CN101402502B - Treatment method and apparatus for mifepristone wastewater - Google Patents
Treatment method and apparatus for mifepristone wastewater Download PDFInfo
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- CN101402502B CN101402502B CN2008101169539A CN200810116953A CN101402502B CN 101402502 B CN101402502 B CN 101402502B CN 2008101169539 A CN2008101169539 A CN 2008101169539A CN 200810116953 A CN200810116953 A CN 200810116953A CN 101402502 B CN101402502 B CN 101402502B
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- 239000002351 wastewater Substances 0.000 title claims abstract description 45
- VKHAHZOOUSRJNA-GCNJZUOMSA-N mifepristone Chemical compound C1([C@@H]2C3=C4CCC(=O)C=C4CC[C@H]3[C@@H]3CC[C@@]([C@]3(C2)C)(O)C#CC)=CC=C(N(C)C)C=C1 VKHAHZOOUSRJNA-GCNJZUOMSA-N 0.000 title claims abstract description 36
- 229960003248 mifepristone Drugs 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 230000001112 coagulating effect Effects 0.000 claims abstract description 28
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 10
- 239000002253 acid Substances 0.000 claims abstract description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 64
- 239000001301 oxygen Substances 0.000 claims description 64
- 229910052760 oxygen Inorganic materials 0.000 claims description 64
- 239000010802 sludge Substances 0.000 claims description 37
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 238000001556 precipitation Methods 0.000 claims description 20
- 238000005345 coagulation Methods 0.000 claims description 16
- 230000015271 coagulation Effects 0.000 claims description 16
- 238000005192 partition Methods 0.000 claims description 11
- 230000003647 oxidation Effects 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 8
- 239000002244 precipitate Substances 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 5
- 230000008878 coupling Effects 0.000 claims description 3
- 238000010168 coupling process Methods 0.000 claims description 3
- 238000005859 coupling reaction Methods 0.000 claims description 3
- 239000011259 mixed solution Substances 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 abstract description 8
- 239000010865 sewage Substances 0.000 abstract description 8
- 238000006460 hydrolysis reaction Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 230000007062 hydrolysis Effects 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 8
- 238000006396 nitration reaction Methods 0.000 description 7
- 238000007034 nitrosation reaction Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000003851 biochemical process Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000036284 oxygen consumption Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 241001453382 Nitrosomonadales Species 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000002894 chemical waste Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Abstract
The invention discloses a mifepristone wastewater treatment method and a treatment equipment thereof. The method comprises the following steps: (1) adding an acid liquor in the treated mifepristone production wastewater, and adjusting the pH value of the wastewater to 7.8-8.2; (2) introducing the wastewater after the pH value is adjusted into a facultative reactor for hydrolysis and denitrification, and introducing the facultative reactor water effluent into an aerobic reactor in which CODCr is removed and ammonia-nitrogen in the wastewater is oxidized; and (3) further removing the CODCr and NH3-N after the aerobic reactor effluent is subjected to coagulating sedimentation treatment, and discharging the effluent. The contents of the CODCr and the NH3-N in the treated mifepristone wastewater meet the first class standard of the national sewage comprehensive emission standard (GB8978-1996), and the content of the effluent ammonia-nitrogen is less than 2mg/l, thereby saving power cost, improving the efficiency of removing the ammonia-nitrogen and lowering the treatment cost, and the treatment cost per ton of wastewater is only 3.3 yuan.
Description
Technical field
The present invention relates to a kind of wastewater processing technology, relate in particular to treatment process and the treatment facility of COD and ammonia nitrogen in a kind of mifepristone waste water of degrading, belong to the environment protection treating field.
Background technology
Mifepristone (mifepristone) factory effluent derives from residue chemical feedstocks, intermediate product and the by product in mifepristone chemosynthesis workshop, organic solvent etc.Containing in the waste water that metabolism has inhibiting pollutent to microorganism growth in a large number, contain the ammonia nitrogen and the organic pollutant of high density, is one of high pollution and more unmanageable trade effluent.Treatment technology to mifepristone waste water has both at home and abroad: physico-chemical process, biochemical process and materialization and the biochemical method that combines.Wherein denitrogenation method is mainly based on biochemical process, and biochemical process has double oxygen-catalytic oxidation, and cyclic activated sludge system etc., these treatment process all are effective mifepristone method of wastewater treatment.In the processing of this waste water, generally cause Pollutant Treatment inefficiencies such as this wastewater through organic matter and ammonia nitrogen because of process parameters design is unreasonable at present, be difficult to reach the design objective requirement, particularly the ammonia nitrogen removal effect is undesirable.
Summary of the invention
Embodiment of the present invention provides a kind of mifepristone method of wastewater treatment and treatment facility, and this method is in the mode that hydrolysis, denitrification cooperate and the ammonia nitrogen oxidizing reaction cooperates, and makes the COD of the mifepristone waste water after the processing
CrWith NH
3-N reaches emission standard, and this treatment process is stable, energy consumption is low and convenient management.
The objective of the invention is to be achieved through the following technical solutions:
Embodiment of the present invention provides a kind of mifepristone method of wastewater treatment, and this method comprises:
(1) regulate the pH value: add acid solution in the mifepristone factory effluent of handling, the pH value of regulating described waste water is 7.8～8.2;
(2) biochemical treatment: make the waste water of regulating after the pH value enter the oxygen reactor of holding concurrently and be hydrolyzed and denitrification denitrogenation, double oxygen reactor water outlet enters aerobic reactor, removes COD at the aerobic reactor internal reaction
CrAnd make the ammonia nitrogen in the waste water carry out oxidation; Wherein, the total hrt of described waste water in hold concurrently oxygen reactor and aerobic reactor is 80～109h; Described waste water is 27 ℃～33 ℃ in the temperature of reaction of the oxygen reactor of holding concurrently, and sludge age is 40～50 days, and dissolved oxygen content DO is 0.05mg/l～0.5mg/l, and the pH value is 7.5～8.5; Described waste water is 27 ℃～33 ℃ in the temperature of reaction of aerobic reactor, and sludge age is 40～50 days, and dissolved oxygen content DO is 1.1～2.5mg/l, and the pH value is 7.5～8.2;
(3) the aerobic reactor water outlet is handled through coagulating sedimentation and is further removed COD
CrWith NH
3Discharge behind-the N.
Described coagulating sedimentation is handled and comprised: the aerobic reactor water outlet enters in the second pond and precipitates, and precipitation obtains supernatant liquor and excess sludge, and supernatant liquor enters coagulation reaction tank to carry out coagulating and remove COD
CrWith NH
3-N, the waste water after the processing enter coagulative precipitation tank and precipitate once more, handle back water and discharge sedimentary excess sludge discharge.
The hydraulic detention time of described coagulation reaction tank is 15～25min, and the surface load of coagulative precipitation tank is 0.6～1.2m
3/ m
2.h.
Described method further comprises: the sedimentary excess sludge of second pond all was back in the described double oxygen reactor and carries out circulating reaction during mixed solution in the aerobic reactor and coagulating sedimentation were handled.
Described return current ratio of the mixed liquid is 300%～500%, and the residual sludge reflux ratio is 50%～100%, and the sludge concentration in the oxygen reactor of holding concurrently is 3.0～4.0g/l, and sludge concentration is 3.0～3.5g/l in the aerobic reactor.
Embodiment of the present invention also provides a kind of treatment facility of realizing above-mentioned each the described method of claim, and this equipment comprises: equalizing tank unit, hold concurrently oxygen reactor, aerobic reactor, second pond, coagulation reaction tank, coagulative precipitation tank, mixed-liquor return pipe, mud return line and variable valve; Wherein, equalizing tank unit, the oxygen reactor of holding concurrently, aerobic reactor, second pond, coagulation reaction tank are connected successively with coagulative precipitation tank; Unitary water inlet pipe of equalizing tank and mifepristone influent waste water pipe coupling; Aerobic reactor returns by the mixed-liquor return pipe and is connected to double oxygen reactor; The excess sludge outlet of second pond is returned through mud return line and is connected to double oxygen reactor; Coagulative precipitation tank is provided with excess sludge relief outlet and water outlet.
Be provided with partition wall in the described aerobic reactor, the partition wall bottom is provided with through hole, and the partition wall that has through hole is separated into aerobic reactor inside two portions of intercommunication.
Described equipment also comprises: blower fan, this blower fan is communicated with two portions of separating in the aerobic reactor respectively by pipeline, variable valve, also is provided with blow-off valve on the described connecting pipeline.
Be provided with divider wall in the described double oxygen reactor, divider wall is provided with through hole, and the described divider wall that the has through hole oxygen reactor inside of will holding concurrently is separated into two portions of intercommunication.
Described equipment also comprises: two reflux pumps are separately positioned on mixed-liquor return pipe and the mud return line.
The technical scheme that provides by the invention described above embodiment as can be seen, embodiment of the present invention is hydrolyzed and the anti-nitration reaction denitrogenation in the oxygen reactor of holding concurrently by the mifepristone waste water that will regulate after the pH value, and enters and remove COD in the aerobic reactor
CrAnd carry out the ammonia nitrogen oxidation, after handling, coagulating sedimentation further removes COD
CrWith NH
3-N reaches the COD that removes in the mifepristone waste water
CrWith NH
3The purpose of-N, the COD of the mifepristone waste water after this method is handled
CrWith NH
3-N has reached the primary standard of national sewage comprehensive emission standard (GB8978-1996), and the water outlet ammonia nitrogen can reach below the 2mg/l, the part nitrosation reaction that takes place in the aerobic reactor has been saved oxygen-consumption, thereby saved part power charge about about 4%, interior Anammox reaction reduction aerobic reactor ammonia nitrogen loading that takes place of the oxygen reactor of holding concurrently, improve the removal efficient of ammonia nitrogen, saved power charge simultaneously, cost of water treatment per ton is about 3.3 yuan, and the water outlet ammonia nitrogen reaches below the 2mg/l.
Description of drawings
Fig. 1 is the mifepristone sewage treatment equipment syndeton synoptic diagram of the embodiment of the invention one;
Fig. 2 is the mifepristone sewage treatment equipment syndeton synoptic diagram of the embodiment of the invention two;
Each label is respectively among the figure: 1, equalizing tank; 2, double oxygen reactor; 21, divider wall; 3, aerobic reactor; 31, partition wall; 4, second pond; 5, coagulation reaction tank; 6, coagulative precipitation tank; 7, mixed-liquor return pipe; 8, mud return line; 9, blower fan; 10, variable valve A; 11, variable valve B; 12, blow-off valve; 13, reflux pump A; 14, reflux pump B; A, coking chemical waste water water inlet pipe; B, water outlet; C, sludge outlet; D, excess sludge relief outlet; E, material add inlet; F, acid solution add inlet.
Embodiment
Embodiment of the present invention provides a kind of mifepristone method of wastewater treatment and treatment facility, oxygen compatibility pool is hydrolyzed this treatment process and denitrification denitrogenation by the mifepristone factory effluent is entered after equalizing tank adds acid solution adjusting pH, and the oxygen compatibility pool water outlet removes COD at Aerobic Pond
CrWith the oxidation of carrying out ammonia nitrogen, the Aerobic Pond water outlet is formed sediment to handle through coagulation and is further removed COD
CrWith NH
3-N.Wherein, described waste water is 27 ℃～33 ℃ in the temperature of reaction of the oxygen reactor of holding concurrently, and sludge age is 40～50 days, and DO is 0.05mg/l～0.5mg/l, and pH is 7.5～8.5; Described waste water is 27 ℃～33 ℃ in the temperature of reaction of aerobic reactor, and sludge age is 40～50 days, and DO is 1.1～2.5mg/l, and pH is 7.5～8.2; Hold concurrently oxygen reactor and aerobic reactor is non-single the mixing fully or the reactor of plug-flow, be mixed type, total hrt is 80～109h, organic hydrolysis reaction takes place in double oxygen reactor, the anti-nitration reaction of concurrent caliche hydrochlorate and nitrite, the reaction of part Anammox, organic oxidation takes place in aerobic reactor, the nitrosation reaction of ammonia nitrogen and nitration reaction.This treatment process is stable, energy consumption is low and convenient management, handles the COD of back mifepristone waste water
CrWith NH
3-N can reach the primary standard of national sewage comprehensive emission standard (GB8978-1996), and the water outlet ammonia nitrogen reaches below the 2mg/l, and processing cost is low, and cost of water treatment per ton is about 3.3 yuan.
For ease of understanding, embodiments of the present invention are described further below in conjunction with the drawings and specific embodiments.
Embodiment one
The treatment facility that a kind of mifepristone production wastewater treatment method that present embodiment provides is adopted as shown in Figure 1, this equipment comprises: equalizing tank unit 1, the oxygen reactor 2 of holding concurrently, aerobic reactor 3, second pond 4, coagulation reactor 5 and coagulative precipitation tank 6; Wherein, equalizing tank unit 1, the oxygen reactor 2 of holding concurrently, aerobic reactor 3, second pond 4, coagulation reaction tank 5 are connected successively with coagulative precipitation tank 6, and double oxygen reactor 2 and aerobic reactor 3 are built jointly and be structure as a whole; The water inlet pipe of equalizing tank unit 1 and mifepristone influent waste water pipe coupling; Aerobic reactor 3 is connected to the oxygen reactor 2 of holding concurrently for 7 times by the mixed-liquor return pipe; The sludge outlet C of second pond 4 is connected to the oxygen reactor 2 of holding concurrently for 8 times through mud return line, and reflux pump A13 and reflux pump B14 can be set on mixed-liquor return pipe 7 and mud return line 8 respectively, to guarantee and control backflow effect; Coagulative precipitation tank 6 is provided with excess sludge relief outlet D and water outlet B.Wherein, be provided with partition wall 31 in the described aerobic reactor 3, partition wall 31 bottoms are provided with through hole, and the partition wall 31 that has through hole is separated into aerobic reactor 3 inside two portions of intercommunication.This equipment also comprises blower fan 10, is used for to aerobic reactor 3 oxygenations, and this blower fan 10 is communicated with two portions of separation in the aerobic reactor 3 respectively by pipeline, variable valve A10 and variable valve B11, also is provided with blow-off valve 12 on the described connecting pipeline.
Utilize the concrete grammar of above-mentioned treatment facility processing mifepristone factory effluent as follows:
(1) regulates pH value: the mifepristone factory effluent of handling is put into the equalizing tank unit, and adding technical hydrochloric acid in this equalizing tank unit, to regulate the pH value of described waste water be 7.8～8.2, to safeguard double oxygen reactor microorganism growth environment;
(2) biochemical treatment: make the waste water of regulating after the pH value enter the oxygen reactor of holding concurrently and be hydrolyzed and denitrification denitrogenation, double oxygen reactor water outlet enters aerobic reactor, removes COD at the aerobic reactor internal reaction
CrAnd carry out oxidation with ammonia nitrogen; Wherein, the total hrt of waste water in hold concurrently oxygen reactor and aerobic reactor is 80～109h, waste water is 27 ℃～33 ℃ in the temperature of reaction of the oxygen reactor of holding concurrently, sludge age is 40～50 days, dissolved oxygen content DO is 0.05mg/l～0.5mg/l, pH is 7.5～8.5, with smooth realization microorganism to organic hydrolytic action, denitrifying bacterium is reduced to nitrogen with nitrate and part nitrite, anaerobic ammonia oxidizing bacteria utilizes nitrite that ammonia nitrogen is oxidized to nitrogen, reaches the purpose of final denitrification;
Waste water is 27 ℃～33 ℃ in the temperature of reaction of aerobic reactor, sludge age is 40～50 days, dissolved oxygen content DO is 1.0～2.5mg/l, the pH value is 7.5～8.2, the dissolved oxygen content DO of oxygen reactor influent side of controlling well is about 2.0mg/l, the dissolved oxygen content DO of water outlet side is 1.0～1.5mg/l, to control the pH value of the waste water in the oxygen reactor well be 7.5～8.2 by add liquid caustic soda in aerobic reactor, the aerobic reactor intermediary has the partition wall of through hole, aerobic reactor is divided into two portions that both sides link to each other, decarburizing reaction mainly takes place in its influent side, the nitration reaction of the Nitromonas of small part takes place simultaneously, and the nitration reaction of Nitromonas and the nitrosation reaction of Nitrosomas mainly take place in water outlet side.
In the reality, hold concurrently oxygen reactor and aerobic reactor is non-single the mixing fully or the reactor of plug-flow, be mixed type, organic hydrolysis reaction takes place in double oxygen reactor, the anti-nitration reaction of concurrent caliche hydrochlorate and nitrite, the reaction of part Anammox, organic oxidation takes place in aerobic reactor, the nitrosation reaction of ammonia nitrogen and nitration reaction;
Return sludge ratio is 50%～100%, and return current ratio of the mixed liquid is 300%～500%, and the oxygen reactor sludge concentration of holding concurrently is 3.0～4.0g/l, and sludge concentration is 3.0～3.5g/l in the aerobic reactor.The water outlet ammonia nitrogen concentration is below the 2mg/l, and COD is below the 100mg/l.
(3) the aerobic reactor water outlet is handled through coagulating sedimentation and is further removed COD
CrWith NH
3-N, described coagulating sedimentation is handled and specifically comprised: the aerobic reactor water outlet is handled through in second pond, coagulation reaction tank and the coagulative precipitation tank successively, at first, the aerobic reactor water outlet enters in the second pond and precipitates, precipitation obtains supernatant liquor and thickened sludge, and supernatant liquor enters coagulation reaction tank to carry out coagulating and remove COD
CrWith NH
3-N, the waste water after the processing enter coagulative precipitation tank and precipitate once more, efflux after the processing, and a part of mud refluxes, excess sludge discharge; Wherein, the hydraulic detention time of coagulation reaction tank is 15～25min, and the surface load of coagulative precipitation tank is 0.6～1.2m
3/ m
2.h.
In coagulating sedimentation was handled, the thickened sludge that mixed solution that obtains in the aerobic reactor and second pond obtain all was back to double oxygen reactor in above-mentioned aerobic reactor water outlet; Described return current ratio of the mixed liquid is 300%～500%, and return sludge ratio is 50%～100%, and the sludge concentration in the oxygen reactor of holding concurrently is 3.0～4.0g/l, and sludge concentration is 3.0～3.5g/l in the aerobic reactor.
After the aforesaid method processing, can remove the COD in the mifepristone factory effluent
CrWith NH
3-N, make waste water after the processing reach the primary standard of national sewage comprehensive emission standard (GB8978-1996), the water outlet ammonia nitrogen can reach below the 2mg/l, and the part nitrosation reaction that this method takes place in aerobic reactor has been saved oxygen-consumption, thereby saved part power charge about about 4%, interior Anammox reaction reduction aerobic reactor ammonia nitrogen loading that takes place of the oxygen reactor of holding concurrently, improve the removal efficient of ammonia nitrogen, saved power charge simultaneously, therefore processing cost is lower, and cost of water treatment per ton only is about 3.3 yuan.
Embodiment two
In the present embodiment, mifepristone production wastewater treatment equipment as shown in Figure 2, each structure of this treatment facility is identical with treatment facility among the embodiment one, with the treatment facility difference of implementing one be that the divider wall that the double oxygen reactor of this equipment is had a through hole is divided into two sections, the double oxygen reactor of this structure helps double oxygen and gathers with separating with rich of anaerobion, improves the speed of reaction of denitrification and Anammox; In addition, the double oxygen reactor of this equipment and aerobic reactor are for dividing the branch body structure of building, and double oxygen reactor and aerobic reactor that this branch is built structure help adapting to sewage treatment project place needs, and adaptability is strong, is convenient to construction.
It is identical with the treatment process of embodiment one to utilize treatment facility in the present embodiment to carry out the treatment process of mifepristone factory effluent, no longer repeats here.
In sum, in the embodiment of the invention by after will regulating mifepristone factory effluent after the pH value and in the oxygen reactor of holding concurrently, handling, in aerobic reactor, carry out decarburization and ammonia nitrogen oxidation, and by after the further processing of coagulation, the COD in the mifepristone factory effluent of processing
CrWith NH
3-N concentration reaches the primary standard of national sewage comprehensive emission standard (GB8978-1996), is a kind of method of wastewater treatment of efficient, energy-saving and environmental protection.
The above; only for the preferable embodiment of the present invention, but protection scope of the present invention is not limited thereto, and anyly is familiar with those skilled in the art in the technical scope that the present invention discloses; the variation that can expect easily or replacement all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claim.
Claims (8)
1. a mifepristone method of wastewater treatment is characterized in that, this method comprises:
(1) regulate the pH value: add acid solution in the mifepristone factory effluent of handling, the pH value of regulating described waste water is 7.8～8.2;
(2) biochemical treatment: make the waste water of regulating after the pH value enter the oxygen reactor of holding concurrently and be hydrolyzed and denitrification denitrogenation, double oxygen reactor water outlet enters aerobic reactor, removes COD at the aerobic reactor internal reaction
CrAnd make the ammonia nitrogen in the waste water carry out oxidation; Wherein, the total hrt of described waste water in hold concurrently oxygen reactor and aerobic reactor is 80～109h; Described waste water is 27 ℃～33 ℃ in the temperature of reaction of the oxygen reactor of holding concurrently, and sludge age is 40～50 days, and dissolved oxygen content DO is 0.05mg/l～0.5mg/l, and the pH value is 7.5～8.5; Described waste water is 27 ℃～33 ℃ in the temperature of reaction of aerobic reactor, and sludge age is 40～50 days, and dissolved oxygen content DO is 1.1～2.5mg/l, and the pH value is 7.5～8.2; The oxygen reactor sludge concentration of holding concurrently is 3.0～4.0g/l, and sludge concentration is 3.0～3.5g/l in the aerobic reactor;
(3) the aerobic reactor water outlet enters in the second pond and precipitates, and precipitation obtains supernatant liquor and dense mud, and supernatant liquor enters coagulation reaction tank to carry out coagulating and remove COD
CrWith NH
3-N becomes treating water and discharges, and the waste water after the processing enters coagulative precipitation tank and precipitates once more, sedimentary excess sludge discharge;
The hydraulic detention time of described coagulation reaction tank is 15～25min, and the surface load of coagulative precipitation tank is 0.6～1.2m
3/ m
2.h.
2. method according to claim 1 is characterized in that, described method further comprises: the sedimentary excess sludge of mixed solution in the aerobic reactor and second pond all is back in the described double oxygen reactor.
3. method according to claim 4 is characterized in that, described return current ratio of the mixed liquid is 300%～500%, and return sludge ratio is 50%～100%.
4. treatment facility of realizing each described method in the claim 1～3, it is characterized in that this equipment comprises: equalizing tank unit, hold concurrently oxygen reactor, aerobic reactor, second pond, coagulation reaction tank, coagulative precipitation tank, mixed-liquor return pipe and mud return line; Wherein, equalizing tank unit, the oxygen reactor of holding concurrently, aerobic reactor, second pond, coagulation reaction tank are connected successively with coagulative precipitation tank; Unitary water inlet pipe of equalizing tank and mifepristone influent waste water pipe coupling; Aerobic reactor returns by the mixed-liquor return pipe and is connected to double oxygen reactor; The sludge outlet of second pond returns through mud return line and is connected to double oxygen reactor; Coagulative precipitation tank is provided with excess sludge relief outlet and water outlet.
5. equipment according to claim 4 is characterized in that, is provided with partition wall in the described aerobic reactor, and the partition wall bottom is provided with through hole, and the partition wall that has through hole is separated into aerobic reactor inside two portions of intercommunication.
6. equipment according to claim 5 is characterized in that, described equipment also comprises: blower fan, this blower fan is communicated with two portions of separating in the aerobic reactor respectively by pipeline, variable valve, also is provided with blow-off valve on the described connecting pipeline.
7. equipment according to claim 4 is characterized in that, is provided with divider wall in the described double oxygen reactor, and divider wall is provided with through hole, and the described divider wall that the has through hole oxygen reactor inside of will holding concurrently is separated into two portions of intercommunication.
8. according to claim 4 or 5 or 7 described equipment, it is characterized in that described equipment also comprises: two reflux pumps are separately positioned on mixed-liquor return pipe and the mud return line.
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|---|---|---|---|
| CN2008101169539A CN101402502B (en) | 2008-07-21 | 2008-07-21 | Treatment method and apparatus for mifepristone wastewater |
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|---|---|---|---|
| CN2008101169539A CN101402502B (en) | 2008-07-21 | 2008-07-21 | Treatment method and apparatus for mifepristone wastewater |
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|---|---|
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| CN101402502B true CN101402502B (en) | 2011-04-27 |
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| JP2012206040A (en) * | 2011-03-30 | 2012-10-25 | Kurita Water Ind Ltd | Treatment method and treatment apparatus of organic matter containing wastewater |
| CN104355501B (en) * | 2014-11-18 | 2016-05-04 | 中国环境科学研究院 | A kind of acetone production process produces the processing method of waste water |
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