CN114133097A - Treatment process of pharmaceutical intermediate production wastewater - Google Patents
Treatment process of pharmaceutical intermediate production wastewater Download PDFInfo
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- CN114133097A CN114133097A CN202111208614.5A CN202111208614A CN114133097A CN 114133097 A CN114133097 A CN 114133097A CN 202111208614 A CN202111208614 A CN 202111208614A CN 114133097 A CN114133097 A CN 114133097A
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F1/72—Treatment of water, waste water, or sewage by oxidation
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- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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- C02F2101/00—Nature of the contaminant
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- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
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- 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
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
Abstract
The invention is applicable to the field of sewage treatment of environmental engineering, and provides a treatment process of pharmaceutical intermediate production wastewater, which comprises the following operation steps: the wastewater is subjected to flow splitting treatment, so that the wastewater is divided into high-concentration wastewater and low-concentration wastewater, the high-concentration wastewater is treated by Fenton, and the tail end process is treated by an MBR membrane tank, so that the solid-liquid separation effect can be improved; according to the invention, through quality-divided flow distribution at the source of the wastewater, the construction cost and the operation cost can be saved through wastewater flow distribution, and the wastewater treatment effect can be improved; the biological toxicity is reduced and the B/C is improved by performing Fenton pretreatment on the high-concentration wastewater, so that the subsequent biochemical treatment capacity is greatly improved; the MBR membrane tank is used for replacing a sedimentation tank in the tail end process, so that the solid-liquid separation effect can be improved, the sludge age is increased, the degradation efficiency of the refractory organic matters is improved, and the area and the civil engineering cost are saved; the problems of high cost and low efficiency in the prior art are solved.
Description
Technical Field
The invention belongs to the field of environmental engineering sewage treatment, and particularly relates to a treatment process of medical intermediate production wastewater.
Background
The pharmaceutical industry is an important link in economic development, and not only influences the economic development level, but also influences the daily life and health level of human beings. In human life, different medicines are needed to deal with different diseases, so that various medicines need to be produced, and the production of medical intermediates is an essential link in medicine production, which means that various medical intermediates need to be produced. Various kinds of waste water can be generated along with the production of the medical intermediate, compared with common waste water, the production waste water of the medical intermediate has complex components, high COD concentration, high salinity and the like, has biotoxicity and is difficult to treat by common biochemistry. If the emissions are not treated, they can have adverse effects on the environment and human survival. The direct biochemical treatment has high civil engineering cost and high operating cost; the wastewater produced by the medical intermediate has biological toxicity, and the treatment efficiency of direct biochemical treatment is low. The technical problem to be solved by the invention is to solve the defects of the prior art and provide a stable and efficient treatment process for the production wastewater of the medical intermediate.
Disclosure of Invention
The embodiment of the invention aims to provide a treatment process of pharmaceutical intermediate production wastewater, so as to solve the problems in the background technology.
In order to achieve the above object, an embodiment of the present invention provides a process for treating wastewater from pharmaceutical intermediate production, comprising the following steps:
carrying out flow dividing treatment on the wastewater to enable the wastewater to be divided into high-concentration wastewater and low-concentration wastewater;
enabling the high-concentration wastewater to flow into a high-concentration wastewater tank and then flow into an oxidation tank, adding acid and Fenton into the oxidation tank for treatment, and enabling the effluent of the oxidation tank to flow into a first coagulation sedimentation tank;
adding alkali, a flocculating agent and a coagulant aid into a first coagulating sedimentation tank for reaction, and enabling supernatant in the first coagulating sedimentation tank to automatically flow into a comprehensive wastewater adjusting tank to be mixed with the low-concentration wastewater to obtain mixed wastewater;
making the mixed wastewater flow into a second coagulation sedimentation tank, and adding alkali, a flocculating agent and a coagulant aid for reaction; the water discharged from the second coagulation sedimentation tank enters a biochemical treatment system; the waste water is discharged after being treated by the biochemical treatment system;
after the water in the second coagulation sedimentation tank is discharged, the water firstly enters a hydrolysis tank in the biochemical treatment system; the effluent of the hydrolysis tank automatically flows into the facultative tank, the facultative bacteria in the facultative tank react, the effluent of the facultative tank automatically flows into the aerobic tank, the aerobic bacteria in the aerobic tank carry out degradation reaction, the effluent in the aerobic tank flows into the MBR membrane tank, and the sludge-water separation and the standard-reaching discharge of sewage are realized by entering the MBR membrane tank.
As a further scheme of the invention: part of sludge in the MBR membrane tank flows back to the hydrolysis tank, the sludge concentration of the hydrolysis tank and the facultative tank is maintained, part of returned sludge is decomposed again in the hydrolysis tank, and nitrate nitrogen in the returned sludge is denitrified into nitrogen in the facultative tank and discharged;
the sludge of the first coagulation sedimentation tank and the sludge of the second coagulation sedimentation tank and the residual sludge in the MBR membrane tank are discharged to the sludge tank together, and after sludge concentration, the sludge flows into the sludge dewatering machine for dewatering, so that the water content reaches 60%, the dry sludge is safely treated, the filtrate returns to the comprehensive wastewater adjusting tank, and the wastewater is discharged after reaching the standard.
As a further scheme of the invention: the high-concentration wastewater is refractory high-concentration wastewater, and the low-concentration wastewater is water flush pump wastewater, ground and equipment cleaning wastewater, maintenance wastewater, waste gas spraying wastewater, cooling wastewater, domestic sewage, initial rainwater and pure water preparation wastewater.
As a further scheme of the invention: the flocculating agent is one of aluminum sulfate, polysilicate iron and poly-phosphorus aluminum chloride.
As a further scheme of the invention: the coagulant aid is one of activated silicic acid, sodium alginate and polyacrylamide.
As a further scheme of the invention: the facultative bacteria are saccharomycetes.
As a further scheme of the invention: the aerobic strain is one or more of bacillus subtilis, bacillus licheniformis, lactic acid bacteria and acetic acid bacteria.
In summary, due to the adoption of the technical scheme, the method has the following beneficial effects:
the embodiment of the invention provides a treatment process of medical intermediate production wastewater, which can save construction cost and operation cost and improve wastewater treatment effect by dividing the wastewater according to the quality and the flow at the source of the wastewater; the biological toxicity is reduced and the B/C is improved by performing Fenton pretreatment on the high-concentration wastewater, so that the subsequent biochemical treatment capacity is greatly improved; the MBR membrane tank is used for replacing a sedimentation tank in the tail end process, so that the solid-liquid separation effect can be improved, the sludge age is increased, the degradation efficiency of the refractory organic matters is improved, and the area and the civil engineering cost are saved.
Description of the drawings:
FIG. 1 is a process flow diagram of an embodiment of the present invention.
Detailed Description
The present invention will be further described with reference to specific examples.
Example 1
The Zhejiang pharmaceutical industry Co Ltd is mainly used for producing medical intermediates, and has a plurality of product production lines, wherein the main products are enalapril, lisinopril, sitagliptin intermediates, rivaroxaban intermediates and the like, and the high-concentration process wastewater is produced by 50 t/d; the total amount of water used for washing the waste water of the water flush pump, the waste water of ground and equipment cleaning, the waste water of maintenance, the waste gas spraying waste water, the cooling waste water, the domestic sewage, the initial rainwater and the waste water of pure water preparation is 300 tons. Wherein the COD, BOD5, ammonia nitrogen and toluene concentration of the high-concentration wastewater are 63500mg/L, 25600mg/L, 153mg/L and 24.7 mg/L; the concentrations of COD, BOD5, ammonia nitrogen and toluene in the low-concentration wastewater are 2330mg/L, 1100mg/L, 28mg/L and 4.2 mg/L.
Please refer to, 100t of refractory high-concentration wastewater generated by each workshop process is collected to a high-concentration regulating tank, the wastewater in the high-concentration regulating tank is lifted to an oxidation tank by a pump, acid and fenton are added for reaction, the addition amount of the fenton is 0.3% of the weight of the wastewater, the B/C value of the wastewater is improved by damaging complex organic matters, and the effluent of the oxidation tank automatically flows into a first coagulation sedimentation tank; adding alkali, a flocculating agent and a coagulant aid into a first coagulation sedimentation tank, wherein the flocculating agent is aluminum sulfate; the coagulant aid is activated silicic acid, and the addition amounts of the flocculant and the coagulant aid are 0.05 percent and 0.01 percent of the mass of the wastewater; a large amount of alum floc is generated, part of organic matters are removed by adsorption so as to remove SS and insoluble organic matters, and supernatant fluid automatically flows into a comprehensive wastewater adjusting tank to be mixed with low-concentration wastewater. Pumping the wastewater in the tank into a second coagulation sedimentation tank, generating a large amount of alum floc by adjusting the pH and adding a flocculating agent and a coagulant aid, wherein the adding amount of the flocculating agent and the coagulant aid is 0.05 percent and 0.01 percent of the mass of the wastewater, and adsorbing and settling to remove partial organic matters; and the effluent of the second coagulation sedimentation tank enters a biochemical treatment system. Effluent enters a hydrolysis tank firstly, part of COD is removed through anaerobic hydrolysis, macromolecular pollutants are degraded into micromolecular pollutants, and the B/C ratio of the wastewater is improved. The effluent of the hydrolysis tank automatically flows into a facultative tank, part of COD is removed through facultative bacteria, denitrification is carried out, the effluent automatically flows into an aerobic tank, pollutants are thoroughly oxidized and degraded through aerobic bacteria, and the facultative bacteria are saccharomycetes. The aerobic strain is a mixture of bacillus subtilis and bacillus licheniformis, the effective viable count of the bacillus subtilis powder and the bacillus licheniformis powder is not less than 2.0 multiplied by 1010cfu/g, and the addition amount of the bacillus subtilis powder and the bacillus licheniformis powder is 0.02 percent of the mass of the wastewater; the sludge-water separation is realized by the MBR membrane in the MBR membrane tank at the tail end, the MBR membrane can effectively intercept strains in the reactor, the higher sludge concentration is kept, the sludge load is reduced, and the removal efficiency is improved. And part of sludge in the MBR membrane tank flows back to the hydrolysis tank, so that the sludge concentration of the hydrolysis tank and the facultative tank can be maintained, part of returned sludge is decomposed in the hydrolysis tank, and nitrate nitrogen in the returned sludge is denitrified into nitrogen in the facultative tank to be discharged out of the system. And (3) discharging the sludge in the first coagulation sedimentation tank and the second coagulation sedimentation tank and excess sludge to a sludge tank, concentrating the sludge, pumping the sludge into a sludge dewatering machine for dewatering, treating the dry sludge safely, and returning the filtrate to the comprehensive wastewater regulating tank.
After Fenton treatment, the removal rates of COD, BOD5, ammonia nitrogen and toluene are respectively 34.74%, 19.78%, 4.58% and 84.37%, and the B/C ratio is 0.5 higher than that of 0.40. After the comprehensive wastewater is treated by A/A/O + MBR, the concentrations of COD, BOD5, ammonia nitrogen and toluene in the effluent are 285mg/L, 75mg/L, 12.6mg/L and 0.37 mg/L; the removal rates were 96.40%, 98.07%, 72.25% and 91.02%, respectively.
Example 2
Collecting 100t of high-concentration wastewater which is difficult to degrade and is generated by each workshop process into a high-concentration regulating tank, lifting the wastewater in the high-concentration regulating tank to an oxidation tank by using a pump, adding acid for regulation, and removing partial organic matters by Fenton oxidation, wherein the addition amount of Fenton is 0.3% of the weight of the wastewater, the B/C value of the wastewater is improved by damaging complex organic matters, and the effluent of the oxidation tank automatically flows into a first coagulating sedimentation tank; adding a flocculating agent and a coagulant aid into the first coagulation sedimentation tank, wherein the flocculating agent is aluminum sulfate; the coagulant aid is activated silicic acid, and the addition amounts of the flocculant and the coagulant aid are 0.05 percent and 0.01 percent of the mass of the wastewater; a large amount of alum floc is generated, part of organic matters are removed by adsorption so as to remove SS and insoluble organic matters, and supernatant fluid automatically flows into a comprehensive wastewater adjusting tank to be mixed with low-concentration wastewater. Pumping the wastewater in the tank into a second coagulation sedimentation tank, generating a large amount of alum floc by adjusting the pH and adding a flocculating agent and a coagulant aid, wherein the adding amount of the flocculating agent and the coagulant aid is 0.05 percent and 0.01 percent of the mass of the wastewater, and adsorbing and settling to remove partial organic matters; and the effluent of the second coagulation sedimentation tank enters a biochemical treatment system. Effluent enters a hydrolysis tank firstly, part of COD is removed through anaerobic hydrolysis, macromolecular pollutants are degraded into micromolecular pollutants, and the B/C ratio of the wastewater is improved. The effluent of the hydrolysis tank automatically flows into a facultative tank, part of COD is removed through facultative bacteria, denitrification is carried out, the effluent automatically flows into an aerobic tank, pollutants are thoroughly oxidized and degraded through aerobic bacteria, and the facultative bacteria are saccharomycetes. The aerobic strain is bacillus subtilis, the effective viable count of bacillus subtilis powder is not less than 2.0 multiplied by 1010cfu/g, and the addition amount of the bacillus subtilis powder is 0.02 percent of the mass of the wastewater; the sludge-water separation is realized by the MBR membrane in the MBR membrane tank at the tail end, the MBR membrane can effectively intercept strains in the reactor, the higher sludge concentration is kept, the sludge load is reduced, and the removal efficiency is improved. And part of sludge in the MBR membrane tank flows back to the hydrolysis tank, so that the sludge concentration of the hydrolysis tank and the facultative tank can be maintained, part of returned sludge is decomposed in the hydrolysis tank, and nitrate nitrogen in the returned sludge is denitrified into nitrogen in the facultative tank to be discharged out of the system. And (3) discharging the sludge in the first coagulation sedimentation tank and the second coagulation sedimentation tank and excess sludge to a sludge tank, concentrating the sludge, pumping the sludge into a sludge dewatering machine for dewatering, treating the dry sludge safely, and returning the filtrate to the comprehensive wastewater regulating tank.
In summary, the following steps: according to the invention, through quality-divided flow distribution at the source of the wastewater, the construction cost and the operation cost can be saved through wastewater flow distribution, and the wastewater treatment effect can be improved; the biological toxicity is reduced and the B/C is improved by performing Fenton pretreatment on the high-concentration wastewater, so that the subsequent biochemical treatment capacity is greatly improved; the MBR membrane tank is used for replacing a sedimentation tank in the tail end process, so that the solid-liquid separation effect can be improved, the sludge age is increased, the degradation efficiency of the refractory organic matters is improved, and the area and the civil engineering cost are saved.
Claims (7)
1. A treatment process of medical intermediate production wastewater is characterized by comprising the following operation steps:
carrying out flow dividing treatment on the wastewater to enable the wastewater to be divided into high-concentration wastewater and low-concentration wastewater;
enabling the high-concentration wastewater to flow into a high-concentration wastewater tank and then flow into an oxidation tank, adding acid and Fenton into the oxidation tank for treatment, and enabling the effluent of the oxidation tank to flow into a first coagulation sedimentation tank;
adding alkali, a flocculating agent and a coagulant aid into a first coagulating sedimentation tank for reaction, and enabling supernatant in the first coagulating sedimentation tank to automatically flow into a comprehensive wastewater adjusting tank to be mixed with the low-concentration wastewater to obtain mixed wastewater;
making the mixed wastewater flow into a second coagulation sedimentation tank, and adding alkali, a flocculating agent and a coagulant aid for reaction; the water discharged from the second coagulation sedimentation tank enters a biochemical treatment system; the waste water is discharged after being treated by the biochemical treatment system;
after the water in the second coagulation sedimentation tank is discharged, the water firstly enters a hydrolysis tank in the biochemical treatment system; the effluent of the hydrolysis tank automatically flows into the facultative tank, the facultative bacteria in the facultative tank react, the effluent of the facultative tank automatically flows into the aerobic tank, the aerobic bacteria in the aerobic tank carry out degradation reaction, the effluent in the aerobic tank flows into the MBR membrane tank, and the sludge-water separation and the standard-reaching discharge of sewage are realized by entering the MBR membrane tank.
2. The process for treating wastewater from the production of pharmaceutical intermediates according to claim 1,
part of sludge in the MBR membrane tank flows back to the hydrolysis tank, the sludge concentration of the hydrolysis tank and the facultative tank is maintained, part of returned sludge is decomposed again in the hydrolysis tank, and nitrate nitrogen in the returned sludge is denitrified into nitrogen in the facultative tank and discharged;
the sludge of the first coagulation sedimentation tank and the sludge of the second coagulation sedimentation tank and the residual sludge in the MBR membrane tank are discharged to the sludge tank together, and after sludge concentration, the sludge flows into the sludge dewatering machine for dewatering, so that the water content reaches 60%, the dry sludge is safely treated, the filtrate returns to the comprehensive wastewater adjusting tank, and the wastewater is discharged after reaching the standard.
3. The process according to claim 1, wherein the high concentration wastewater is a refractory high concentration wastewater, and the low concentration wastewater is water flush pump wastewater, ground and equipment cleaning wastewater, maintenance wastewater, waste gas spray wastewater, cooling wastewater, domestic sewage, initial rainwater, and pure water preparation wastewater.
4. The process according to claim 1, wherein the flocculating agent is one of aluminum sulfate, polysilicate iron, and poly aluminum phosphate chloride.
5. The process for treating wastewater from the production of pharmaceutical intermediates according to claim 1, wherein the coagulant aid is one of activated silicic acid, sodium alginate and polyacrylamide.
6. The process for treating wastewater from the production of pharmaceutical intermediates according to claim 1, wherein said facultative aerobe is yeast.
7. The process for treating wastewater from the production of pharmaceutical intermediates according to any of claims 1 to 6, wherein said aerobic bacterial species is one or more of Bacillus subtilis, Bacillus licheniformis, lactic acid bacteria, and acetic acid bacteria.
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| CN115259540A (en) * | 2022-05-17 | 2022-11-01 | 景德镇澳蓝亚特环境科技有限公司 | Treatment method of respiratory targeting drug wastewater |
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| CN115259540A (en) * | 2022-05-17 | 2022-11-01 | 景德镇澳蓝亚特环境科技有限公司 | Treatment method of respiratory targeting drug wastewater |
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