CN104609540A - Ammonia-containing wastewater treatment method - Google Patents
Ammonia-containing wastewater treatment method Download PDFInfo
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- CN104609540A CN104609540A CN201310537904.3A CN201310537904A CN104609540A CN 104609540 A CN104609540 A CN 104609540A CN 201310537904 A CN201310537904 A CN 201310537904A CN 104609540 A CN104609540 A CN 104609540A
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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
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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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
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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
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention provides an ammonia-containing wastewater treatment method which comprises the following content: nitrification sludge and aerobic denitrification sludge are added into a bioreactor with a built-in membrane separation assembly; the nitrification sludge undergoes nitration in an area outside the membrane separation assembly; the aerobic denitrification sludge undergoes nitrogen removal by denitrification inside the membrane separation assembly; wastewater inside and outside the membrane separation assembly is communicated; and the side wall of the membrane separation assembly adopts a separation membrane and the bottom of the membrane separation assembly doesn't adopt the separation membrane. By the use of the membrane separation assembly, the nitrification sludge and the aerobic denitrification sludge in the reactor are separated from each other. Thus, sludge plays its role in a respective independent space, not interfering with each other. Blending and intercommunication of wastewater composition are realized. In addition, different dissolved oxygen environments can be provided, and synchronous nitrification and denitrification efficiency is raised.
Description
Technical field
The invention belongs to field of waste water treatment, relate in particular to a kind for the treatment of process of ammonia-containing water.
Background technology
Every day, because of its production technology characteristic, is discharged a large amount of ammonia-containing water by Chemical Manufacture enterprise.If directly discharged, can body eutrophication be caused, algal blooms, not only reduce water body ornamental value, and make hydrobiont hypoxia death.Some algae protein toxin also can make people poisoning through food chain, the serious harm mankind and biological existence.For this reason, how cost-effectively the ammonia nitrogen removed in waste water becomes problem demanding prompt solution.
Biological denitrificaion is one of comparatively cost-effective method removing nitrate pollution from waste water, generally comprises nitrifying process and denitrification process.Nitrifying process is NO by nitrifier by mineralized nitrogen
2 -and NO
3 -reaction process.Denitrification process is under anaerobic or hypoxia condition, NO
3 -and NO
2 -be converted into the process of gaseous matter by micro-reduction, need in reaction process using organic carbon as carbon source and the energy.No matter be traditional denitrification process or novel denitrification process, if be responsible for microbial host nitrifier and the denitrifying bacteria of denitrogenation.In actual applications, due to the difference of two kinds of thalli growth environment, be generally nitrifying process and denitrification process are separated, as traditional A/O, A
2, there is technique tediously long in/O technique, sewage treatment structure floor space is large, many drawbacks such as investment and working cost height.
Synchronous nitration denitrification denitrogenation is novel process nitration reaction and anti-nitration reaction carried out in same reactor inter-sync, not only overcome the deficiency that traditional technology nitrification and denitrification process is carried out or carried out in turn in same reactor in two different reactors, and in reduction energy consumption and material consumption etc., there is outstanding advantage.Such as, anti-nitration reaction equipment can be reduced, save capital cost; The alkali that denitrification process produces in part and the acid that produces of nitrifying process, can reduce the consumption of alkali lye, can effectively keep pH in reactor to stablize.Therefore, synchronous nitration denitrification denitrogenation process, has become the study hotspot of water treatment field.
Geng Jinju etc. utilize aerobic denitrifying bacteria group and the denitrogenation of Autotrophic nitrification flora composition (application and environmental organism journal, 2002,8 (1): 78-82), although have good ammonia nitrogen removal ability, impact resistance is more weak, and the ammonia nitrogen in high density higher than 300mg/L can suppress the growth of thalline, and when ammonia nitrogen concentration is higher than 200mg/L, after denitrogenation, ammonia nitrogen residual volume is more, synchronously not enduring high-concentration organic carbon, and the organic carbon control of the concentration thalli growth of 500mg/L also reduces denitrification effect; All kinds of microbial culture in this combination flora and growth conditions inconsistent, a kind of when playing function another kind be but in holddown, cause inharmonious each other, biological denitrificaion time lengthening, cost increases, and nitric efficiency is affected.
CN200910188109.1 discloses the method for a kind of synchronous nitration and denitrification process containing ammonia sewage, and first this method cultivates nitrogen removal granule sludge, then adopts the process of synchronous nitration and denitrification process containing ammonia sewage with this nitrogen removal granule sludge; This method is separation screening aerobic denitrifying bacteria from enrichment flora, then carries out domestication to it and cultivates, then be inoculated in nitrifying granular activated sludge and carry out nitrogen removal granule sludge cultivation; The nitrogen removal granule sludge of having tamed can be obtained when ammonia nitrogen and nitrogen removal rate reach more than 50%.This invention can complete nitration denitrification process in same reactor, although part solves traditional technology Problems existing, and, due to the difference of thalline, the operation that direct combination treatment waste water can not be steady in a long-term, the denitrification effect of long-term disposal is unsatisfactory.
Although the research of relative synchronous nitration denitrification has had larger development, the deficiencies such as it is less that but ubiquity load, and clearance is on the low side, fluctuation of service, can not effective Ammonia-Containing Wastewater Treatment, and some technique run does not consider the removal problem of total nitrogen.Which greatly limits development and the industrial application of synchronous nitration and denitrification technique.Therefore, how better to provide suitable growth conditions, ensure that nitrification and denitrification can efficiently carry out, make the operation of synchronous nitration and denitrification long-term stability, to the process accelerating the application of synchronous nitration denitrification denitrogenation process industry, there is positive effect.
Summary of the invention
The invention provides a kind for the treatment of process of ammonia-containing water.The present invention utilizes membrane separation assemblies the nitrifying sludge in reactor and aerobic denitrification mud to be kept apart, make mud at respective space behavior separately, do not interfere with each other to each other, waste component is then realize blended and intercommunication, and different dissolved oxygen environment can be provided, improve the efficiency of synchronous nitration and denitrification.
The treatment process of ammonia-containing water of the present invention, comprise following content: nitrifying sludge and aerobic denitrification mud are joined in the bio-reactor with built-in membrane separation assemblies, nitrifying sludge carries out nitration reaction in membrane separation assemblies external region, aerobic denitrification mud carries out denitrification denitrogenation in membrane separation assemblies inside, the waste water intercommunication of exterior domain in membrane separation assemblies, the sidewall of membrane separation assemblies adopts separatory membrane, and bottom does not adopt separatory membrane.
In the present invention, the material of membrane separation assemblies can adopt the various film with stalling characteristic, preferably adopts ceramic separation film, and film hole diameter is 0.05 ~ 0.5 μm.According to practical situation, design membrane separation assemblies is 1:2 ~ 1:6 with the effective volume ratio of bio-reactor, and diameter is than being 1:2 ~ 4:5.Membrane separation assemblies only has sidewall to adopt separatory membrane, bottom does not adopt separatory membrane, both can reduce the membrane area that gas enters denitrification zone, and increase gas in the residence time of nitrification zone simultaneously, make aerobic denitrifying bacteria play nitrogen removal performance under hypoxia condition preferably.Reactor is given prominence in membrane separation assemblies upper end, and the sidewall of protuberance sets out the mouth of a river, and water outlet establishes separatory membrane, ensures in water outlet not containing suspended substance.Agitator is established in membrane separation assemblies inside, realizes the back-mixing of membrane separation assemblies inner counter nitrifying sludge.
In the present invention, bio-reactor can be the bio-aeration reactor that aerating system is established in bottom, also can be bio-aeration pool.Other operational condition of bio-reactor processes the nitrifying sludge of waste water and the condition control of denitrification mud routinely.The determinator of culture system dissolved oxygen content can be set, adjust the oxygen concn in aeration as required, to obtain good effect.There is provided pH electrode to detect, so that by external source adds acid, alkali realizes system pH control simultaneously.Temperature controls as inner coil pipe type of heating or maintains required temperature at reactor outer setting temperature control chuck.
In the present invention, nitrifying sludge is nitrifying granular activated sludge, can be nitre nitrogen and/or nitrite nitrogen by mineralized nitrogen; Aerobic denitrification mud is aerobic denitrification particle sludge, and the nitre nitrogen that mineralized nitrogen can be become and/or nitrite nitrogen change into nitrogen.In the process of actual waste water process, the sludge concentration controlling nitrifying sludge is 2.0 ~ 8.0g/L, and the sludge concentration of aerobic denitrification mud is 1.0 ~ 5.0g/L.
In the present invention, ammonia-containing water is the sewage containing COD and ammonia nitrogen of all applicable Biochemical method, and ammonia nitrogen concentration is generally 100 ~ 1000mg/L.Adopt batch water inlet or a continuum micromeehanics mode, take continuum micromeehanics mode to carry out biological denitrificaion process, hydraulic detention time is less than 24h, is generally 8 ~ 24 hours.When running into treatment effect appearance fluctuation, additional nitration and/or denitrification strengthening microbial inoculum can be distinguished, keep stable synchronous nitration denitrification denitrogenation effect.
In the present invention, the nutritive substance needed for sludge treatment waste water can be added, to improve its reactive behavior.The proportioning of nutritive substance is: Fe
2+concentration is 0.01 ~ 0.06g/L, K
+concentration is 0.05 ~ 0.5g/L, Ca
2+concentration is 0.01 ~ 0.1g/L, Mg
2+concentration is 0.05 ~ 0.5g/L; PH value is 6.5 ~ 7.5.
In the present invention, be that 3:1 ~ 10:1 adds organic carbon source according to carbon-nitrogen mass ratio, organic carbon source can be Soduxin, sodium acetate, methyl alcohol, glucose and cellulosic hydrolysate etc.With batch or continuous mode supplement organic carbon source, preferably carry out stream according to the spending rate of organic carbon source and add, to reduce the impact of organic carbon source on nitrifying sludge.
In the inventive method, the treatment condition of membrane separation assemblies external region adopt the condition with nitrifying sludge conditional likelihood, and as temperature is generally 20 DEG C ~ 40 DEG C, pH value is generally 6 ~ 9, and dissolved oxygen concentration is generally 1 ~ 5mg/L etc.In order to realize effective back-mixing of membrane separation assemblies external region, maintain aeration rate constant.When fluctuation appears in denitrification space dissolved oxygen concentration, by regulating the oxygen concn in aeration, to ensure that membrane separation assemblies external region dissolved oxygen concentration is at 1 ~ 5mg/L.
Compared with prior art, the present invention has following outstanding feature:
1, utilize membrane separation assemblies that the nitrifying sludge in reactor and aerobic denitrification mud are kept apart Ammonia-Containing Wastewater Treatment, make nitrifying sludge and denitrification mud at space behavior independent separately, waste component is then realize blended and intercommunication, set up nitrifying sludge and denitrification mud cooperation and the non-interfering stable system for handling of iuntercellular, and different dissolved oxygen environment can be provided, make the two can grow under dissolved oxygen conditions suitable separately, improve the efficiency of synchronous nitration and denitrification.
2, nitrifier is different with the demand of aerobic denitrifying bacteria to dissolved oxygen, although aerobic denitrifying bacteria has oxygen-resistant ability, under the condition of hypoxemia, its nitrogen removal performance is higher, is therefore directly mixed by two kinds of bacterium and there is drawback.The present invention carries out aeration in the external region of membrane separation assemblies, due to the acting in conjunction of nitrifying sludge, separatory membrane, aeration and stirring, in membrane separation assemblies, exterior domain can form different dissolved oxygen concentrations, the dissolved oxygen concentration of external region, higher than interior region, is conducive to aerobic denitrification mud and plays nitrogen removal performance under the hypoxia condition be suitable for.With two kinds of direct mixed phase ratios of bacterium, the present invention can make nitrifier and denitrifying bacteria grow under dissolved oxygen conditions suitable separately, effectively improves the denitrification activity of nitrifier and denitrifying bacteria, improves the nitric efficiency of synchronous nitration and denitrification.
3, nitrifier utilizes the ammonia nitrogen in waste water to carry out nitration reaction, and the nitre nitrogen of generation and/or nitrite nitrogen can enter the inner nutritive substance as aerobic denitrifying bacteria of membrane separation assemblies, and nitre nitrogen and/or nitrite nitrogen are changed into gas and constantly discharges by aerobic denitrifying bacteria.Along with the carrying out of aerobic denitrification, nitre nitrogen and/or nitrite nitrogen can enter the needs that membrane separation assemblies inside meets aerobic denitrifying bacteria; Simultaneously due to the reduction of product inhibition, contribute to the process and the effect that improve nitration reaction, the two complements each other and promotes, realizes the efficient removal of total nitrogen.
4, along with the carrying out of nitration reaction, need to add the pH that alkali lye maintains suitable growth, and the alkali that denitrification process produces in part and the acid that produces of nitrifying process, can reduce the consumption of alkali lye, pH in reactor effectively can be kept to stablize, meet the requirement of energy-saving and emission-reduction.
Accompanying drawing explanation
Fig. 1 is the structural representation of bio-reactor of the present invention;
Wherein: 1-bio-reactor, 2-membrane separation assemblies, 3-nitrification zone, 4-aerobic denitrification district, 5-aerating system, 6-agitator, 7-water-in, 8-fluid infusion mouth, 9-mends carbon mouth, 10-pneumatic outlet, 11-nitrifying sludge row mouth, 12-denitrification mud row mouth, 13-water outlet.
Embodiment
The present invention utilizes the technical process of membrane separation assemblies Ammonia-Containing Wastewater Treatment as shown in Figure 1.Arrange membrane separation assemblies 2 in bio-reactor 1, the sidewall of membrane separation assemblies adopts separatory membrane, and bottom does not adopt separatory membrane.Membrane separation assemblies outside is nitrification zone 3, and inside is aerobic denitrification zone 4.Membrane separation assemblies adopts ceramic separation film, and film hole diameter is 0.05 μm ~ 0.5 μm.Membrane separation assemblies is 1:2 ~ 1:6 with the effective volume ratio of bio-reactor, and diameter is than being 1:2 ~ 4:5.Reactor is given prominence in membrane separation assemblies upper end, and the sidewall of protuberance sets out the mouth of a river 13, and water outlet establishes separatory membrane, ensures in water outlet not containing suspended substance.Establish aerating system 5 bottom bio-reactor, realize the back-mixing of nitrification zone and the oxygen needed for nitrification and denitrification is provided.Agitator 6 is established in membrane separation assemblies inside, realizes the abundant back-mixing of membrane separation assemblies inner counter nitrifying sludge.
First nitrifying sludge and aerobic denitrification mud are joined respectively nitrification zone 3 and the aerobic denitrification zone 4 of bio-reactor.Then to be added in bio-reactor by ammonia-containing water by water-in 7 and process, nitrifying sludge carries out nitration reaction in nitrification zone, and aerobic denitrification mud carries out denitrogenation in denitrification zone, and the waste water composition inside and outside membrane separation assemblies is blended with intercommunication.PH value in detecting processing system, regulates pH to 6.0 ~ 9.0 of waste water by fluid infusion mouth 8 simultaneously.In treating processes, by mending carbon mouth 9, organic carbon source and course is added in membrane separation assemblies.The gas that aerobic denitrification and aeration produce is discharged by pneumatic outlet 10.When sludge excess, by mud discharging mouth 11 and 12, nitrifier and aerobic denitrifying bacteria are discharged a part.If processed continuously, processed waste water is discharged by water outlet 13.
In the present invention, nitrifier is different with required nutritive substance with the growth conditions of aerobic denitrifying bacteria.Mineralized nitrogen in waste water is become nitre nitrogen and/or nitrite nitrogen by nitrifier, the nitre nitrogen produced and/or nitrite nitrogen can enter the inner substrate as aerobic denitrifying bacteria of membrane separation assemblies, nitre nitrogen and/or nitrite nitrogen are changed into gas, because the bodily form is comparatively large, tunicle retains mud, realize independent role, weaken different iuntercellular ecological impact.
Below by embodiment, the present invention is described in further details.But therefore do not limit the present invention.
Embodiment 1
Adopt the system for handling shown in Fig. 1 of the present invention.The effective volume of bio-reactor is 20L, and reactor adopts synthetic glass, is provided with temperature control disk pipe in reactor, and the controller such as pH, dissolved oxygen.Reactor bottom establishes aerator, can realize the back-mixing of outside culture system and the supply of oxygen.The effective volume of membrane separation assemblies is 10L, and adopt ceramic separation film, film hole diameter is 0.2 μm.Membrane separation assemblies is 3:5 with the diameter ratio of bio-reactor.Agitator is established in bio-reactor membrane separation assemblies inside, to realize the back-mixing of internal system.
First nitrifying sludge and aerobic denitrification mud are joined the nitrification zone of bio-reactor and aerobic denitrification zone respectively, then by water-in, ammonia-containing water is added in bio-reactor, the sludge concentration controlling nitrifying sludge is 3.0 ~ 4.0g/L, and the sludge concentration of aerobic denitrification mud is 2.0 ~ 3.0g/L.Adopt continuum micromeehanics, ammonia nitrogen concentration is 400mg/L, and hydraulic detention time is 12h.
In wastewater treatment process, add nitrifying sludge and the nutritive substance needed for aerobic denitrification sludge treatment waste water, to improve its reactive behavior.The proportioning of nutritive substance is: Fe
2+concentration is 0.05g/L, K
+concentration is 0.1g/L, Ca
2+concentration is 0.05g/L, Mg
2+concentration is 0.5g/L; PH value is 7.5.
PH value in detecting processing system simultaneously, regulates the pH to 7.5 of waste water.Temperature controls as inner coil pipe type of heating, and control temperature is 30 DEG C.The dissolved oxygen concentration being controlled nitrification zone by dissolved oxygen control instrument is 2.0 ~ 3.0mg/L.
Organic carbon source adopts methyl alcohol, and carbon-nitrogen mass ratio is 5:1, carries out stream add according to the spending rate of organic carbon source.When mud growth is superfluous, exceedes required sludge concentration, by mud discharging mouth, mud is discharged a part.Processed waste water is discharged by water outlet.
Run after 15 days, in water outlet, ammonia nitrogen concentration is lower than 5mg/L, and ammonia nitrogen removal frank can reach more than 98.8%.Total nitrogen concentration is less than 30mg/L, and nitrogen removal rate is greater than 92.5%.COD is less than 50mg/L, and there do not have while the supply of guarantee organic carbon source to be excessive, and water outlet COD can not be caused to increase.Result is as shown in table 1.
Embodiment 2
Adopt the flow process shown in Fig. 1 of the present invention.The effective volume of bio-reactor is 20L, and reactor adopts synthetic glass, is provided with temperature control disk pipe in reactor, and the controller such as pH, dissolved oxygen.Reactor bottom establishes aerator, can realize the back-mixing of outside culture system and the supply of oxygen.The effective volume of membrane separation assemblies is 10L, and adopt ceramic separation film, film hole diameter is 0.5 μm.Membrane separation assemblies is 4:5 with the diameter ratio of bio-reactor.Agitator is established in membrane separation assemblies inside, to realize the back-mixing of internal system.
Nitrifying sludge and aerobic denitrification mud are mud granule, first nitrifying sludge particle and aerobic denitrification mud granule are joined the nitrification zone of bio-reactor and aerobic denitrification zone respectively, then by water-in, ammonia-containing water is added in bio-reactor, the sludge concentration controlling nitrifying sludge is 3.0 ~ 4.0g/L, and the sludge concentration of aerobic denitrification mud is 2.0 ~ 3.0g/L.Adopt continuum micromeehanics, ammonia nitrogen concentration is 800mg/L, and hydraulic detention time is 18h.
In wastewater treatment process, add nitrifying sludge and the nutritive substance needed for aerobic denitrification sludge treatment waste water, to improve its reactive behavior.The proportioning of nutritive substance is: Fe
2+concentration is 0.01g/L, K
+concentration is 0.5g/L, Ca
2+concentration is 0.1g/L, Mg
2+concentration is 0.05g/L; PH value is 7.0.
PH value in detecting processing system simultaneously, regulates the pH to 8.0 of waste water.Temperature controls as inner coil pipe type of heating, and control temperature is 35 DEG C.The dissolved oxygen concentration being controlled nitrification zone by dissolved oxygen control instrument is 1.0 ~ 2.0mg/L.
Organic carbon source adopts methyl alcohol, and carbon-nitrogen mass ratio is 4:1, carries out stream add according to the spending rate of organic carbon source.When mud growth is superfluous, exceedes required sludge concentration, by mud discharging mouth, mud is discharged a part.Processed waste water is discharged by water outlet.
Run after 15 days, in water outlet, ammonia nitrogen concentration is lower than 5mg/L, and ammonia nitrogen removal frank reaches more than 99.4%.Total nitrogen concentration is lower than 66mg/L, and nitrogen removal rate is greater than 91.8%.COD concentration is less than 40mg/L, and there do not have while the supply of guarantee organic carbon source to be excessive, and water outlet COD can not be caused to increase.Result is as shown in table 1.
Comparative example 1
Adopt the reactor identical with embodiment 1 and processing condition, do not adopt membrane separation assemblies, directly nitrifying sludge and aerobic denitrification mud are added in bio-reactor.Run after 15 days, in water outlet, ammonia nitrogen concentration is lower than 20mg/L, and ammonia nitrogen removal frank is 95%.Nitre nitrogen concentration is 21mg/L, and nitrite nitrogen concentration is 42 mg/L, and total nitrogen concentration is about 80mg/L, and nitrogen removal rate is 80%.COD concentration is about 150mg/L, because nitre nitrogen and nitrite nitrogen have accumulation, therefore causes the accumulation of COD.Result is as shown in table 1.
Comparative example 2
Adopt the reactor identical with embodiment 1 and processing condition, do not adopt membrane separation assemblies, first nitrifying sludge is added reactor, run 5 days after ammonia nitrogen removal is stable, then aerobic denitrification mud is added in membrane separation assemblies.Run after 15 days, in water outlet, ammonia nitrogen concentration is lower than 15mg/L, and ammonia nitrogen removal frank is 96.3%.Nitre nitrogen concentration is 17mg/L, and nitrite nitrogen concentration is 40mg/L, and total nitrogen concentration is about 70mg/L, and nitrogen removal rate is 82.5%.COD concentration is about 120mg/L, because nitre nitrogen and nitrite nitrogen have accumulation, therefore causes the accumulation of COD.Result is as shown in table 1.
The result of table 1 embodiment and comparative example
From table 1, although the ammonia nitrogen removal frank of comparative example is higher, nitrogen removal rate is lower, the removal effect of direct mixed influence total nitrogen.
Claims (11)
1. the treatment process of an ammonia-containing water, it is characterized in that comprising following content: nitrifying sludge and aerobic denitrification mud are joined in the bio-reactor with built-in membrane separation assemblies, nitrifying sludge carries out nitration reaction in membrane separation assemblies external region, aerobic denitrification mud carries out denitrification denitrogenation in membrane separation assemblies inside, the waste water intercommunication of exterior domain in membrane separation assemblies, the sidewall of membrane separation assemblies adopts separatory membrane, and bottom does not adopt separatory membrane.
2. method according to claim 1, is characterized in that: membrane separation assemblies adopts ceramic separation film, and film hole diameter is 0.05 ~ 0.5 μm.
3. method according to claim 1 and 2, is characterized in that: membrane separation assemblies is 1:2 ~ 1:6 with the effective volume ratio of bio-reactor, and diameter is than being 1:2 ~ 4:5.
4. method according to claim 1 and 2, is characterized in that: reactor is given prominence in membrane separation assemblies upper end, and the sidewall of protuberance sets out the mouth of a river, and water outlet establishes separatory membrane, ensures in water outlet not containing suspended substance.
5. method according to claim 1 and 2, is characterized in that: membrane separation assemblies inside is established agitator or passed into nitrogen aeration, realizes abundant back-mixing.
6. method according to claim 1, is characterized in that: nitrifying sludge and aerobic denitrification mud are granule sludge.
7. the method according to claim 1 or 6, is characterized in that: the sludge concentration controlling nitrifying sludge is 2.0 ~ 8.0g/L, and the sludge concentration of aerobic denitrification mud is 1.0 ~ 5.0g/L.
8. method according to claim 1, it is characterized in that: ammonia-containing water is the waste water containing COD and ammonia nitrogen, and ammonia nitrogen concentration is 100 ~ 1000mg/L, adopt batch water inlet or a continuum micromeehanics mode, adopt continuum micromeehanics mode, hydraulic detention time is 8 ~ 24 hours.
9. the method according to claim 1 or 8, is characterized in that: add the nutritive substance needed for sludge treatment ammonia-containing water, and the proportioning of nutritive substance is: Fe
2+concentration is 0.01 ~ 0.06g/L, K
+concentration is 0.05 ~ 0.5g/L, Ca
2+concentration is 0.01 ~ 0.1g/L, Mg
2+concentration is 0.05 ~ 0.5g/L; PH value is 6.5 ~ 7.5.
10. method according to claim 1, it is characterized in that: be that 3:1 ~ 10:1 adds organic carbon source according to carbon-nitrogen mass ratio, organic carbon source is Soduxin, sodium acetate, methyl alcohol, glucose or cellulosic hydrolysate, with batch or continuous mode supplement organic carbon source.
11. methods according to claim 1, is characterized in that: the treatment condition of membrane separation assemblies external region are: control temperature is 20 ~ 40 DEG C, and pH value is 6 ~ 9, and dissolved oxygen concentration is 1 ~ 5mg/L; Maintenance aeration rate is constant, by controlling the oxygen concn in aeration, to ensure that membrane separation assemblies external region dissolved oxygen concentration is at 1 ~ 5mg/L.
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| CN107585926A (en) * | 2017-10-31 | 2018-01-16 | 科瑞斯众（天津）科技有限公司 | A kind of sewage water denitrification processing unit |
| CN111285478A (en) * | 2020-03-27 | 2020-06-16 | 乐山师范学院 | Sewage treatment device system and method thereof |
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| CN101234815A (en) * | 2008-02-05 | 2008-08-06 | 中国科学院沈阳应用生态研究所 | Membrane bioreactor capable of realizing synchronous nitration denitrification denitrogenation function |
| CN102010061A (en) * | 2010-10-28 | 2011-04-13 | 广州大学 | Nitrification and denitrification sewage treatment device and system |
| CN102372362A (en) * | 2011-09-30 | 2012-03-14 | 东北林业大学 | Integrated biomembrane and granule sludge coupling reactor and method for synchronously removing nitrogen and phosphorus from sewage |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101234815A (en) * | 2008-02-05 | 2008-08-06 | 中国科学院沈阳应用生态研究所 | Membrane bioreactor capable of realizing synchronous nitration denitrification denitrogenation function |
| CN102010061A (en) * | 2010-10-28 | 2011-04-13 | 广州大学 | Nitrification and denitrification sewage treatment device and system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107585926A (en) * | 2017-10-31 | 2018-01-16 | 科瑞斯众（天津）科技有限公司 | A kind of sewage water denitrification processing unit |
| CN111285478A (en) * | 2020-03-27 | 2020-06-16 | 乐山师范学院 | Sewage treatment device system and method thereof |
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