CN104609566B - The method of synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment - Google Patents

The method of synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment Download PDF

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CN104609566B
CN104609566B CN201310537906.2A CN201310537906A CN104609566B CN 104609566 B CN104609566 B CN 104609566B CN 201310537906 A CN201310537906 A CN 201310537906A CN 104609566 B CN104609566 B CN 104609566B
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membrane separation
separation assemblies
denitrification
sludge
concentration
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CN104609566A (en
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赵磊
李宝忠
孙丹凤
张鹏
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China Petroleum and Chemical Corp
Sinopec Fushun Research Institute of Petroleum and Petrochemicals
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China Petroleum and Chemical Corp
Sinopec Fushun Research Institute of Petroleum and Petrochemicals
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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

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  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

The present invention provides a kind of method of synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment, including following content: nitrifying sludge and denitrification mud are joined in the bioreactor with built-in membrane separation assemblies, nitrifying sludge carries out nitration reaction at the interior zone of membrane separation assemblies, denitrification mud carries out denitrification denitrogenation in the perimeter of membrane separation assemblies, the waste water intercommunication of exterior domain in membrane separation assemblies；Ammonia-containing water initially enters the interior zone of membrane separation assemblies, realizes back-mixing by aerating system, is then passed through the perimeter of membrane separation assemblies, after the outlet that arranges through perimeter flow out.The present invention utilizes membrane separation assemblies the nitrifying sludge in reactor and denitrification mud to be kept apart, make mud at the most individually space behavior, it does not interfere with each other to each other, waste component is then to realize being blended and intercommunication, and different dissolved oxygen environment can be provided, improve the efficiency of synchronous nitration and denitrification.

Description

The method of synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment
Technical field
The invention belongs to field of waste water treatment, a kind of method being specifically related to synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment.
Background technology
A large amount of ammonia-containing waters discharge because of its production technology characteristic, every day in Chemical Manufacture enterprise.If directly discharged, body eutrophication, algal blooms can be caused, not only reducing water body ornamental value, and making aquatile hypoxia death.Some algae protein toxin also can make people be poisoned through food chain, the serious harm mankind and biological existence.To this end, the ammonia nitrogen removed the most cost-effectively in waste water has become problem demanding prompt solution.
Biological denitrificaion is one of relatively inexpensive effective method removing nitrate pollution from waste water, generally comprises nitrifying process and denitrification process.Nitrifying process is to be NO by nitrifier by mineralized nitrogen2 -And NO3 -Course of reaction.Denitrification process is under anaerobic or hypoxia condition, NO3 -And NO2 -It is converted into the process of gaseous matter by micro-reduction, course of reaction needs using organic carbon as carbon source and the energy.No matter being tradition denitrification process or novel denitrification process, the microorganism being responsible for denitrogenation is mainly nitrifier and denitrifying bacterium.In actual applications, due to the difference of two kinds of thalli growth environment, it is usually and nitrifying process and denitrification process is separated, such as traditional A/O, A2, there is technique tediously long in/O technique, sewage treatment structure floor space is big, investment and many drawbacks such as operating cost is high.
Synchronous nitration denitrification denitrogenation refers to the novel process that nitration reaction and anti-nitration reaction are carried out in same reactor inter-sync, not only overcome the deficiency that traditional handicraft nitrification and denitrification process carries out in two different reactors or sequentially carries out in same reactor, and reducing the aspect such as energy consumption and material consumption, there is prominent advantage.For example, it is possible to reduce anti-nitration reaction equipment, save capital cost；The alkali that denitrification process produces can partly neutralize the acid that nitrifying process produces, and reduces the consumption of alkali liquor, can effectively keep pH in reactor stable.Therefore, synchronous nitration denitrification denitrogenation process, have become as the study hotspot of water treatment field.
Geng Jinju etc. utilize aerobic denitrifying bacteria group and Autotrophic nitrification flora composition denitrogenation (application and environmental organism journal, 2002,8 (1): 78-82), although having preferable ammonia nitrogen removal ability, but impact resistance being more weak, 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, synchronizes not tolerate high concentration organic carbon, and the organic carbon control of the concentration thalli growth of 500mg/L also reduces denitrification effect；All kinds of antibacterial culturing in this combination flora are inconsistent with growth conditions, and during a kind of function, another kind is but in inhibitory state, causes the most inharmonious, biological denitrificaion time lengthening, and cost increases, and nitric efficiency is affected.
CN200910188109.1 discloses a kind of synchronous nitration and denitrification and processes the method containing ammonia sewage, and first this method cultivates nitrogen removal granule sludge, then uses synchronous nitration and denitrification process to process the sewage Han ammonia with this nitrogen removal granule sludge；This method is separation screening aerobic denitrifying bacteria from enrichment flora, then it is carried out domestication and cultivates, then is inoculated in nitrifying granular activated sludge and carries out nitrogen removal granule sludge cultivation；The nitrogen removal granule sludge 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 the problem that traditional handicraft exists, but, due to the difference of thalline, the operation that direct mixed processing waste water can not be steady in a long-term, the denitrification effect of long-term disposal is unsatisfactory.
Although synchronous nitration and denitrification has had bigger development at present, but generally there is the deficiencies such as load is less, and clearance is on the low side, fluctuation of service, it is impossible to effectively Ammonia-Containing Wastewater Treatment, and some technique being currently running does not considers the removal problem of total nitrogen.Which greatly limits development and the application of synchronous nitration and denitrification technique.Therefore, the most preferably provide suitable growth conditions, it is ensured that nitrification and denitrification can efficiently be carried out, and makes the operation that synchronous nitration and denitrification is steady in a long-term, the process accelerating the application of synchronous nitration denitrification denitrogenation process industry is had positive effect.
Summary of the invention
For the deficiencies in the prior art, the present invention provides a kind of method of synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment.The present invention utilizes membrane separation assemblies the nitrifying sludge in reactor and denitrification mud to be kept apart, make mud at the most individually space behavior, it does not interfere with each other to each other, waste component is then to realize being blended and intercommunication, and different dissolved oxygen environment can be provided, improve the efficiency of synchronous nitration and denitrification.
The method of synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment of the present invention, including following content: nitrifying sludge and denitrification mud are joined in the bioreactor with built-in membrane separation assemblies, nitrifying sludge carries out nitration reaction at the interior zone of membrane separation assemblies, denitrification mud carries out denitrification denitrogenation in the perimeter of membrane separation assemblies, the waste water intercommunication of exterior domain in membrane separation assemblies；Ammonia-containing water initially enters the interior zone of membrane separation assemblies, realizes back-mixing by aerating system, is then passed through the perimeter of membrane separation assemblies, after the outlet that arranges through perimeter flow out.
In the present invention, the material of membrane separation assemblies can use the various film with stalling characteristic, it is preferred to use ceramic separation film, and film hole diameter is 0.05～0.5 μm.According to practical situation, the effective volume of design membrane separation assemblies and bioreactor ratio is for 1:3～4:5.Membrane separation assemblies upper end highlights reactor, and ledge arranges material-feeding port and gas outlet.The outlet of membrane separation assemblies perimeter sets separation film, it is ensured that do not contain float in water outlet.Setting stirring system outside membrane separation assemblies or be passed through nitrogen, it is achieved the abundant back-mixing of membrane separation assemblies perimeter denitrification mud, nitrogen around membrane separation assemblies Stirring, or can be passed through coiled aerator by stirring system.
In the present invention, setting guide shell inside membrane separation assemblies, guide shell is hollow structure, and aerating system is aeration inside guide shell, and water inlet is positioned at inside guide shell.So outer circulation be can form at membrane separation assemblies interior zone, waste water and the more preferable back-mixing of nitrifying sludge contributed to；Simultaneously as the effusion of gas and the utilization of nitrifier, the oxygen entering denitrification zone is few, and beneficially denitrification mud plays higher nitrogen removal performance under suitable anaerobic or hypoxia condition.
In the present invention, bioreactor can be the bio-aeration reactor that bottom sets aerating system, it is also possible to be airlift bioreactor.The condition of nitrifying sludge and denitrification mud that other operating condition of bioreactor processes waste water routinely controls.The determinator of cultivating system dissolved oxygen content is set, adjusts the oxygen concentration in aeration as required, to obtain good effect.There is provided pH electrode detection, in order to add control sour, that alkali realizes system pH by external source simultaneously.Temperature controls as internal coil pipe mode of heating or arranges temperature control chuck outside reactor to maintain required temperature.
In the present invention, nitrifying sludge is preferably nitrifying granular activated sludge, can be nitrate nitrogen and/or nitrite nitrogen by mineralized nitrogen；Denitrification mud is anaerobic denitrifying granule sludge or aerobic denitrification particle sludge, nitrate nitrogen and/or nitrite nitrogen can be changed into gaseous matter.During actual waste water processes, the sludge concentration controlling nitrifying sludge is 2.0～8.0g/L, and the sludge concentration of denitrification mud is 1.0～5.0g/L.
In the present invention, ammonia-containing water be all applicable Biochemical method containing COD and the sewage of ammonia nitrogen, ammonia nitrogen concentration is generally 100 ~ 1000mg/L.Using batch water inlet or continuum micromeehanics mode, take continuum micromeehanics mode to carry out biological denitrificaion process, hydraulic detention time is generally 8～24 hours.Containing in ammonia sewage disposal process, 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 nutrient substance needed for Treatment of Sludge waste water can be added, to improve its reactivity.The proportioning of nutrient substance is: Fe2+Concentration is 0.01～0.06g/L, K+Concentration is 0.05～0.5g/L, Ca2+Concentration is 0.01～0.1g/L, Mg2+Concentration is 0.05～0.5g/L；PH value is 6.5～7.5.
In the present invention, being the organic carbon source that 3:1～10:1 adds needed for denitrification according to carbon-nitrogen mass ratio, organic carbon source can be sodium succinate, sodium acetate, methanol, glucose or cellulosic hydrolysate etc..Supplement organic carbon source with batch or continuation mode, carry out stream preferably based on the depletion rate of organic carbon source and add, to reduce the organic carbon source impact on nitrifying sludge.
In the present invention, the treatment conditions of membrane separation assemblies interior zone use the condition with nitrifying sludge conditional likelihood, and as temperature is generally 20 DEG C～40 DEG C, pH value is 6～9, and dissolved oxygen concentration is 1～5mg/L etc..In order to realize effective back-mixing of membrane separation assemblies interior zone, maintain aeration rate constant.When fluctuation occurs in denitrification space dissolved oxygen concentration, by the oxygen concentration in regulation aeration, to ensure that membrane separation assemblies interior zone dissolved oxygen concentration is 1～5mg/L.
Compared with prior art, the present invention has a feature highlighted below:
1, utilize membrane separation assemblies that the nitrifying sludge in reactor and denitrification mud are kept apart Ammonia-Containing Wastewater Treatment, make nitrifying sludge and denitrification mud at the most individually space behavior, waste component is then to realize being 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 act under the most suitable dissolved oxygen conditions, improve the efficiency of synchronous nitration and denitrification.
2, nitrifier is different to the demand of dissolved oxygen with denitrifying bacterium, although aerobic denitrifying bacteria has oxygen-resistant ability, but its nitrogen removal performance is higher under conditions of hypoxia, therefore two kinds of bacterium is directly mixed drawback.The present invention carries out aeration at the interior zone of membrane separation assemblies, owing to separating the common effect of film, nitrifying sludge, aerating system, guide shell and stirring, in membrane separation assemblies, exterior domain can form different dissolved oxygen concentrations, the dissolved oxygen concentration of perimeter plays nitrogen removal performance far below interior zone, beneficially denitrification mud under hypoxia or oxygen free condition.With two kinds of bacterium direct mixed phase ratios, the present invention can make nitrifier and denitrifying bacterium grow under the most suitable dissolved oxygen conditions, be effectively improved the denitrification activity of nitrifier and denitrifying bacterium, improve the nitric efficiency of synchronous nitration and denitrification.
3, the ammonia nitrogen during nitrifier utilizes waste water carries out nitration reaction, and the nitrate nitrogen of generation and/or nitrite nitrogen can enter the nutrient substance outside membrane separation assemblies as aerobic denitrifying bacteria, and nitrate nitrogen and/or nitrite nitrogen are changed into gas and constantly discharge by denitrifying bacterium.Carrying out along with denitrifying, nitrate nitrogen and/or nitrite nitrogen can enter the needs meeting denitrifying bacterium outside membrane separation assemblies；Simultaneously because the reduction of product inhibition, being favorably improved process and the effect of nitration reaction, the two complements each other and promotes, it is achieved that the efficient removal of total nitrogen.
4, along with the carrying out of nitration reaction, need to add alkali liquor and maintain the pH of suitable growth, and the alkali that denitrification process produces can partly neutralize the acid that nitrifying process produces, and reduces the consumption of alkali liquor, can effectively keep pH in reactor stable, meets the requirement of energy-saving and emission-reduction.
Accompanying drawing explanation
Fig. 1 is the structural representation of the inventive method bioreactor；
Wherein: 1-bioreactor, 2-membrane separation assemblies, 3-nitrification zone, 4-denitrification zone, 5-aerating system, 6-agitator or exposure nitrogen, 7-water inlet, 8-material-feeding port, 9-mends carbon mouth, 10-gas outlet, 11-nitrifying sludge row's mouth, 12-denitrification mud row's mouth, 13-outlet, 14-guide shell.
Detailed description of the invention
The technological process that the synchronous nitration and denitrification that the present invention utilizes membrane separation assemblies to realize ammonia-containing water processes is as shown in Figure 1.Arranging membrane separation assemblies 2 in bioreactor 1, membrane separation assemblies is internal is nitrification zone 3, and outside is denitrification zone 4.Membrane separation assemblies uses ceramic separation film, and film hole diameter is 0.05 μm～0.5 μm.The effective volume of membrane separation assemblies and bioreactor is than for 1:3～4:5.Membrane separation assemblies upper end highlights reactor, and ledge arranges material-feeding port and gas outlet.The outlet of membrane separation assemblies perimeter sets separation film, it is ensured that do not contain float in water outlet.Setting stirring system outside membrane separation assemblies or be passed through nitrogen, it is achieved the abundant back-mixing of membrane separation assemblies perimeter denitrification mud, nitrogen around membrane separation assemblies Stirring, or can be passed through coiled aerator by stirring system.Aerating system 5 is set, it is achieved the back-mixing of nitrification zone the oxygen needed for nitrification and denitrification is provided bottom membrane separation assemblies.Membrane separation assemblies perimeter is passed through nitrogen, it is achieved the abundant back-mixing of denitrification region mud.Setting guide shell inside membrane separation assemblies, guide shell is hollow structure, and aerating system is aeration inside guide shell, and water inlet is positioned at inside guide shell.Aerating system uses aeration plate, and aeration outlet is higher than guide shell lower end.
First nitrifying sludge and denitrification mud are added separately to nitrification zone 3 and the denitrification zone 4 of bioreactor.Then being added in bioreactor by ammonia-containing water by water inlet 7 and process, nitrifying sludge carries out nitration reaction in nitrification zone, and denitrification mud carries out denitrogenation in denitrification zone, and the waste water composition inside and outside membrane separation assemblies is to be blended and intercommunication.PH value in detection processing system, regulates the pH to 6.0～9.0 of waste water by material-feeding port 8 simultaneously.In processing procedure, by mending carbon mouth 9, organic carbon source stream is added in bioreactor.The gas that denitrification and aeration produce is discharged by gas outlet 10.When sludge excess, by mud discharging mouth 11 and 12, nitrifier and denitrifying bacterium are discharged a part.If carried out continuous processing, processed waste water is discharged by outlet 13.
In the present invention, nitrifier is different with required nutrient substance with the growth conditions of denitrifying bacterium.Nitrifier utilizes the ammonia nitrogen in waste water to carry out nitration reaction, and the nitrate nitrogen of generation and/or nitrite nitrogen can enter the nutrient substance outside membrane separation assemblies as denitrifying bacterium, and nitrate nitrogen and/or nitrite nitrogen are changed into gas and constantly discharge by denitrifying bacterium.Mud is rejected by owing to the bodily form is relatively big, it is achieved independent role, weakens different iuntercellular ecology influence.Simultaneously because the effect of concentration difference, carrying out along with denitrifying, nitrate nitrogen and/or nitrite nitrogen can enter the needs meeting denitrifying bacterium outside membrane separation assemblies；Simultaneously because the reduction of product inhibition, being favorably improved process and the effect of nitration reaction, the two complements each other and promotes, it is achieved that the efficient removal of total nitrogen.
Below by embodiment, the present invention is described in further details.But it is not so limited the present invention.
Embodiment 1
Use the reactor shown in Fig. 1 of the present invention.The effective volume of bioreactor is 20L, and reactor uses lucite, has temperature control disk pipe, and the controller such as pH, dissolved oxygen in reactor.The effective volume of membrane separation assemblies is 10L, uses ceramic separation film, and film hole diameter is 0.2 μm.Aerating system is set, it is achieved the back-mixing of nitrification zone the oxygen needed for nitrification and denitrification is provided bottom membrane separation assemblies.Membrane separation assemblies perimeter is passed through nitrogen, it is achieved the abundant back-mixing of denitrification region mud.Setting guide shell inside membrane separation assemblies, guide shell is hollow structure, and aerating system is aeration inside guide shell, and water inlet is positioned at inside guide shell.Aerating system uses aeration plate, and aeration outlet is higher than guide shell lower end.
First nitrifying sludge and aerobic denitrification mud are added separately to the nitrification zone of bioreactor and aerobic denitrification zone, then by water inlet, ammonia-containing water is added in membrane separation assemblies guide shell, 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.Using continuum micromeehanics, ammonia nitrogen concentration is 400mg/L, and hydraulic detention time is 12h.
In wastewater treatment process, add the nutrient substance needed for nitrifying sludge and aerobic denitrification Treatment of Sludge waste water, to improve its reactivity.The proportioning of nutrient substance is: Fe2+Concentration is 0.05g/L, K+Concentration is 0.1g/L, Ca2+Concentration is 0.05g/L, Mg2+Concentration is 0.5g/L；PH value is 7.5.
PH value in detection processing system, the pH to 7.5 of regulation waste water simultaneously.Temperature controls to be internal coil pipe mode of heating, and controlling temperature is 30 DEG C.Owing to setting guide shell in reactor, guide shell can form outer circulation at membrane separation assemblies interior zone, causes the dissolved oxygen of zones of different to be slightly different, and the dissolved oxygen concentration therefore controlling guide shell inside region is 2.0～3.0mg/L.
Organic carbon source uses methanol, and carbon-nitrogen mass ratio is 5:1, carries out stream according to the depletion rate of organic carbon source and adds.When mud growth is superfluous, exceed required sludge concentration, by mud discharging mouth, mud can be discharged a part.Processed waste water is discharged by outlet.
After running 15 days, in water outlet, ammonia nitrogen concentration is less than 5mg/L, and ammonia nitrogen removal frank reaches more than 98.8%.Total nitrogen concentration is less than 15mg/L, and nitrogen removal rate is more than 96.3%.COD concentration is less than 50mg/L, does not has excess, be not result in that water outlet COD increases while ensureing organic carbon source supply.Result is as shown in table 1.
Embodiment 2
Use the reactor shown in Fig. 1 of the present invention.The effective volume of bioreactor is 20L, and reactor uses lucite, has temperature control disk pipe, and the controller such as pH, dissolved oxygen in reactor.The effective volume of membrane separation assemblies is 10L, uses ceramic separation film, and film hole diameter is 0.5 μm.Aerating system is set, it is achieved the back-mixing of nitrification zone the oxygen needed for nitration reaction is provided bottom membrane separation assemblies.Membrane separation assemblies perimeter is passed through nitrogen, it is achieved the abundant back-mixing of denitrification region mud.Setting guide shell inside membrane separation assemblies, guide shell is hollow structure, and aerating system is aeration inside guide shell, and water inlet is positioned at inside guide shell.Aerating system uses aeration plate, and aeration outlet is higher than guide shell lower end.
Nitrifying sludge is nitrifying granular activated sludge, and denitrification mud is anaerobic denitrifying granule sludge.First nitrifying granular activated sludge and anaerobic denitrifying granule sludge are added separately to nitrification zone and the denitrification zone of bioreactor, then by water inlet, ammonia-containing water is added in bioreactor, the sludge concentration controlling nitrifying sludge is 3.0～4.0g/L, and the sludge concentration of denitrification mud is 2.0～3.0g/L.Using continuum micromeehanics, ammonia nitrogen concentration is 800mg/L, and hydraulic detention time is 18h.
In wastewater treatment process, add the nutrient substance needed for nitrifying sludge and anaerobic denitrifying Treatment of Sludge waste water, to improve its reactivity.The proportioning of nutrient substance is: Fe2+Concentration is 0.01g/L, K+Concentration is 0.5g/L, Ca2+Concentration is 0.1g/L, Mg2+Concentration is 0.05g/L；PH value is 7.0.
PH value in detection processing system, the pH to 8.0 of regulation waste water simultaneously.Temperature controls to be internal coil pipe mode of heating, and controlling temperature is 35 DEG C.Owing to setting guide shell in reactor, guide shell can form outer circulation at membrane separation assemblies interior zone, causes the dissolved oxygen of zones of different to be slightly different, and the dissolved oxygen concentration therefore controlling guide shell inside region is 1.0～1.5mg/L.
Organic carbon source uses glucose, and carbon-nitrogen mass ratio is 4:1, carries out stream according to the depletion rate of organic carbon source and adds.When mud growth is superfluous, exceed required sludge concentration, by mud discharging mouth, mud can be discharged a part.Processed waste water is discharged by outlet.
After running 15 days, in water outlet, ammonia nitrogen concentration is less than 5mg/L, and ammonia nitrogen removal frank reaches more than 99.4%.Total nitrogen concentration is less than 40mg/L, and nitrogen removal rate is more than 94.4%.COD concentration is less than 40mg/L, does not has excess, be not result in that water outlet COD increases while ensureing organic carbon source supply.Result is as shown in table 1.
Comparative example 1
Use reactor same as in Example 1 and process conditions, do not use membrane separation assemblies, directly nitrifying sludge and aerobic denitrification mud are added in bioreactor.After running 15 days, in water outlet, ammonia nitrogen concentration is less than 20mg/L, and ammonia nitrogen removal frank is 95%.Nitrate 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, owing to nitrate nitrogen and nitrite nitrogen have accumulation, thus results in the accumulation of COD.Result is as shown in table 1.
Comparative example 2
Use reactor same as in Example 1 and process conditions, do not use 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.After running 15 days, in water outlet, ammonia nitrogen concentration is less than 15mg/L, and ammonia nitrogen removal frank is 96.3%.Nitrate 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, owing to nitrate nitrogen and nitrite nitrogen have accumulation, thus results in the accumulation of COD.Result is as shown in table 1.
Table 1 embodiment and the result of comparative example
From table 1, although the ammonia nitrogen removal frank of comparative example is higher, but nitrogen removal rate is relatively low, directly by the removal effect of nitrifier Yu denitrifying bacterium mixed influence total nitrogen.

Claims (12)

1. the method for a synchronous nitration and denitrification Ammonia-Containing Wastewater Treatment, including following content: nitrifying sludge and denitrification mud are joined in the bioreactor with built-in membrane separation assemblies, nitrifying sludge carries out nitration reaction at the interior zone of membrane separation assemblies, denitrification mud carries out denitrification denitrogenation in the perimeter of membrane separation assemblies, the waste water intercommunication of exterior domain in membrane separation assemblies；Ammonia-containing water initially enters the interior zone of membrane separation assemblies, realizes back-mixing by aerating system, is then passed through the perimeter of membrane separation assemblies, after the outlet that arranges through perimeter flow out.
Method the most according to claim 1, it is characterised in that: membrane separation assemblies uses ceramic separation film, and film hole diameter is 0.05～0.5 μm.
Method the most according to claim 1 and 2, it is characterised in that: the effective volume of membrane separation assemblies and bioreactor is than for 1:3～4:5.
Method the most according to claim 1 and 2, it is characterised in that: membrane separation assemblies upper end highlights reactor, and ledge arranges material-feeding port and gas outlet；The outlet of membrane separation assemblies perimeter sets separation film, it is ensured that do not contain float in water outlet.
Method the most according to claim 1 and 2, it is characterized in that: set stirring system outside membrane separation assemblies or be passed through nitrogen, realize the abundant back-mixing of membrane separation assemblies perimeter denitrification mud, nitrogen around membrane separation assemblies Stirring, or can be passed through coiled aerator by stirring system.
Method the most according to claim 1 and 2, it is characterised in that: setting guide shell inside membrane separation assemblies, guide shell is hollow structure, and aerating system is aeration inside guide shell, and water inlet is positioned at inside guide shell.
Method the most according to claim 1, it is characterised in that: nitrifying sludge is nitrifying granular activated sludge, and denitrification mud is anaerobic denitrifying granule sludge or aerobic denitrification particle sludge.
8. according to the method described in claim 1 or 7, it is characterised in that: the sludge concentration controlling nitrifying sludge is 2.0～8.0g/L, and the sludge concentration of denitrification mud is 1.0～5.0g/L.
Method the most according to claim 1, it is characterised in that: ammonia-containing water is the waste water containing COD and ammonia nitrogen, and ammonia nitrogen concentration is 100 ~ 1000mg/L；Using batch water inlet or continuum micromeehanics mode, take continuum micromeehanics mode, hydraulic detention time is 8～24 hours.
Method the most according to claim 1, it is characterised in that: in wastewater treatment process, adding the nutrient substance needed for Treatment of Sludge ammonia-containing water, the proportioning of nutrient substance is: Fe2+Concentration is 0.01～0.06g/L, K+Concentration is 0.05～0.5g/L, Ca2+Concentration is 0.01～0.1g/L, Mg2+Concentration is 0.05～0.5g/L；PH value is 6.5～7.5.
11. methods 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 sodium succinate, sodium acetate, methanol, glucose or cellulosic hydrolysate, supplements organic carbon source with batch or continuation mode.
12. methods according to claim 1, it is characterised in that: the treatment conditions of membrane separation assemblies interior zone are: controlling 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 concentration in aeration, to ensure that membrane separation assemblies interior zone dissolved oxygen concentration is 1～5mg/L.
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