CN108455793A - A kind of processing method of cephalosporin antibiotic production waste water - Google Patents
A kind of processing method of cephalosporin antibiotic production waste water Download PDFInfo
- Publication number
- CN108455793A CN108455793A CN201810180806.1A CN201810180806A CN108455793A CN 108455793 A CN108455793 A CN 108455793A CN 201810180806 A CN201810180806 A CN 201810180806A CN 108455793 A CN108455793 A CN 108455793A
- Authority
- CN
- China
- Prior art keywords
- water
- processing method
- biochemical
- waste water
- production waste
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- 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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
-
- 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
Abstract
A kind of processing method of cephalosporin antibiotic production waste water, belongs to field of waste water treatment.The present invention uses the method that electrodialysis MVR evaporative crystallization A/O biochemical treatments are combined, and control its salt content by adjusting the conductivity for concentrating concentrated water and biochemical fresh water in electrodialytic process, so that the salt and water of raw water are sufficiently separated in electrodialysis plant, improve MVR evaporative crystallization efficiency, the harm to microorganism in biochemical system is reduced, the removal rate of organic matter and ammonia nitrogen is improved；Meanwhile adjusting its acid or alkali environment by the way that ammonium hydroxide is added into concentration concentrated water so that the pH into the concentration concentrated water of MVR is maintained at 6 ~ 8.5, hydrogen ion is avoided persistently to be enriched in MVR systems, the boiling point Wen Sheng for influencing the salt such as ammonium sulfate, enables MVR persistently to go out salt, extends the system stable operation time.
Description
Technical field
A kind of processing method of cephalosporin antibiotic production waste water, belongs to field of waste water treatment.
Background technology
Cephalosporin antibiotic production waste water is the organic pharmacy waste water of high-content of element of the first species's complexity, wherein including lipid, alcohol
A variety of hard-degraded substances such as class, fermentating metabolism product, mycelium and antibiotic residues, moreover, the also a large amount of sulphur of content in waste water
Sour ammonium increases its intractability.
Currently, the method for handling such waste water mainly has flocculent precipitation, Iron carbon reduction method, advanced oxidation processes, film point
From technology and bioanalysis, the above processing method has respective limitation, and in flocculent precipitation, flocculant removal rate is not high, closes
It is still the direction developed at present at efficient flocculant；Iron carbon filler is susceptible to hardened, electrolytic efficiency in Iron carbon reduction method
It reduces；Required oxidant content is big in advanced oxidation processes, and operating cost is high, and economy is the bottleneck of entire engineering, and generates chemistry
Sludge；Membrane separation technique is used only to the antibiotic organic matter of removal remaining, and control membrane fouling is difficult in engineering, cleaning performance
It is bad；Bioanalysis：As the guarantee of follow-up discharged wastewater met the national standard, before must pre-process the antibiotic of removal remaining and with high salt
Point.For the limitation of the above each method, concentration+evaporative crystallization+biochemical treatment group technology is also current popular height
Salinity wastewater treatment method, but complicated component and the higher pharmacy waste water of COD and ammonia-nitrogen content, processing system are easily occurred
Serious blocking and etching problem, moreover, in evaporation and crystal process, since boiling point temperature rises larger, crystalline rate reduction so that be
System continuous operating time is short, fluctuation of service is even unable to operate normally, moreover, the treatment effect of organic matter, ammonia nitrogen is not good enough.
Invention content
The technical problem to be solved by the present invention is to：It is useless to overcome the deficiencies of the prior art and provide a kind of cephalosporin antibiotic production
The processing method of water effectively improves the continuous operating time of system, enables a system to long-time steady operation, and be obviously improved
The treatment effect of organic matter and ammonia nitrogen.
The technical solution adopted by the present invention to solve the technical problems is：The cephalosporin antibiotic produces the processing method of waste water
Include the following steps：
1）Filtering：Raw water enters ultrafiltration apparatus after basket filter filters and carries out fine filtering, removes the suspended matter in raw water
With the organic matter of macromolecule；
2）Electrodialysis：Ultra-filtration water enters electrodialysis system, carries out continuous brine separation through two-stage electrodialysis, obtains concentration concentrated water
With biochemical fresh water, the conductance for concentrating concentrated water is more than 160ms/cm, and the conductance of biochemical fresh water is less than 6ms/cm；
3）Evaporative crystallization：Step 2）Described in concentrated water enter MVR systems and be evaporated and crystallize to obtain solid salt, and generate condensed water；
4）Biological treatment：Step 2）Middle fresh water and step 3）The condensed water of middle generation enters A/O biochemical systems, carries out anaerobism successively
Processing and Aerobic Process for Treatment remove large amount of organic and ammonia nitrogen；
Step 2）Ammonium hydroxide is added before entering MVR systems in gained concentrated water, and it is 6 ~ 9 to adjust its pH.
The sulfuric acid added in being produced due to cephalosporin antibiotic waster water process is excessive, so sulfate radical is excessive in raw water,
It is hot operation to form sulfuric acid-ammonium sulfate acidic buffer solution, pH value 3 ~ 4, and MVR systems, and sulfuric acid-ammonium sulfate enters
Ammonia radical ion part, which can decompose, in hot environment causes internal system pH value to further decrease, and sulfate radical is gradually rich in system
Collection.Under normal circumstances, the boiling point heating of pure ammonium sulfate is 9 DEG C, in practical operation, since sulfate radical enrichment and higher COD contain
Amount so that the boiling point heating of crystal solution increases, and higher boiling point heating influences the crystalline rate of ammonium sulfate so that MVR goes out salt amount
It reduces, or even does not go out salt, cause subsequent handling that can not run.Ammonium hydroxide is added before electrodialysis concentrated water enters MVR, adjusts its pH
It is 6 ~ 9, the boiling point heating decline of ammonium sulfate, evaporation efficiency improve in MVR evaporation and crystal processes, go out the increase of salt amount, MVR is lasting
Going out salt just can make electrodialysis concentrated water continue into MVR so that whole system normal operation.
The processing method of the cephalosporin antibiotic production waste water of the present invention includes mainly filtering, electrodialysis, evaporative crystallization and A/O
Biochemical processing process, the suspended matter and larger molecular organics of filter element acting as in removal raw water, waste water after filtering
Into electrodialysis cell, electrodialytic to act as carrying out brine separation, concentration concentrated water enters MVR and is evaporated crystallization, biochemical light
Water enters A/O units, and the conductance of electrodialysis cell control concentration concentrated water of the present invention is to be not only able to effectively carry more than 160ms/cm
The evaporative crystallization efficiency of high MVR units, and the amount that condensed water is generated in evaporation and crystal process can be reduced, reduce whole system
Heat consumption, and reduce the processing load of A/O units；The conductance of electrodialysis cell biochemistry fresh water of the present invention is less than 6ms/cm, contains
Salt amount is relatively low to be directly entered subsequent biochemical system, will not generate harm to sludge, helps to improve the processing effect of biochemical system
Rate.
Preferably, step 2）Ammonium hydroxide is added before entering MVR systems in gained concentrated water, and it is 7.5 ~ 8.5 to adjust its pH.
Preferably, step 2）Described in concentration concentrated water conductance be more than 180ms/cm, concentrate the higher explanation of conductance of concentrated water
Wherein salt content is higher, i.e., electrodialysis effect is better, and MVR crystallization effects are better.
Preferably, step 2）Described in the conductance of biochemical fresh water be less than 4ms/cm, the salt content of biochemical fresh water is smaller, right
The harm of microorganism is smaller in biochemical system, is conducive to the efficient removal to organic matter and ammonia nitrogen in biochemical system.
Preferably, step 4）Described in A/O biochemical systems return current ratio of the mixed liquid be the ponds A in 800 ~ 1100%, A/O techniques
It is mainly used for denitrogenation dephosphorizing for anaerobic pond, the ponds O are aerobic tank, are mainly used for organics removal, return current ratio of the mixed liquid directly affects
The removal rate of anaerobic pond ammonia nitrogen, the removal rate of ammonia nitrogen is relatively low when mixed-liquor return is relatively low, increases return current ratio of the mixed liquid ammonia nitrogen
Removal rate increases, but return current ratio of the mixed liquid do not answer it is excessively high because excessively high return current ratio of the mixed liquid can so that anaerobic pond oxygen content is difficult
To maintain, moreover, increasing additional energy consumption.
It is furthermore preferred that step 4）Described in A/O biochemical systems return current ratio of the mixed liquid be 1000%, by a series of tune
It haircuts existing, when return current ratio of the mixed liquid is 1000%, the removal rate for being discharged ammonia nitrogen is higher, and water outlet ammonia-nitrogen content is relatively low.
Step 4）Described in anaerobic treatment stage anaerobic pond oxygen content be 0.4 ~ 0.8mg/l.
Step 4）Described in Aerobic Process for Treatment stage aerobic tank oxygen content be 2 ~ 2.5mg/l.
In biochemical system, the oxygen content of anaerobic pond and aerobic tank is also to influence the principal element of its treatment effect, timely root
The oxygen content that anaerobic pond and aerobic tank are adjusted according to influent quality is also to improve the effective means of its treatment effect.
External pressing type hollow fibrous membrane is used in the ultrafiltration.
Compared with prior art, advantageous effect possessed by the present invention is：
1, processing method combination electrodialysis-MVR evaporative crystallization-A/O biochemical processing process of the invention, by control electrodialysis
Unit exports the salt content of concentrated water and fresh water, and the mode of ammonium hydroxide is added in MVR water inlets, avoids sulfate radical enrichment, effectively
Reduce the influence that boiling point heats up for salt crystallization effect, extends the operation stability of internal system MVR, by extending MVR systems
The operation stability of system ensures that the long-period stable operation of whole system, system stable operation time were improved from 2 ~ 3 days to 8 ~ 10
It, goes out the increase of salt amount, is 3t/ days.
2, the present invention improves organic matter and ammonia nitrogen by adjusting return current ratio of the mixed liquid and oxygen content in A/O biochemical systems
Treatment effect so that water outlet COD contents be reduced to 68 ~ 120mg/L, ammonia-nitrogen content to decrease below 5mg/L.
3, the efficiency of MVR evaporative crystallizations can be improved by the concentrated water conductance of control into MVR, reduce evaporation and crystal process
The middle amount for generating condensed water, reduces whole system heat consumption；And reduce the conductance of electrodialysis water outlet fresh water, that is, it is lowered into life
The salt content of the fresh water of change system can improve the treatment effeciency of biochemical system.
Specific implementation mode
Below by specific embodiment, the present invention will be further described.
The content of influent ammonia nitrogen is 800 ~ 1200mg/L in the embodiment of the present invention 1 ~ 6 and comparative example 1 ~ 4, and influent COD contains
Amount is 12000 ~ 15000mg/L.
Embodiment 1
The processing method of the present invention includes the following steps：
1）Filtering：Raw water enters ultrafiltration apparatus, ultrafiltration apparatus packet under the action of raw water pumps after basket filter filters
Four ultrafilters parallel with one another are included, the organic matter of the suspended matter and macromolecular in raw water is removed, external pressure is used in the ultrafiltration
Formula hollow-fibre membrane；
2）Electrodialysis：Ultra-filtration water enters the electrodialytic level-one concentrated water tank of level-one and level-one fresh water tank, is used for polishing liquid level, level-one
The concentrated water of concentrated water tank and the fresh water of level-one fresh water tank are delivered to the electrodialytic concentration chamber inlet of level-one and desalination chamber inlet by the road,
Setting voltage is 190 ~ 240V, and brine separation, the electrodialytic concentrated water outlet setting conductivity of level-one are carried out by level-one electrodialysis
Detector detects the conductance of exit concentrated water at any time, and when the conductance of exit concentrated water is higher than 180ms/cm, concentrated water enters concentration
Concentrated water tank, this concentrated water are concentration concentrated water；Electric conductivity detector is arranged in the electrodialytic water outlet of level-one, and it is light to detect exit at any time
The conductance of water, when the conductance of exit fresh water is higher than 24ms/cm, fresh water is back to level-one fresh water tank, when exit fresh water
When conductance is less than 24ms/cm, fresh water enters the two level concentrated water tank of two level electrodialysis cell and two level fresh water tank is used for polishing liquid level,
Similarly, electric conductivity detector is respectively set in the electrodialytic concentrated water outlet of two level and water outlet, detects concentrated water and fresh water at any time
Conductance, when the electrodialytic concentrated water conductance of two level be higher than 30ms/cm when, concentrate recirculation to level-one fresh water tank, when two level electrodialysis
Fresh water conductance when being less than 4ms/cm, fresh water enters biochemical system, this fresh water is biochemical fresh water, the level-one electrodialysis plant packet
Two groups of electrodialysis plants parallel with one another are included, zwitterion alloy is used in level-one electrodialysis plant and two level electrodialysis plant
Resin film, electrodialysis system carry out continuous brine separation through two-stage electrodialysis, must concentrate concentrated water and biochemical fresh water, and concentration is dense
The conductance of water is more than 180ms/cm, and the conductance of biochemical fresh water is less than 4ms/cm；
3）Evaporative crystallization：Ammonium hydroxide is added into concentration concentrated water tank, it is 7.5 ~ 8.5 to adjust its pH, and is examined in real time by pH detectors
It surveys, and the opening and closing of valve are added in chain control ammonium hydroxide, keeps pH in concentration concentrated water tank to remain 7.5 ~ 8.5, and will concentration
Concentrated water is pumped into the plate-type heat-exchange of MVR systems and condensed water exchanges heat, and temperature increases, and into forced circulation heater, forces to follow
Ring heater and crystallizer unicom, feed temperature is maintained at 95 ~ 102 DEG C in crystallizer, in forced circulation heater and crystallizer
Vapor in portion's material is evaporated out, and feed liquid has constantly been concentrated into after crystallization generates and has been discharged into thickener and passes through centrifuge output
Crystal salt, centrifuge make solid salt and mother liquor detach, and mother liquor enters mother liquor tank, then enter in crystallizer through mother liquor pump
It carries out repeating crystallization, evaporate the vapor generated in crystallizer is compressed by vapour compression machine, and into forced circulation is added
Hot device shell side, steam are cooled to condensed water to feed liquid heating part, are heated to concentrated water by plate heat exchanger, itself cooling
Enter biochemical system after within to 35 DEG C；
4）Biological treatment：Step 2）Mesophytization fresh water and step 3）The condensed water of middle generation enters A/O biochemical systems, sequentially enters
Anaerobic pond and aerobic tank, oxygen content is maintained at 0.5 ~ 0.6mg/l, hydraulic detention time 5.5d in anaerobic pond, and aerobic tank includes
Oxygen amount is maintained at 2.2 ~ 2.40mg/l, and return current ratio of the mixed liquid is 1000% in hydraulic detention time 22d, A/O biochemical system, is gone out
Water detects water quality, is shown in Table 1.
Embodiment 2
The present embodiment with embodiment 1 difference lies in：The electric conductivity detector detection water outlet concentrated water of level-one electrodialysis concentrated water outlet
Conductance be higher than 160ms/cm when, water outlet concentrated water enter concentration concentrated water tank, and then enter MVR；And two level electrodialysis fresh water goes out
When conductivity detector detection fresh water conductance is less than 6ms/cm at mouthful, fresh water enters biochemical system.
Embodiment 3
The present embodiment with embodiment 1 difference lies in：Ammonium hydroxide is added into concentration concentrated water tank, it is 6 ~ 7 to adjust its pH.
Embodiment 4
The present embodiment with embodiment 1 difference lies in：Ammonium hydroxide is added into concentration concentrated water tank, it is 8.5 ~ 9 to adjust its pH.
Embodiment 5
The present embodiment with embodiment 1 difference lies in：Step 4）Described in A/O biochemical systems return current ratio of the mixed liquid be 800%,
Oxygen content is maintained at 0.4 ~ 0.5mg/l in anaerobic pond, and oxygen content is maintained at 2.0 ~ 2.3mg/l in aerobic tank.
Embodiment 6
The present embodiment with embodiment 1 difference lies in：Step 4）Described in A/O biochemical systems return current ratio of the mixed liquid be 1100%,
Oxygen content is maintained at 0.6 ~ 0.8mg/l in anaerobic pond, and oxygen content is maintained at 2.3 ~ 2.5mg/l in aerobic tank.
Comparative example 1
This comparative example with embodiment 1 difference lies in：Concentration concentrated water, which is not added with ammonium hydroxide and is directly entered MVR, is evaporated crystallization.
Comparative example 2
This comparative example with embodiment 1 difference lies in：Ammonium hydroxide is added in concentration concentrated water, it is 5.5 ~ 6.5 to adjust its pH.
Comparative example 3
This comparative example with embodiment 1 difference lies in：The electric conductivity detector detection water outlet concentrated water of level-one electrodialysis concentrated water outlet
Conductance be higher than 150ms/cm when, water outlet concentrated water enter concentration concentrated water tank, and then enter MVR；And two level electrodialysis fresh water goes out
When conductivity detector detection fresh water conductance is less than 7ms/cm at mouthful, fresh water enters biochemical system.
Comparative example 4
This comparative example with embodiment 1 difference lies in：Step 4）Described in A/O biochemical systems return current ratio of the mixed liquid be 700%,
Oxygen content is maintained at 0.2 ~ 0.4mg/l in anaerobic pond, and oxygen content is maintained at 2.6 ~ 3mg/l in aerobic tank.
Table 1 is the treatment effect of 1 ~ 4 processing method of embodiment 1 ~ 6 and comparative example
As shown in Table 1, compared with comparative example 1 ~ 4, system uptime rises appreciably embodiment 1 ~ 6, illustrates to add ammonium hydroxide
The problem of effectively improving difficult crystallization in MVR so that system uptime was extended for 8 ~ 10 days by 2 ~ 3 days, and went out salt
Amount is consequently increased, and is crystallized out salt and smoothly be ensure that raw water is sustainable and into device and ensures the stable operation of subsequent technique；
Meanwhile embodiment 1 ~ 6 is discharged COD and ammonia-nitrogen content is decreased obviously, in embodiment 1 ~ 6, COD contents are in 68 ~ 120mg/L, hence it is evident that
Less than 165 ~ 212mg/L of comparative example 1 ~ 4；Ammonia-nitrogen content also has 8 ~ 12mg/L of comparative example 1 ~ 4 to drop to 2.9 ~ 5mg/L.
The above described is only a preferred embodiment of the present invention, being not that the invention has other forms of limitations, appoint
What those skilled in the art changed or be modified as possibly also with the technology contents of the disclosure above equivalent variations etc.
Imitate embodiment.But it is every without departing from technical solution of the present invention content, according to the technical essence of the invention to above example institute
Any simple modification, equivalent variations and the remodeling made, still fall within the protection domain of technical solution of the present invention.
Claims (9)
1. a kind of processing method of cephalosporin antibiotic production waste water, it is characterised in that：Include the following steps：
1）Filtering：Raw water enters ultrafiltration apparatus after basket filter filters and carries out fine filtering, removes the suspended matter in raw water
With the organic matter of macromolecule；
2）Electrodialysis：Ultra-filtration water enters electrodialysis system, carries out continuous brine separation through two-stage electrodialysis, obtains concentration concentrated water
With biochemical fresh water, the conductance for concentrating concentrated water is more than 160ms/cm, and the conductance of biochemical fresh water is less than 6ms/cm；
3）Evaporative crystallization：Step 2）Described in concentrated water enter MVR systems and be evaporated and crystallize to obtain solid salt, and generate condensed water；
4）Biological treatment：Step 2）Middle fresh water and step 3）The condensed water of middle generation enters A/O biochemical systems, carries out anaerobism successively
Processing and Aerobic Process for Treatment remove large amount of organic and ammonia nitrogen；
Step 2）Ammonium hydroxide is added before entering MVR systems in gained concentrated water, and it is 6 ~ 9 to adjust its pH.
2. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：Step 2）Gained is dense
Ammonium hydroxide is added before entering MVR systems in water, and it is 7.5 ~ 8.5 to adjust its pH.
3. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：Step 2）Described in
The conductance for concentrating concentrated water is more than 180ms/cm.
4. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：Step 2）Described in
The conductance of biochemical fresh water is less than 4ms/cm.
5. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：Step 4）Described in
Return current ratio of the mixed liquid is 800 ~ 1100% in A/O biochemical systems.
6. the processing method of cephalosporin antibiotic production waste water according to claim 5, it is characterised in that：Step 4）Described in
Return current ratio of the mixed liquid is 1000% in A/O biochemical systems.
7. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：Step 4）Described in
The oxygen content of anaerobic treatment stage anaerobic pond is 0.4 ~ 0.8mg/l.
8. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：Step 4）Described in
The oxygen content of Aerobic Process for Treatment stage aerobic tank end is 2 ~ 2.5mg/l.
9. the processing method of cephalosporin antibiotic production waste water according to claim 1, it is characterised in that：It is adopted in the ultrafiltration
Use external pressing type hollow fibrous membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810180806.1A CN108455793B (en) | 2018-03-06 | 2018-03-06 | Method for treating cephalosporin antibiotic production wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810180806.1A CN108455793B (en) | 2018-03-06 | 2018-03-06 | Method for treating cephalosporin antibiotic production wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108455793A true CN108455793A (en) | 2018-08-28 |
| CN108455793B CN108455793B (en) | 2021-04-27 |
Family
ID=63217163
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810180806.1A Active CN108455793B (en) | 2018-03-06 | 2018-03-06 | Method for treating cephalosporin antibiotic production wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108455793B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109502930A (en) * | 2019-01-10 | 2019-03-22 | 山东蓝然环境科技有限公司 | A kind of technique waste water processing unit of biological enzyme antibiotic |
| CN109851162A (en) * | 2019-01-18 | 2019-06-07 | 中国石油工程建设有限公司 | A kind of oil gas field brine waste treatment process up to standard |
| CN110746046A (en) * | 2019-11-04 | 2020-02-04 | 浙江迈沃加科技有限公司 | Cephalosporin pharmaceutical wastewater treatment process |
| CN111484182A (en) * | 2020-05-12 | 2020-08-04 | 华北制药股份有限公司 | 7-ADCA mother liquor recovery processing method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040055955A1 (en) * | 2002-08-02 | 2004-03-25 | University Of South Carolina | Production of purified water and high value chemicals from salt water |
| US20050247631A1 (en) * | 2004-05-07 | 2005-11-10 | Ecolochem, Inc | Water purification system and method using reverse osmosis reject stream in an electrodeionization unit |
| CN103183403A (en) * | 2011-12-31 | 2013-07-03 | 南开大学 | Antibiotic pharmaceutical wastewater processing method and device |
| CN103771642A (en) * | 2014-01-09 | 2014-05-07 | 杭州蓝然环境技术有限公司 | Recycling method for saponified ammonium-sulfate wastewater in rare soil |
| CN104058537A (en) * | 2014-04-30 | 2014-09-24 | 浙江工业大学 | Method for treating cefalexin enzyme-process synthesizing mother liquor wastewater |
-
2018
- 2018-03-06 CN CN201810180806.1A patent/CN108455793B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040055955A1 (en) * | 2002-08-02 | 2004-03-25 | University Of South Carolina | Production of purified water and high value chemicals from salt water |
| US20050247631A1 (en) * | 2004-05-07 | 2005-11-10 | Ecolochem, Inc | Water purification system and method using reverse osmosis reject stream in an electrodeionization unit |
| CN103183403A (en) * | 2011-12-31 | 2013-07-03 | 南开大学 | Antibiotic pharmaceutical wastewater processing method and device |
| CN103771642A (en) * | 2014-01-09 | 2014-05-07 | 杭州蓝然环境技术有限公司 | Recycling method for saponified ammonium-sulfate wastewater in rare soil |
| CN104058537A (en) * | 2014-04-30 | 2014-09-24 | 浙江工业大学 | Method for treating cefalexin enzyme-process synthesizing mother liquor wastewater |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109502930A (en) * | 2019-01-10 | 2019-03-22 | 山东蓝然环境科技有限公司 | A kind of technique waste water processing unit of biological enzyme antibiotic |
| CN109851162A (en) * | 2019-01-18 | 2019-06-07 | 中国石油工程建设有限公司 | A kind of oil gas field brine waste treatment process up to standard |
| CN110746046A (en) * | 2019-11-04 | 2020-02-04 | 浙江迈沃加科技有限公司 | Cephalosporin pharmaceutical wastewater treatment process |
| CN111484182A (en) * | 2020-05-12 | 2020-08-04 | 华北制药股份有限公司 | 7-ADCA mother liquor recovery processing method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108455793B (en) | 2021-04-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108249646B (en) | Power plant desulfurization wastewater zero-emission treatment process and device capable of recycling resources | |
| CN108529802B (en) | Zero-discharge process for discharging high-salt-content wastewater in titanium dioxide production | |
| CN101734820B (en) | Method for treating high slat-containing wastewater | |
| CN108455793A (en) | A kind of processing method of cephalosporin antibiotic production waste water | |
| CN107265734B (en) | Reverse osmosis concentrated seawater treatment system and method | |
| CN104803448A (en) | Forward osmosis treatment method of wastewater with high salinity and high organic matter concentration | |
| CN105461157A (en) | High-salinity high-organic-matter contentwastewater zero discharge method | |
| CN110818192A (en) | Industrial park mixed wastewater desalination process | |
| CN105540980A (en) | Advanced oxidation-separate salt crystallization combination system of high-salt-salt industrial wastewater | |
| CN107915360A (en) | Zero-emission crystallization divides salt device and technique | |
| CN105198143A (en) | High-concentration wastewater zero-discharging method | |
| CN208120896U (en) | Can resource recycling power plant desulfurization wastewater zero discharge treatment device | |
| CN203768159U (en) | Small seawater desalination device | |
| CN108658345A (en) | A kind of method and system of high-salt wastewater purified salt | |
| CN105219892A (en) | A kind of xylose production process | |
| CN103172212A (en) | Treatment method of lignin production waste water | |
| CN110451707A (en) | A kind of waste water of mine Zero discharge treatment method | |
| CN113651468A (en) | Seawater recycling treatment process | |
| CN114180768A (en) | Multi-stage nanofiltration salt separation system for separating sodium sulfate and sodium chloride in coking wastewater and method for treating wastewater by using same | |
| CN104591456B (en) | A kind of processing method of high salt ammonia nitrogen waste water | |
| CN205222911U (en) | Zero release of coal industry strong brine and salt manufacturing device | |
| CN110550802A (en) | High-salinity aqueous solution zero-emission treatment system and method | |
| CN102745852B (en) | Brine-desalination method | |
| CN204434415U (en) | Concentrating and treating system is softened in a kind of heat-engine plant desulfurized Wastewater by Electric dialysis | |
| CN104671572A (en) | Electrodialysis softening and concentrating treatment system and method for desulfurization wastewater from thermal power plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210325 Address after: Room 1908, 19th floor, Hall B, Huangtai e-commerce Industrial Park, 19 Lishan North Road, Tianqiao District, Jinan City, Shandong Province, 250032 Applicant after: SHANDONG BLUESKY ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Address before: 256400 Tianqi Auto Expo Park, Huantai County, Zibo City, Shandong Province Applicant before: Wang Lei |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |