozone
The oxidized waste water that device is transferred to is adjusted to acidity；
The evaporator is connected by pipeline with the 3rd pH regulating reservoirs.
2. pharmacy wastewater treatment system according to claim 1, it is characterised in that also including sludge filter press, the dirt
Mud filter press is connected with the sedimentation basin and the ozone treatment apparatus respectively.
3. pharmacy wastewater treatment system according to claim 1 or 2, it is characterised in that also including the sour storage pool, institute
Sour storage pool is stated with the first pH regulating reservoirs and/or the 3rd pH regulating reservoirs to be connected.
4. pharmacy wastewater treatment system according to claim 1 or 2, it is characterised in that also including alkali storage pool and flocculation
Agent storage pool, the alkali storage pool is connected by pipeline with the 2nd pH regulating reservoirs, the flocculant storage pool be used for
The 2nd pH regulating reservoirs supply flocculant.
5. pharmacy wastewater treatment system according to claim 1 or 2, it is characterised in that the first pH regulating reservoirs, second
PH regulating reservoirs and the 3rd pH regulating reservoirs are equipped with pH meter and agitating device.
6. a kind of pharmacy wastewater treatment method, it is characterised in that using the pharmacy waste water any one of claim 1 to 5
Processing system, comprises the following steps：
S1, collects pharmacy waste water；
S2,1~12 is adjusted to by the pH value of the pharmacy waste water, is carried out iron-carbon micro-electrolysis, is obtained electrolysis wastewater；
S3,7~12 are adjusted to by the pH value of the step S2 electrolysis wastewaters obtained, add flocculant, and precipitation obtains supernatant waste water；
S4, carries out catalytic ozonation processing to the supernatant waste water obtained in step S3, obtains oxidized waste water；
S5,1~10 is adjusted to by the oxidized waste water pH value that step S4 is obtained, and is transferred in evaporator and is evaporated concentration, crystallization, receives
Collect product, and collect condensate liquid recycling.
7. pharmacy wastewater treatment method according to claim 6, it is characterised in that in step s 4, in addition to by step
The first sludge for being obtained in S3 carries out press filtration processing, obtains the second sludge and press filtration waste water, and by the press filtration waste water with it is described on
Stripping is hydrated simultaneously, is carried out the catalytic ozonation processing, is obtained the oxidized waste water.
8. the pharmacy wastewater treatment method according to claim 6 or 7, it is characterised in that in step s 2, by the pharmacy
The pH value of waste water is adjusted to 3~5；
In step s3, the pH value of the electrolysis wastewater is adjusted to 8~10；And/or
In step s 5, the pH value of the oxidized waste water is adjusted to 3~6.
9. the pharmacy wastewater treatment method according to claim 6 or 7, it is characterised in that in step s 2, the iron carbon is micro-
The time of electrolysis is 1~30h；And/or
In step s3, the time of the precipitation is 1~10h.
10. pharmacy wastewater treatment method according to claim 9, it is characterised in that in step s 2, the micro- electricity of iron carbon
The time of solution is 2.5~4h；And/or
In step s3, the time of the precipitation is 1.5~4h.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109354338A (en) * | 2018-12-14 | 2019-02-19 | 科盛环保科技股份有限公司 | A kind of device and method of advanced treating Lonster production waste water |
| CN109354295A (en) * | 2018-10-22 | 2019-02-19 | 陈先锐 | Utilize the method for antibiotic in light electrolysis-ozone cooperative degrading cultivation field waste water |
| CN112456746A (en) * | 2020-10-13 | 2021-03-09 | 同济大学 | Catalytic wet oxidation treatment method for antibiotic pharmaceutical sludge |
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| CN105000734A (en) * | 2015-06-18 | 2015-10-28 | 四川珍福堂商贸有限公司 | Pharmaceutical wastewater treating system and method |
| CN105419383A (en) * | 2015-10-30 | 2016-03-23 | 浙江奇彩环境科技股份有限公司 | Improved dye synthesis process |
| CN207158999U (en) * | 2017-08-15 | 2018-03-30 | 广州市勃发环境科技有限公司 | Pharmacy wastewater treatment system |
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| CN103508637A (en) * | 2013-10-12 | 2014-01-15 | 江苏大学 | Traditional Chinese medicine wastewater treatment system and method for treating traditional Chinese medicine wastewater |
| CN105000734A (en) * | 2015-06-18 | 2015-10-28 | 四川珍福堂商贸有限公司 | Pharmaceutical wastewater treating system and method |
| CN105419383A (en) * | 2015-10-30 | 2016-03-23 | 浙江奇彩环境科技股份有限公司 | Improved dye synthesis process |
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| CN109354295A (en) * | 2018-10-22 | 2019-02-19 | 陈先锐 | Utilize the method for antibiotic in light electrolysis-ozone cooperative degrading cultivation field waste water |
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