CN112479484A - Pharmaceutical adjuvant production wastewater treatment process - Google Patents
Pharmaceutical adjuvant production wastewater treatment process Download PDFInfo
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- CN112479484A CN112479484A CN202011207541.3A CN202011207541A CN112479484A CN 112479484 A CN112479484 A CN 112479484A CN 202011207541 A CN202011207541 A CN 202011207541A CN 112479484 A CN112479484 A CN 112479484A
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- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000000546 pharmaceutical excipient Substances 0.000 title claims abstract description 25
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 11
- 239000002351 wastewater Substances 0.000 claims abstract description 57
- 230000003647 oxidation Effects 0.000 claims abstract description 49
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 49
- 238000004062 sedimentation Methods 0.000 claims abstract description 31
- 230000001112 coagulating effect Effects 0.000 claims abstract description 21
- 229940124531 pharmaceutical excipient Drugs 0.000 claims abstract description 13
- 230000003301 hydrolyzing effect Effects 0.000 claims abstract description 10
- 239000010865 sewage Substances 0.000 claims description 28
- 239000010802 sludge Substances 0.000 claims description 20
- 230000015271 coagulation Effects 0.000 claims description 18
- 238000005345 coagulation Methods 0.000 claims description 18
- 230000020477 pH reduction Effects 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000005868 electrolysis reaction Methods 0.000 claims description 12
- 230000007062 hydrolysis Effects 0.000 claims description 9
- 238000006460 hydrolysis reaction Methods 0.000 claims description 9
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 9
- 238000001556 precipitation Methods 0.000 claims description 8
- 239000000701 coagulant Substances 0.000 claims description 6
- 239000000084 colloidal system Substances 0.000 claims description 6
- 239000000470 constituent Substances 0.000 claims description 6
- 230000003311 flocculating effect Effects 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 4
- 238000003860 storage Methods 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 239000003513 alkali Substances 0.000 claims description 3
- 230000015556 catabolic process Effects 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 238000006731 degradation reaction Methods 0.000 claims description 3
- 238000000855 fermentation Methods 0.000 claims description 3
- 230000004151 fermentation Effects 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 244000005700 microbiome Species 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 5
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract 1
- 229910052799 carbon Inorganic materials 0.000 abstract 1
- 229910052742 iron Inorganic materials 0.000 abstract 1
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 9
- 239000000706 filtrate Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012065 filter cake Substances 0.000 description 2
- 239000000825 pharmaceutical preparation Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000011701 zinc Substances 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- 208000005156 Dehydration Diseases 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- UOURRHZRLGCVDA-UHFFFAOYSA-D pentazinc;dicarbonate;hexahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Zn+2].[Zn+2].[Zn+2].[Zn+2].[Zn+2].[O-]C([O-])=O.[O-]C([O-])=O UOURRHZRLGCVDA-UHFFFAOYSA-D 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
-
- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- 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
-
- 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
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention relates to the technical field of pharmaceutical excipient production wastewater, in particular to a pharmaceutical excipient production wastewater treatment process, which is used for solving the problems that pollutants in wastewater are difficult to effectively treat and secondary pollution is easily caused when high-concentration pharmaceutical excipient production wastewater is treated in the prior art. The invention comprises the following steps: step 1: removing floating objects; step 2: air floatation; and step 3: adjusting the pH value; and 4, step 4: electrolyzing iron and carbon; and 5: performing primary Fenton oxidation; step 6: primary coagulating sedimentation; and 7: hydrolyzing and acidifying; and 8: biological contact oxidation; and step 9: secondary Fenton oxidation; step 10: and (5) performing secondary coagulating sedimentation. Through the treatment process, various indexes of treated effluent can meet the discharge standard, so that harmful substances in high-concentration pharmaceutical adjuvant production wastewater can be more effectively removed, and secondary pollution can be reduced.
Description
Technical Field
The invention relates to the technical field of pharmaceutical excipient production wastewater, and particularly relates to a pharmaceutical excipient production wastewater treatment process.
Background
The pharmaceutic adjuvant is a basic material and an important component of the pharmaceutical preparation and is a material basis for ensuring the production and development of the pharmaceutical preparation. At present, more than 500 pharmaceutical excipients are proposed in China, and because the products are multiple, the production process is diversified, the components of the produced wastewater are more complex, and the wastewater has the characteristics of high concentration, high salinity, difficult biodegradation and the like, so that the wastewater is one of the industrial wastewater which is difficult to treat, and the wastewater produced by the pharmaceutical excipients needs a corresponding wastewater treatment process for better treatment.
The wastewater treatment process in the prior art adopts a pulse filler extraction tower, wastewater of a sartan drug quenching process is taken as a light phase and pumped into the tower from the bottom of the tower, an extracting agent is taken as a heavy phase and pumped into the tower from the top of the tower, continuous extraction is carried out under the conditions that the volume flow ratio of the heavy phase to the light phase is 1:1 and the pulse frequency is 40-100 times/min, the extracted light phase is collected from the top of the tower respectively, and the extracted heavy phase is collected from the bottom of the tower; rectifying the extracted heavy phase to recover the extractant and dimethyl formamide (DMF), wherein the recovery rate of the extractant and the dimethyl formamide is more than 98.0%, the purity is more than 99.0%, and the heavy phase is recycled; adjusting the pH of the extracted light phase to 6-7, decoloring and removing impurities, adding a sodium carbonate aqueous solution, stirring and reacting at 40-70 ℃ for 0.5-3h to remove zinc, filtering at normal temperature to obtain filtrate and filter cake, and drying the filter cake to obtain a basic zinc carbonate byproduct; the zinc value of the filtrate is less than 1mg/L, and the filtrate can be directly merged into a factory sewage system for treatment.
However, in the prior art, the process for treating wastewater from pharmaceutical adjuvant production is difficult to effectively treat the pollutants in the wastewater when treating high-concentration wastewater, and is easy to cause secondary pollution. Therefore, a process for treating wastewater from pharmaceutical adjuvant production, which can effectively remove harmful substances from high-concentration wastewater and reduce secondary pollution, is urgently needed.
Disclosure of Invention
Based on the above problems, the present invention aims to: the utility model provides a pharmaceutical excipients waste water treatment process for solve among the prior art when handling high concentration pharmaceutical excipients waste water effectively handle the pollutant material in the sewage, cause secondary pollution's problem moreover easily. According to the invention, by adopting the treatment process of air floatation, iron carbon electrolysis, primary Fenton oxidation, primary coagulation precipitation, hydrolytic acidification, biological contact oxidation, secondary Fenton oxidation and secondary coagulation precipitation, all indexes of treated effluent can meet the discharge standard, so that harmful substances in high-concentration pharmaceutical adjuvant production wastewater can be more effectively removed, and secondary pollution can be reduced.
The invention specifically adopts the following technical scheme for realizing the purpose:
a process for treating wastewater generated in pharmaceutical adjuvant production comprises the following steps:
step 1: removing floating objects, intercepting the floating objects in the sewage through a grating channel, and periodically cleaning;
step 2: air floatation, namely floating suspended particles in the wastewater on the water surface by utilizing the buoyancy principle through an air floatation machine and removing the suspended particles;
and step 3: adjusting the pH, namely adding acid or alkali into a pH adjusting tank to adjust the pH in the sewage;
and 4, step 4: iron-carbon electrolysis, namely lifting the sewage with the adjusted pH value to an iron-carbon electrolysis reactor through a pump for electrolysis;
and 5: carrying out primary Fenton oxidation, and conveying the electrolyzed sewage into a Fenton oxidation reactor for oxidation treatment;
step 6: primary coagulating sedimentation, namely conveying the wastewater after the primary Fenton oxidation to a primary coagulating sedimentation tank, adding a coagulant and a coagulant aid into the wastewater to ensure that particles which are difficult to precipitate in the wastewater can be mutually polymerized to form colloid, then combining the colloid with impurities in the wastewater to form a flocculating constituent, and removing the flocculating constituent;
and 7: carrying out hydrolytic acidification, conveying the sewage subjected to primary coagulation precipitation into a hydrolytic acidification tank, converting non-soluble organic matters in the sewage into soluble organic matters through hydrolysis, and carrying out fermentation degradation treatment on the soluble organic matters through acidification;
and 8: biological contact oxidation, namely conveying the sewage subjected to hydrolysis and acidification in the step 7 into a biological contact oxidation tank, adsorbing organic matters in the wastewater through a biological membrane, and oxidizing and decomposing the organic matters by microorganisms under the aerobic condition;
and step 9: carrying out secondary Fenton oxidation, namely conveying the sewage subjected to biological contact oxidation into a secondary Fenton oxidation reactor for secondary Fenton oxidation treatment;
step 10: and (4) secondary coagulating sedimentation, namely conveying the wastewater after the secondary Fenton oxidation to a secondary coagulating sedimentation tank, and performing secondary coagulating sedimentation treatment to obtain clear water reaching the standard.
Still be equipped with middle pond between first coagulating sedimentation pond and hydrolysis-acidification pool, low concentration waste water is directly carried the hydrolysis-acidification in the pond through middle pond and is carried out hydrolysis-acidification.
And (3) conveying the sludge subjected to primary coagulation sedimentation and secondary coagulation sedimentation into a sludge storage tank for sludge dewatering treatment, discharging the dewatered dry sludge, and feeding the dewatered water into the step 2 again.
The discharge standard of the clear water discharged in the step 10 is as follows: COD less than or equal to 300mg/L, BOD5≤150mg/L，NH3-N≤30mg/L，SS≤150mg/L。
The invention has the following beneficial effects:
(1) by adopting the treatment process of air flotation, iron carbon electrolysis, primary Fenton oxidation, primary coagulation precipitation, hydrolytic acidification, biological contact oxidation, secondary Fenton oxidation and secondary coagulation precipitation, all indexes of treated effluent can meet the discharge standard, so that harmful substances in high-concentration pharmaceutical adjuvant production wastewater can be more effectively removed, and the process is mature and reliable, stable in operation, easy to operate, capable of reducing secondary pollution and simultaneously reducing pollution of sewage to the ecological environment.
(2) The invention starts to process from step 1 if the wastewater is high-concentration wastewater, and starts to process from step 7 if the wastewater is low-concentration wastewater, so that the targeted processing can reduce the processing cost of the wastewater.
(3) In the invention, the sludge after primary coagulation sedimentation and secondary coagulation sedimentation is conveyed to the sludge storage tank for sludge dehydration treatment, the dehydrated dry sludge is discharged, and the dehydrated water enters the step 2 again, so that the sludge can be effectively utilized, and the water resource in the sludge can be utilized again, thereby greatly saving water resource and soil resource.
Drawings
FIG. 1 is a process flow diagram of the wastewater treatment of pharmaceutical adjuvant production according to the present invention;
Detailed Description
For a better understanding of the present invention by those skilled in the art, the present invention will be described in further detail below with reference to the accompanying drawings and the following examples.
Example (b):
as shown in figure 1, the process for treating the pharmaceutical excipient production wastewater comprises the following steps:
step 1: removing floating objects, intercepting the floating objects in the sewage through a grating channel, and periodically cleaning; the grid channel can be provided with a steel-concrete structure, and the size of the grid channel is 2.0 mx0.5mx1.5m;
step 2: air floatation, namely floating suspended particles in the wastewater on the water surface by utilizing the buoyancy principle through an air floatation machine and removing the suspended particles; an air floatation machine is arranged, and the processing capacity of the air floatation machine is 5m3H, size 1.5mx1.8 m;
and step 3: adjusting the pH, namely adding acid or alkali into a pH adjusting tank to adjust the pH in the sewage; a PH adjusting tank is arranged, and the effective volume of the PH adjusting tank is 5.6m3A size of 1.5 mx1.5mx3m;
and 4, step 4: iron-carbon electrolysis, namely lifting the sewage with the adjusted pH value to an iron-carbon electrolysis reactor through a pump for electrolysis; 2 pumps can be arranged, 1 pump is used for standby, the lift of the pump is 20m, and the power is 0.55 KW;
and 5: carrying out primary Fenton oxidation, and conveying the electrolyzed sewage into a Fenton oxidation reactor for oxidation treatment; arranging a Fenton oxidation reactor;
step 6: primary coagulating sedimentation, namely conveying the wastewater after the primary Fenton oxidation to a primary coagulating sedimentation tank, adding a coagulant and a coagulant aid into the wastewater to ensure that particles which are difficult to precipitate in the wastewater can be mutually polymerized to form colloid, then combining the colloid with impurities in the wastewater to form a flocculating constituent, and removing the flocculating constituent; the primary coagulation sedimentation tank is of a steel-concrete structure, and the size of the primary coagulation sedimentation tank is 2.2 mx2.2mx4m;
and 7: hydrolyzing and acidifying, namely conveying the sewage subjected to primary coagulating sedimentation into a hydrolyzing and acidifying tank, and converting non-soluble organic matters in the sewage into non-soluble organic matters through hydrolysisPerforming fermentation degradation treatment on soluble organic matters through acidification; the effective volume of the hydrolysis acidification tank is 347.2m3And has a size of 8 mx7mx6.5m;
and 8: biological contact oxidation, namely conveying the sewage subjected to hydrolysis and acidification in the step 7 into a biological contact oxidation tank, adsorbing organic matters in the wastewater through a biological membrane, and oxidizing and decomposing the organic matters by microorganisms under the aerobic condition; the biological contact oxidation pond is of a steel-concrete structure, the size of the biological contact oxidation pond can be 10mx5mx5.5m, and the effective volume of the biological contact oxidation pond is 250m3The retention time is 60 hours;
and step 9: carrying out secondary Fenton oxidation, namely conveying the sewage subjected to biological contact oxidation into a secondary Fenton oxidation reactor for secondary Fenton oxidation treatment;
step 10: and (4) secondary coagulating sedimentation, namely conveying the wastewater after the secondary Fenton oxidation to a secondary coagulating sedimentation tank, and performing secondary coagulating sedimentation treatment to obtain clear water reaching the standard. The discharge standard of the discharged clear water is as follows: COD less than or equal to 300mg/L, BOD5≤150mg/L，NH3-N≤30mg/L，SS≤150mg/L。
Preferably, still be equipped with middle pond between initial coagulating sedimentation pond and hydrolysis acidification pond, low concentration waste water is directly carried the hydrolysis acidification pond through middle pond and is carried out the hydrolysis acidification in. If the wastewater is high-concentration wastewater, the treatment is started from the step 1, and if the wastewater is low-concentration wastewater, the treatment is started from the step 7, so that the targeted treatment can be realized, and the treatment cost of the wastewater can be reduced.
Preferably, the sludge after the primary coagulation sedimentation and the secondary coagulation sedimentation is conveyed to a sludge storage tank for sludge dewatering treatment, the dewatered dry sludge is discharged, and the dewatered water enters the step 2 again. Therefore, the sludge can be effectively utilized, and water resources in the sludge can be reused, so that a large amount of water resources and soil resources can be saved.
The treatment effect of the wastewater treated by the process flow is as follows:
according to the above table and the actual treatment conditions, by adopting the treatment process of air floatation, iron carbon electrolysis, primary Fenton oxidation, primary coagulation precipitation, hydrolytic acidification, biological contact oxidation, secondary Fenton oxidation and secondary coagulation precipitation, all indexes of the treated effluent can meet the discharge standard, so that harmful substances in the high-concentration pharmaceutical adjuvant production wastewater can be more effectively removed, and the process is mature and reliable, stable in operation, easy to operate, capable of reducing secondary pollution and simultaneously reducing pollution of sewage to the ecological environment.
The above is an embodiment of the present invention. The embodiments and specific parameters in the embodiments are only for the purpose of clearly illustrating the verification process of the invention and are not intended to limit the scope of the invention, which is defined by the claims, and all equivalent structural changes made by using the contents of the specification and the drawings of the present invention should be covered by the scope of the present invention.
Claims (4)
1. A process for treating wastewater generated in pharmaceutical adjuvant production is characterized by comprising the following steps: the method comprises the following steps:
step 1: removing floating objects, intercepting the floating objects in the sewage through a grating channel, and periodically cleaning;
step 2: air floatation, namely floating suspended particles in the wastewater on the water surface by utilizing the buoyancy principle through an air floatation machine and removing the suspended particles;
and step 3: adjusting the pH, namely adding acid or alkali into a pH adjusting tank to adjust the pH in the sewage;
and 4, step 4: iron-carbon electrolysis, namely lifting the sewage with the adjusted pH value to an iron-carbon electrolysis reactor through a pump for electrolysis;
and 5: carrying out primary Fenton oxidation, and conveying the electrolyzed sewage into a Fenton oxidation reactor for oxidation treatment;
step 6: primary coagulating sedimentation, namely conveying the wastewater after the primary Fenton oxidation to a primary coagulating sedimentation tank, adding a coagulant and a coagulant aid into the wastewater to ensure that particles which are difficult to precipitate in the wastewater can be mutually polymerized to form colloid, then combining the colloid with impurities in the wastewater to form a flocculating constituent, and removing the flocculating constituent;
and 7: carrying out hydrolytic acidification, conveying the sewage subjected to primary coagulation precipitation into a hydrolytic acidification tank, converting non-soluble organic matters in the sewage into soluble organic matters through hydrolysis, and carrying out fermentation degradation treatment on the soluble organic matters through acidification;
and 8: biological contact oxidation, namely conveying the sewage subjected to hydrolysis and acidification in the step 7 into a biological contact oxidation tank, adsorbing organic matters in the wastewater through a biological membrane, and oxidizing and decomposing the organic matters by microorganisms under the aerobic condition;
and step 9: carrying out secondary Fenton oxidation, namely conveying the sewage subjected to biological contact oxidation into a secondary Fenton oxidation reactor for secondary Fenton oxidation treatment;
step 10: and (4) secondary coagulating sedimentation, namely conveying the wastewater after the secondary Fenton oxidation to a secondary coagulating sedimentation tank, and performing secondary coagulating sedimentation treatment to obtain clear water reaching the standard.
2. The pharmaceutical excipient production wastewater treatment process according to claim 1, which is characterized in that: still be equipped with middle pond between first coagulating sedimentation pond and hydrolysis-acidification pool, low concentration waste water is directly carried the hydrolysis-acidification in the pond through middle pond and is carried out hydrolysis-acidification.
3. The pharmaceutical excipient production wastewater treatment process according to claim 1, which is characterized in that: and (3) conveying the sludge subjected to primary coagulation sedimentation and secondary coagulation sedimentation into a sludge storage tank for sludge dewatering treatment, discharging the dewatered dry sludge, and feeding the dewatered water into the step 2 again.
4. The pharmaceutical excipient production wastewater treatment process according to claim 1, which is characterized in that: the discharge standard of the clear water discharged in the step 10 is as follows: COD less than or equal to 300mg/L, BOD5≤150mg/L，NH3-N≤30mg/L，SS≤150mg/L。
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|---|---|---|---|---|
| US20130206692A1 (en) * | 2010-10-28 | 2013-08-15 | Shiwen Zhang | Tanning wastewater treatment and recycling method based on nano-catalytic electrolysis technology and membrane technology |
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| CN104649512A (en) * | 2014-12-23 | 2015-05-27 | 安徽省天虹绿洲环保科技有限公司 | High-concentration medicinal adjuvant wastewater treatment process |
| CN208995338U (en) * | 2018-09-25 | 2019-06-18 | 成都渤茂科技有限公司 | A kind of processing system of oilfield drilling waste liquid |
| CN111153565A (en) * | 2020-02-26 | 2020-05-15 | 广东广深环保科技有限公司 | Treatment system and treatment method for esterification wastewater |
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- 2020-11-03 CN CN202011207541.3A patent/CN112479484A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130206692A1 (en) * | 2010-10-28 | 2013-08-15 | Shiwen Zhang | Tanning wastewater treatment and recycling method based on nano-catalytic electrolysis technology and membrane technology |
| CN103739150A (en) * | 2013-11-15 | 2014-04-23 | 安徽省绿巨人环境技术有限公司 | Medicinal auxiliary material production wastewater treatment technology |
| CN104649512A (en) * | 2014-12-23 | 2015-05-27 | 安徽省天虹绿洲环保科技有限公司 | High-concentration medicinal adjuvant wastewater treatment process |
| CN208995338U (en) * | 2018-09-25 | 2019-06-18 | 成都渤茂科技有限公司 | A kind of processing system of oilfield drilling waste liquid |
| CN111153565A (en) * | 2020-02-26 | 2020-05-15 | 广东广深环保科技有限公司 | Treatment system and treatment method for esterification wastewater |
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Application publication date: 20210312 |