CN1102130C - System and method for removing biologically both nitrogen and phosphorous removal in sewage and wastewater - Google Patents
System and method for removing biologically both nitrogen and phosphorous removal in sewage and wastewater Download PDFInfo
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- CN1102130C CN1102130C CN97116878A CN97116878A CN1102130C CN 1102130 C CN1102130 C CN 1102130C CN 97116878 A CN97116878 A CN 97116878A CN 97116878 A CN97116878 A CN 97116878A CN 1102130 C CN1102130 C CN 1102130C
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 175
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 89
- 238000000034 method Methods 0.000 title claims abstract description 66
- 239000002351 wastewater Substances 0.000 title claims abstract description 51
- 239000010865 sewage Substances 0.000 title claims description 16
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 title 1
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 127
- 239000011574 phosphorus Substances 0.000 claims abstract description 127
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 125
- 238000005273 aeration Methods 0.000 claims abstract description 83
- 239000010802 sludge Substances 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 230000008569 process Effects 0.000 claims abstract description 23
- 239000002699 waste material Substances 0.000 claims abstract description 14
- 239000006228 supernatant Substances 0.000 claims abstract description 13
- 239000011368 organic material Substances 0.000 claims abstract description 3
- 238000002156 mixing Methods 0.000 claims description 38
- 244000005700 microbiome Species 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 11
- 239000007787 solid Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- 238000004065 wastewater treatment Methods 0.000 claims description 8
- 230000005484 gravity Effects 0.000 claims description 6
- 230000008719 thickening Effects 0.000 claims description 6
- 238000011068 loading method Methods 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 17
- 239000000203 mixture Substances 0.000 abstract description 9
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 abstract description 4
- 238000012545 processing Methods 0.000 abstract description 3
- 229910019142 PO4 Inorganic materials 0.000 abstract 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 abstract 2
- 239000010452 phosphate Substances 0.000 abstract 2
- 238000004064 recycling Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 22
- 239000000126 substance Substances 0.000 description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 12
- 238000002474 experimental method Methods 0.000 description 12
- 239000001301 oxygen Substances 0.000 description 12
- 229910052760 oxygen Inorganic materials 0.000 description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 230000006872 improvement Effects 0.000 description 7
- 235000015097 nutrients Nutrition 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 2
- 241000976983 Anoxia Species 0.000 description 2
- 206010021143 Hypoxia Diseases 0.000 description 2
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000007953 anoxia Effects 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 150000003017 phosphorus Chemical class 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical class OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- -1 denitrification Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006194 liquid suspension Substances 0.000 description 1
- 239000010871 livestock manure Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 150000002829 nitrogen Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 239000001038 titanium pigment Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
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Classifications
-
- 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
-
- 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
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
-
- 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
- C02F3/308—Biological phosphorus removal
-
- 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)
- Biodiversity & Conservation Biology (AREA)
- Chemical & Material Sciences (AREA)
- Water Supply & Treatment (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Hydrology & Water Resources (AREA)
- Microbiology (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Analytical Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Activated Sludge Processes (AREA)
Abstract
The present invention relates to a process and apparatus for removal of both the nitrogen and the phosphorus in processing waste or dirty water. The apparatus comprises: a denitrification reactor in which water from a first settling vessel is mixed with recycled activated sludge to reduce the mixture using organic materials in the incoming waste water and to give N2 which is released into the atmosphere; an aeration reactor receiving a water/activated sludge mixture from the denitrification reactor and recycling it with further waste water and a high concentration of nitrate nitrogen to the denitrification reactor; a second settling vessel taking up the waste water/activated sludge mixture from the aeration reactor to precipitate the sludge and recycle a previously established amount of activated sludge into denitrification reactor and a phosphate separator, and a phosphate separator for separating the low nitrate nitrogen-containing activated sludge by means of a shear force in a solid-liquid system, this sludge and the supernatant component of the separator then being recycled to the aeration reactor.
Description
Technical field
The present invention relates to biological a kind of system and method except that nitrogen and phosphorus in decontaminated water and the waste water, in particular, relate to by improveing system and the technology that traditional only being used to removes the Phostrip technology of dephosphorization and make said improved technology adaptation biological sewage and wastewater treatment make it to remove organic substance and can remove nutrient substances such as denitrification, phosphorus.
Background technology
Organic sewage and waste water are handled in the dual-spectrum process of traditional activated sludge method usually, thereby organic substance is removed from sewage and waste water.But, owing in secondary treatment, nutrient substances such as the nitrogen of q.s, phosphorus are not removed, contain these a large amount of nutrient substances in the treating water and emitted from sewage and wastewater treatment plant.Therefore, this treating water is in case in the water body such as lakelet and bay of inflow sealing, the nutrient substance for the treatment of water right over there accumulates, and this accumulation of nutrient substance may cause the serious problems of sealing water body eutrophication.
In traditional sewage and wastewater treatment plant, proposed various physico-chemical processes and be used for denitrogenating, for example, control the aquatic ammoniacal nitrogen NH that will be included in the waste water by PH
3-N) outgas air desorption method in the atmosphere, with the ion-exchange techniques and the chlorine method for implanting of zeolite selectivity displacement ammonia.Also proposed a kind of method of dephosphorization, this method, becomes soluble phosphorus after the insoluble settling as the chemical substance of Tai-Ace S 150, lime and analogue and so on by input, removes the phosphorus in the waste water in final clarifying tank.But the physical chemistry treatment process of above-mentioned dephosphorization and nitrogen is being very expensive aspect the operation and maintenance expense.Therefore, in order to remove phosphorus and the nitrogen in the sewage or waste water, the main recently bioremediation that adopts, this method is more more economical than physical chemistry treatment process.
The principle of biological removal of nitrogen method is under the aerobic condition that has a large amount of dissolved oxygen (DO) to exist, ammonium ion (
) be oxidized to nitrite nitrogen (
) or nitric nitrogen
N), under anoxia condition, it is reduced into nitrogen then and from treating water, the nitrogen that is reduced into is removed then by bacterium.
In the method for said biological removal of nitrogen, for ammonium ion being oxidized to nitrite nitrogen and nitric nitrogen, need dissolved oxygen, and under this denitrogenates the anoxia condition of technology, also need to inject organic carbon source (for example, methyl alcohol) by microorganism.But the operation and maintenance expense of this method is also very high.Therefore, developed BOD (biological oxygen demand) component that a kind of use is included in the sewage or waste water and replaced the inexpensive method of methyl alcohol as organic carbon source.
Secondly, will explain hereinafter as the principle of the anaerobic-aerobic technology dephosphorization of biological phosphate-eliminating main technique.
In anaerobic jar, the microorganism of being responsible for dephosphorization absorbs the organism in the sewage or waste water and it form with PHB (gathering hydroxyl-β-butyric ester) is stored in the cell.During this time, obtain required energy by the ATP in the hydrolysis cell.In this process, the ATP in the cell is with orthophosphoric acid salt (PO
4 ----P) form discharges.Then, in aerobic jar, microbiological oxidation is stored in the more phosphorus of phosphorus amount that PHB in its cell and the cell of specific absorption from anaerobic jar give off, and is used for the resynthesis of cell.In biological secondary treatment, phosphorus is absorbed by stoichiometry, and the phosphorus amount that comprises in the cell is 1.5～2% of its dry weight.But in the aerobic treatment process after anaerobic treatment, the phosphorus amount that comprises in the cell reaches 4～8%, and is more much higher than stoichiometric amount, and this amount is 2～4 times of phosphorus content in the traditional biological secondary treatment.
According to the principle of above-mentioned biological phosphate-eliminating and nitrogen, the technology of various recommended use is arranged, especially the Phostrip process quilt is recommended as the high selection process of dephosphorization efficiency by using.
In Phostrip technology, the organism that flows in the waste water is removed in the aeration tank, and the part mud that turns back to the aeration tank from the secondary clarifying tank is stayed in the long residence time the phosphorus separator as the gravity thickening jar then.At this moment, the organism that is produced by microbial cell-Decomposition in the phosphorus separator is used as the required organism of release phosphorus.The poor phosphorus activated sludge that has discharged phosphorus in the phosphorus separator is sent into the aeration tank again, and described poor phosphorus activated sludge absorbs a large amount of phosphorus there.Then, remove the rich phosphorus supernatant liquor of rich phosphorated by chemical treatment.
But, in above-mentioned Phostrip technology, in view of not only dephosphorization but also denitrogenate, when the operational condition of aeration tank is adjusted to not only oxidation of organic compounds but also nitrogen oxide, discharges the required organism of phosphorus turned back to the phosphorus separator from the secondary clarifying tank the nitric nitrogen that mud comprised and consume.Therefore, the release of phosphorus is worsened in the phosphorus separator, the result, and the dephosphorization efficiency by using of above-mentioned Phostrip technology descends.
In order to address the above problem, the Phostrip technology of the improvement that has proposed a kind of not only dephosphorization but also denitrogenated, by only removing the organism in the aeration tank and behind the secondary clarifying tank, setting up nitrated and nitrogen rejection facility then, or by device denitrogenation jar between secondary clarifying tank and phosphorus separator, this technology can reduce the nitric nitrogen that flow in the phosphorus separator.
But preceding a kind of method need be provided with nitrated and nitrogen rejection facility in secondary clarifying tank back, and expense is increased, and owing to compare with the waste water that flows into, very low by the organic concentration in the treating water of secondary clarifying tank, must provide organic carbon source to the denitrogenation jar, for example methyl alcohol.In a kind of method in back, between secondary clarifying tank and phosphorus separator, only need the denitrogenation jar, therefore, executive cost is lower, and still, the residence time is increased to 8 hours or more, and pass through flow velocity only for about 30% from the secondary clarifying tank to the denitrogenation jar, the result, total efficient of denitrogenating reduces.
Summary of the invention
Therefore, the present invention is proposed to address the above problem, basic purpose of the present invention is to provide the system and method for a kind of biological phosphate-eliminating and nitrogen, wherein, only before the aeration tank, be provided with the denitrogenation jar, then, make blended liquid suspension mud (MLSS) nitrated and in the aeration tank, reach high nitric nitrogen concentration.Itrated MLSS is turned back in the denitrogenation jar, by all organism in the high inflow waste water of organic concentration are used as carbon source, and in the denitrogenation jar, the nitric nitrogen that is included among the MLSS is removed, therefore, the efficient of always denitrogenating of total system is further improved, as a result, dephosphorization efficiency by using is than higher by the dephosphorization efficiency by using that reduces the traditional method that flows into nitric nitrogen concentration in the phosphorus separator.
In order to achieve the above object, the invention provides a kind of Phostrip technology biological phosphate-eliminating of improvement and system of nitrogen of using, this system comprises: the denitrogenation jar, this denitrogenation jar is mixing from the waste water of one-level clarifying tank inflow and the mud that returns from the aeration tank, and by flowing into the organism in the waste water mixing liquid suspended sludge is reduced into nitrogen, then gaseous emission in atmosphere; The aeration tank, this aeration tank receives the mixing liquid suspended sludge that gives off from the denitrogenation jar, will have the mixing liquid suspended sludge of high density nitric nitrogen to turn back in the denitrogenation jar then; The secondary clarifying tank, this groove receives the mixing liquid suspended sludge that gives off from the aeration tank, makes sludge settling, and the mud with predetermined amount returns in above-mentioned the denitrogenation jar and phosphorus separator then; With the phosphorus separator, this separator is by the gravity thickening method, receives nitric nitrogen concentration mud low, that return from the secondary clarifying tank, and it is separated into the solid-liquid state, then mud in the phosphorus separator and supernatant liquor returned in the aeration tank.
To achieve these goals, the present invention further provides a kind of method of using the Phostrip technology biology of improvement in conjunction with dephosphorization and nitrogen, this method comprises: the first step mixing step, promptly the mud that will return from the aeration tank in the denitrogenation jar and mix from the effusive sewage of one-level clarifying tank is discharged into the mixing liquid suspended sludge in the aeration tank then; Second step was to remove the organism of inflow and the TKN of nitrated inflow (TKN) in the aeration tank, and the mixing liquid suspended sludge with nitrated mistake turns back in the denitrogenation jar then; The 3rd step was in the denitrogenation jar, removed nitric nitrogen by using all organism that flow in the sewage from the mixing liquid suspended sludge of nitrated mistake, had increased the efficient of denitrogenating of total system thus; The 4th step was precipitated the microorganism that grows in the aeration tank by the microorganism that separates the solid-liquid state in the secondary clarifying tank, then some mud was returned the phosphorus separator, and remaining turns back in the denitrogenation jar; The 5th step separated with the solid-liquid state and is stored in mud in the phosphorus separator, forms anaerobic condition, and then the mud of poor phosphorus and the supernatant liquor of rich phosphorus are returned in the aeration tank that is in aerobic state; The 6th step was removed phosphorus from the mud that the phosphorus separator returns by making microorganism absorb enough phosphorus in the aeration tank.
More particularly, the present invention includes the system of biological removal of nitrogen and phosphorus in a kind of sewage and the waste water treatment process, this system comprises:
The denitrogenation jar, this jar will and return mud and mix to form the mixing liquid suspended sludge from the inflow waste water of one-level clarifying tank, with the organism in the inflow waste water described mixing liquid suspended sludge will be reduced into nitrogen, then formed nitrogen will be discharged in the atmosphere;
Mixing device, this device will flow into waste water and the mud that returns from secondary clarifying tank and aeration tank mixes, and this mixing device is installed in the described denitrogenation jar;
The aeration tank, this pond receives the mixing liquid suspended sludge of discharging from the denitrogenation jar, and then that nitric nitrogen concentration is high mixing liquid suspended sludge turns back in the denitrogenation jar;
The secondary clarifying tank, this groove receives the mixing liquid suspended sludge of discharging from the aeration tank, precipitation mud wherein, the mud with predetermined amount turns back in denitrogenation jar and the phosphorus separator then; With
Phosphorus separator, this separator receive nitric nitrogen concentration mud low, that return from the secondary clarifying tank, and by the gravity thickening method it are separated into mushy stage, then mud in the phosphorus separator and supernatant liquor are turned back in the aeration tank.
In system of the present invention, preferably a kind of anoxic jar of said denitrogenation jar, this anoxic jar allow all inflow waste water of one-level clarifying tank only to be consumed in denitrification process, to improve the efficient of denitrogenating of total system.
On the other hand, the present invention also comprises the method for biological removal of nitrogen and phosphorus in a kind of sewage and the waste water treatment process, and this method comprises:
The first step, in the denitrogenation jar, will return from the aeration tank come return mud and mix from the waste discharge of one-level clarifying tank, then formed mixing liquid suspended sludge is discharged in the aeration tank;
Second step, in the aeration tank, remove the organism of inflow and the TKN (TKN) of nitrated inflow, the mixing liquid suspended sludge with nitrated mistake turns back in the denitrogenation jar then;
The 3rd step, in the denitrogenation jar, pass through to use all organism that flow in the waste water, nitric nitrogen in the mixing liquid suspended sludge of nitrated mistake is removed, increase the efficient of denitrogenating of total system thus, wherein, in the 3rd step, in the denitrogenation jar, flow into waste water and be used as and remove the required carbon source of nitric nitrogen, only allow in denitrification process, to be consumed from all waste discharges of one-level clarifying tank;
The 4th step, in the secondary clarifying tank, by the microorganism that grows in the aeration tank being separated into mushy stage and they being precipitated, then the mud of a part is returned in the phosphorus separator and with the part of remainder and return in the denitrogenation jar, wherein, in described the 3rd step and the 4th step, by handling the nitric nitrogen that in the aeration tank, generates with all organism that flow in the waste water, the nitric nitrogen that is comprised from the secondary clarifying tank turns back to mud the phosphorus separator is reduced, and the release of phosphorus just is not subjected to the influence of nitric nitrogen in the phosphorus separator like this;
The 5th step, be separated in the mud that stores with the solid-liquid state in the phosphorus separator, and formation anaerobic condition, then poor phosphorus sludge and rich phosphorus supernatant liquor are returned in the aeration tank that is in aerobic condition, wherein, in the 5th step, between residence time, cell decomposes the organism that produces and is used as the required organism of release phosphorus at predetermined mud; With
In the 6th step, remove the phosphorus in the mud of returning from the phosphorus separator by making microorganism in the aeration tank, absorb enough phosphorus.
In the method for the invention, preferably second step provide the optimum condition of microorganism growth, this condition be organic material loading speed in the scope of 0.1kg BOD/kg MLVSSd～0.3kg BOD/kg MLVSSd and the hydromechanics residence time in 4～5 hours scope.
Description of drawings
Fig. 1 is the synoptic diagram according to biological phosphate-eliminating of the present invention and nitrogen system.
Embodiment
Hereinafter the system and method for biological phosphate-eliminating and nitrogen is according to embodiments of the present invention described with reference to Fig. 1.
As shown in Figure 1, system according to the present invention comprises: denitrogenation jar 2, this denitrogenation jar receives the inflow waste water 1 from the one-level clarifying tank, then will be in aeration tank 4 cycle period contain the high density nitric nitrogen and the 4 mixing liquid suspended sludges that return from the aeration tank, be reduced into nitrogen by the organism that use to flow in the waste water, subsequently with formed nitrogen discharge in atmosphere; Aeration tank 4, this aeration tank receive from the MLSS 3 of denitrogenation jar 2 dischargings and will be aeration tank 4 cycle period become the MLSS 5 that contains the high density nitric nitrogen and turn back in the denitrogenation jar 2; Secondary clarifying tank 7, this secondary clarifying tank are used to receive the waste discharge 6 from aeration tank 4, the mud in this sedimentation waste water 6, and the mud with predetermined amount turns back in denitrogenation jar 2 and the phosphorus separator 11 then; With phosphorus separator 11, it is low and from the discharging mud of secondary clarifying tank 7 that this phosphorus separator is used to receive nitric nitrogen concentration, by the gravity thickening method mud separated with the solid-liquid state, then mud 13 and supernatant liquor 12 delivered in the aeration tank 4.
According to process shown in Figure 1, hereinafter will describe operation of the present invention in detail.
In denitrogenation jar 2, return mud 10 from the 3rd of the waste discharge 1 of one-level clarifying tank (not shown), secondary clarifying tank 7 and contain the high density nitric nitrogen and from the aeration tank 4 return first return mud 5 and mix, by using the organism in the waste discharge 1 that the one-level clarifying tank is discharged, first nitrate-nitrogen reduction of returning in the mud 5 is become nitrogen, and with this nitrogen discharge in atmosphere.
The function of nitrogen removing device has some difference in the Phostrip technology of the function of denitrogenation jar 2 of the present invention and tradition improvement.In the Phostrip technology of tradition improvement, because nitrogen removing device denitrogenated processing arrangement after the secondary clarifying tank, then with having removed treatment of organic matters of organic waste water as carbon source, total system denitrogenate the efficient step-down, the nitrate nitrogen content that therefore flows into the phosphorus separator uprises.As a result, it is difficult discharging phosphorus from the phosphorus separator.But in the present invention, denitrogenation jar 2 is positioned in before the aeration tank 4, and this denitrification process further improves the efficient of denitrogenating of total system by consuming all organism that flow in the waste water.Because most inflow organism has been consumed in the denitrogenation jar,, also can reach the high efficient of denitrogenating even its hydromechanics residence time (HRT) in the aeration tank is short.At this moment, according to the amount that flows into from the one-level clarifying tank, the hydromechanics residence time in denitrogenation jar 2 preferably is defined in 1～2 hour the scope, and the mixing tank 2a that the mixture that flows into waste water and return mud is mixed is housed in the denitrogenation jar 2.
As mentioned above, the present invention has the feature of the nitrogen rejection facility that is different from conventional P hostrip technology.The poor phosphorus sludge that aeration tank 4 receives after having passed through the waste discharge that contains mixing sludge 3 of denitrogenation jar 2 and discharge phosphorus in phosphorus separator 11.In aeration tank 4, the oxidation operation in the inflow waste water that has passed through the denitrogenation jar, wherein ammoniacal nitrogen is oxidized to nitric nitrogen, and absorbs wherein a large amount of phosphorus by the microorganism that is used for removing dephosphorization.For the optimum condition of nitrated microorganism growth is provided, the organism feeding rate of aeration tank 4 is preferably established in 0.1kg BOD/kg MLVSSd～0.3kg BOD/kg MLVSSd scope, and its hydromechanics residence time (HRT) is appropriately determin and is about 4 hours.
In aeration tank 4 by nitrated and become that the mixing sludge that contains the high density nitric nitrogen turns back in the denitrogenation jar 2 and nitrated there, it is flow back in the aeration tank 4.
The mud that aeration tank 4 and denitrogenation jar are 2 returns than determining to be determined in the scope of 1～4 times waste discharge amount, and the material loading speed of nitric nitrogen preferably is decided to be and makes described returning than being about as much as flow into 1/4 of waste water COD in the denitrogenation jar 2.
The microorganism of growth in aeration tank 4 is separated into the solid-liquid state and makes it sedimentation in secondary clarifying tank 7, will be approximately the 3rd of 50% sedimentation mud then and return mud and turn back in the denitrogenation jar 2 and will be approximately second of 10～15% sedimentation mud and return mud and turn back in the phosphorus separator 11.
Return mud 9 from second of secondary clarifying tank 7 and in the phosphorus separator 11 of gravity thickening jar, be separated into the solid-liquid state.Phosphorus is discharged in the sludge blanket from the phosphorus separator that has formed anaerobic condition, and the poor phosphorus sludge that discharges then behind the phosphorus is returned in the aeration tank 4, and this pond has been in oxygen condition, utilizes microorganism there to absorb a large amount of phosphorus.In traditional Phostrip technology, the supernatant liquor 12 that contains sufficient phosphorus in the phosphorus separator be therein phosphorus by chemical treatment remove after the discharging.But in the present invention, most supernatant liquor is returned in the aeration tank 4, because it is to discharging not influence of phosphorus by nitric nitrogen.By being decomposed the organism that produces, cell discharges phosphorus reposefully as carbon source, required suitable detention time of mud (SDT) is 8～12 hours, the flow velocity that returns mud that returns phosphorus separator 11 from secondary clarifying tank 7 is about 10～15% of an influent flow velocity 1, the amount of transferring to the transfer mud of aeration tank 4 from phosphorus separator 11 is approximately 50% of phosphorus separator 11 influent flow velocitys, and the supernatant liquor 12 in this phosphorus jar is approximately 50% of phosphorus separator 11 influent flow velocitys.In the Phostrip technology of traditional Phostrip technology and improvement, returning than usually from secondary clarifying tank 7 to phosphorus separator 11 up to 30% of aeration tank influent flow velocity.But, in the present invention, when the organism when use to flow into waste water in the denitrogenation jar in is handled the nitric nitrogen that produces in aeration tank 4, owing to improved nitrogen-removing rate, returning from the secondary clarifying tank to the phosphorus separator than determining in 10%～15% scope of influent flow velocity.
In the experiment of this specific embodiments, sanitary sewage and waste water are used as inflow water below.In the concentration fixed of phosphorus and nitrogen with when only change flows into organic concentration, this experiment has been carried out about six months.As shown in table 1, the characteristic that flows into waste water under each condition is identical with state, and this experiment is that ability at treating water is 20m
3Carry out in the pilot plant in/sky.
Table 1
| Classification | COD | BOD | SS | TKN | NH 3-N | NO 3-N | T-N | T-P | Month |
| Condition I | 360 | 180 | 150 | 37 | 24 | 0.1 | 37.1 | 5.0 | 2 |
| Condition II | 250 | 125 | 145 | 35 | 26 | 0.5 | 35.5 | 5.0 | 2 |
| Condition III | 150 | 75 | 100 | 35 | 24 | 0.4 | 35.4 | 5.0 | 2 |
(unit: mg/litre)
Wherein, COD and BOD represent chemical oxygen demand (COD) and biological oxygen demand respectively, and SS represents suspended solids, and TKN, T-N and T-P represent TKN, total nitrogen and total phosphorus, NH respectively
3-N and NO
3-N (NO
x-N) represent ammoniacal nitrogen and nitric nitrogen respectively.
Tap water with supply dilutes the waste water that flows into, thereby quality, chemical oxygen demand (COD) (COD), biological oxygen demand (BOD) of making the inflow waste water of organic concentration such as wastewater treatment plant or the like are minimized, and add urea (urea) fertilizer and phosphatic manure then so that prevent ammoniacal nitrogen (NH
3-N) and the concentration of total phosphorus (TP) be lowered.
This experimental system is made up of denitrogenation jar 2, aeration tank 4, secondary clarifying tank 7 and phosphorus separator 11, and they are to be made by the steel plate of 3.2 mm thick.
The size of denitrogenation jar 2 is approximately 1.7m
3, being approximately 2 hours according to the residence time of influent flow velocity, mixing tank 2a is installed in the denitrogenation jar 2, and the rotating speed of this mixing tank is 90rpm so that 4 mud that return 5 and mud 10 uniform mixing that return from secondary clarifying tank 7 from the aeration tank.The volume of aeration tank 4 is approximately 3.4m
3, this aeration tank is furnished with three dividing plates and forms four chambers, in order oxygen to be provided for aeration tank 4 and oxygen to be mixed fully, supplies with 150 liters/minute air with gas blower.
The volume of secondary clarifying tank is approximately 3.3m
3, sedimentary a part of mud is directly turned back in the denitrogenation jar in clarifying tank 7, and rest part is returned in the phosphorus separator by pump.
The volume of phosphorus separator 11 is 3.3m
3, in order to absorb phosphorus, mud in this separator and supernatant liquor all are returned in the aeration tank 4.
In this experiment, the experiment condition of each retort is listed in the table below 2.
Table 2
| Classification | Experiment condition | |
| Flow into the amount (Q) of waste water | 20 cubic metres/day | |
| The denitrogenation jar | HRT:2 hour (according to the flow velocity that flows into waste water) | |
| The aeration tank | HRT:4 hour F/M ratio: the concentration of 0.1-0.3kgBOD/kgMLVSS.d microorganism: 3,000-4,000 mg/litre | |
| The phosphorus separator | The concentration of detention time of mud: 8-12 hour microorganism: 20,000-25,000 mg/litre | |
| The amount of circulating sludge | Aeration tank → denitrogenation jar | 4Q |
| Secondary clarifying tank → denitrogenation jar | 0.5Q | |
| Secondary clarifying tank → phosphorus separator | 0.1-0.15Q | |
| Phosphorus separator → aeration tank | 0.05-0.75Q | |
Table 3 has hereinafter been listed the result of the waste discharge quality of secondary clarifying tank discharge, and this result is the experiment condition of fixed table 2, analyzes after experimentizing respectively under each condition of table 1.
Table 3
| Classification | COD | BOD | SS | TKN | NH 3-N | NO x-N | T-N | T-P |
| Condition I | 15 | 6 | 4 | 1.5 | 0.5 | 5 | 5.5 | 0.1 |
| Remove rate (%) | 96 | 97 | 97 | 96 | 98 | - | 85 | 98 |
| Condition II | 10 | 6 | 5 | 1.0 | 0.5 | 7 | 7.5 | 0.3 |
| Remove rate (%) | 96 | 95 | 97 | 97 | 98 | - | 79 | 94 |
| Condition III | 10 | 5 | 3 | 1.0 | 0.5 | 13 | 13.5 | 1.5 |
| Remove rate (%) | 93 | 95 | 97 | 97 | 98 | - | 62 | 70 |
(unit: mg/litre)
Total nitrogen (T-N): TKN (TKN)+nitrite nitrogen (NO
x-N)
Total phosphorus (T-P): suspended solids (SS)+titanium pigment
In order to analyze with the method according to this invention, under the experiment condition identical with specific embodiments of the present invention, the inventor has carried out the experiment of traditional improvement Phostrip method that is used for dephosphorization.That is, what be provided with in aeration tank and phosphorus separator and the specific embodiments is big or small identical, is that 8 hours denitrogenation jar is installed between secondary clarifying tank and the phosphorus separator the residence time is arranged, and carries out this contrast experiment then under same cycle and same condition.Experimental result is listed in table 4, and this result is the water quality analysis of the outflow waste water handled with the Phostrip method.With reference to table 4, as biological oxygen demand (BOD), chemical oxygen demand (COD) (COD), the suspended solids organic efficient of removing such as (SS), and the nitrification efficiency of TKN (TKN), ammoniacal nitrogen etc. and of the present invention similar.But, only being positioned in the function of the denitrogenation jar between secondary clarifying tank and the phosphorus separator, nitrogen-removing rate is failed to reach and is obtained the required nitrogen-removing rate of native system preferred operations efficient.Therefore, total system always to denitrogenate efficient very low, and, owing to the nitric nitrogen that flow into the phosphorus separator, total dephosphorization efficiency by using with of the present invention compare also low.
Table 4
| Classification | COD | BOD | SS | TKN | NH 3-N | NO x-N | T-N | T-P |
| Condition I | 16 | 5 | 5 | 1.0 | 0.5 | 23 | 24 | 3.2 |
| Remove rate (%) | 96 | 97 | 97 | 97 | 98 | - | 35 | 36 |
| Condition II | 10 | 5 | 8 | 1.0 | 0.5 | 20 | 21 | 3.0 |
| Remove rate (%) | 96 | 96 | 94 | 97 | 98 | - | 41 | 40 |
(unit: mg/litre)
In order to analyze with the method according to this invention, under the experiment condition identical with specific embodiments of the present invention, the contriver has also made the A of dephosphorization and nitrogen
2The experiment of/O method.That is, install and specific embodiments big or small identical aeration tank and denitrogenation jar, another anaerobic jar that is used for discharging phosphorus is installed in the denitrogenation jar before, then as shown in table 1 according to specific embodiments of the present invention condition I and II under experimentize.
Its result is as shown in table 5, and this result is A
2The water quality analysis of the waste discharge that/O method was handled.With reference to table 5, compare with the present invention, at A
2Under the situation of/O method, nitrogen-removing rate is obviously fluctuation along with the variation that flows into the organic concentration in the waste water.But dephosphorization in the present invention and nitrogen-removing rate are stable and are better than A
2/ O method.
Table 5
| Classification | COD | BOD | SS | TKN | NH 3-N | NO x-N | T-N | T-P |
| Condition I | 19 | 8 | 5 | 1.5 | 0.5 | 10 | 11.5 | 0.5 |
| Remove rate (%) | 95 | 96 | 97 | 96 | 98 | - | 69 | 90 |
| Condition II | 15 | 5 | 8 | 1.30 | 0.5 | 16 | 17.3 | 4.0 |
| Remove rate (%) | 94 | 96 | 94 | 97 | 98 | - | 51 | 20 |
(unit: mg/litre)
According to the traditional Phostrip technology and the contrast of processing efficiency of the present invention, under the situation of traditional Phostrip method, because the process of denitrogenating is arranged in after the secondary settlement process, and this process by in the aeration tank after the oxidation remaining organic matters carry out as carbon source, the nitrogen-removing rate of total system is low.On the other hand, under situation of the present invention, as shown in Figure 1, nitrated nitric nitrogen is returned in the denitrogenation jar 2 that is placed in before the aeration tank in the aeration tank, at this moment, by the high inflow waste water of organic concentration as carbon source, remove the first high nitric nitrogen that returns in the mud 5 of nitric nitrogen concentration, therefore, improved the efficient of denitrogenating of total system.Because most inflow organism is removed in denitrogenation jar 2, the volume of aeration tank 4 can be reduced to smaller than the traditional method.Because the rate of removing of nitric nitrogen is very high in denitrogenation jar 2, flowing into second of phosphorus separator 11 from secondary clarifying tank 7, to return the concentration of the nitric nitrogen the mud 9 very low.The result, even the process of between secondary clarifying tank 7 and phosphorus separator 11, not denitrogenating and mud is directly turned back to the denitrogenation jar 2 from secondary clarifying tank 7, owing in phosphorus separator 2, there is not the influence of nitric nitrogen, discharging phosphorus in phosphorus separator 11 is easy to carry out, and absorbing phosphorus in aeration tank 4 is easy to carry out, therefore, dephosphorization efficiency by using is stable.
As mentioned above,, consume all organism that flow in the waste water, can improve the efficient of denitrogenating of total system by the denitrification process in the denitrogenation jar before the aeration tank according to the present invention.As a result, by making the nitric nitrogen that flows in the phosphorus separator minimum, discharge phosphorus and carry out easily in the phosphorus separator, compare with traditional method, the efficient of dephosphorization and nitrogen is improved widely.
Therefore, be understood that, the present invention is not limited to the particular of estimating as realization best mode of the present invention disclosed herein, but the present invention also is not limited to the specific specific embodiments of describing in this manual except that claims limit.
Claims (4)
1. the system of biological removal of nitrogen and phosphorus in sewage and the waste water treatment process, this system comprises:
The denitrogenation jar, this jar will and return mud and mix to form the mixing liquid suspended sludge from the inflow waste water of one-level clarifying tank, with the organism in the inflow waste water described mixing liquid suspended sludge will be reduced into nitrogen, then formed nitrogen will be discharged in the atmosphere;
Mixing device, this device will flow into waste water and the mud that returns from secondary clarifying tank and aeration tank mixes, and this mixing device is installed in the described denitrogenation jar;
The aeration tank, this pond receives the mixing liquid suspended sludge of discharging from the denitrogenation jar, and then that nitric nitrogen concentration is high mixing liquid suspended sludge turns back in the denitrogenation jar;
The secondary clarifying tank, this groove receives the mixing liquid suspended sludge of discharging from the aeration tank, precipitation mud wherein, the mud with predetermined amount turns back in denitrogenation jar and the phosphorus separator then; With
Phosphorus separator, this separator receive nitric nitrogen concentration mud low, that return from the secondary clarifying tank, and by the gravity thickening method it are separated into mushy stage, then mud in the phosphorus separator and supernatant liquor are turned back in the aeration tank.
2. system as claimed in claim 1, wherein said denitrogenation jar is a kind of anoxic jar, this anoxic jar allows all inflow waste water of one-level clarifying tank only to be consumed in denitrification process, to improve the efficient of denitrogenating of total system.
3. the method for biological removal of nitrogen and phosphorus in sewage and the waste water treatment process, this method comprises:
The first step, in the denitrogenation jar, will return from the aeration tank come return mud and mix from the waste discharge of one-level clarifying tank, then formed mixing liquid suspended sludge is discharged in the aeration tank;
Second step, in the aeration tank, remove the organism of inflow and the TKN of nitrated inflow, the mixing liquid suspended sludge with nitrated mistake turns back in the denitrogenation jar then;
The 3rd step, in the denitrogenation jar, pass through to use all organism that flow in the waste water, nitric nitrogen in the mixing liquid suspended sludge of nitrated mistake is removed, increase the efficient of denitrogenating of total system thus, wherein, in the 3rd step, in the denitrogenation jar, flow into waste water and be used as and remove the required carbon source of nitric nitrogen, only allow in denitrification process, to be consumed from all waste discharges of one-level clarifying tank;
The 4th step, in the secondary clarifying tank, by the microorganism that grows in the aeration tank being separated into mushy stage and they being precipitated, then the mud of a part is returned in the phosphorus separator and with the part of remainder and return in the denitrogenation jar, wherein, in described the 3rd step and the 4th step, by handling the nitric nitrogen that in the aeration tank, generates with all organism that flow in the waste water, the nitric nitrogen that is comprised from the secondary clarifying tank turns back to mud the phosphorus separator is reduced, and the release of phosphorus just is not subjected to the influence of nitric nitrogen in the phosphorus separator like this;
The 5th step, be separated in the mud that stores with a solid liquid status in the phosphorus separator, and formation anaerobic condition, then poor phosphorus sludge and rich phosphorus supernatant liquor are returned in the aeration tank that is in aerobic condition, wherein, in the 5th step, between residence time, cell decomposes the organism that produces and is used as the required organism of release phosphorus at predetermined mud; With
In the 6th step, remove the phosphorus in the mud of returning from the phosphorus separator by making microorganism in the aeration tank, absorb enough phosphorus.
4. method as claimed in claim 3, wherein second step provide the optimum condition of microorganism growth, this condition be organic material loading speed in the scope of 0.1kg BOD/kg MLVSSd～0.3kg BOD/kg MLVSSd and the hydromechanics residence time in 4～5 hours scope.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR69931/1996 | 1996-12-21 | ||
| KR69931/96 | 1996-12-21 | ||
| KR1019960069931A KR100231084B1 (en) | 1996-12-21 | 1996-12-21 | Biological phosphor and nitrogen removal device and method modificating phostrip method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1186050A CN1186050A (en) | 1998-07-01 |
| CN1102130C true CN1102130C (en) | 2003-02-26 |
Family
ID=19490177
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97116878A Expired - Lifetime CN1102130C (en) | 1996-12-21 | 1997-09-03 | System and method for removing biologically both nitrogen and phosphorous removal in sewage and wastewater |
Country Status (3)
| Country | Link |
|---|---|
| KR (1) | KR100231084B1 (en) |
| CN (1) | CN1102130C (en) |
| DE (1) | DE19737373B4 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100377968C (en) * | 2003-11-11 | 2008-04-02 | 哈曼股份公司 | Process and assembly for the treatment of waste water on ships |
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| KR20000024252A (en) * | 2000-02-01 | 2000-05-06 | 김창수 | Advanced Treatment System using Rotating Immobilized Phosphorus Sweeper from Wastewater, Sewage and Industrial Wastewater |
| PL365164A1 (en) | 2000-08-03 | 2004-12-27 | Bioclar A.S. | Activated sludge method and device for the treatment of effluent with nitrogen and phosphorus removal |
| CN100395196C (en) * | 2006-08-15 | 2008-06-18 | 北京工业大学 | Improved MUCT technology and device |
| CN100395197C (en) * | 2006-08-15 | 2008-06-18 | 北京工业大学 | Improved UCT technology and device |
| KR101005793B1 (en) * | 2010-06-03 | 2011-01-06 | 부산환경공단 | Reconstructed-plung lime ii process for nitrogenand and phosphate removal in sewage |
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| CN106746391A (en) * | 2016-11-16 | 2017-05-31 | 环境保护部南京环境科学研究所 | A kind of phosphatization recycling sludge method of disposal |
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| CN110550823B (en) * | 2019-09-11 | 2024-09-10 | 清上(苏州)环境科技有限公司 | System and method for treating algal bloom in water body |
| CN111233151A (en) * | 2020-03-17 | 2020-06-05 | 山东太平洋环保股份有限公司 | Efficient synchronous nitrogen and phosphorus removal system and method for high-nitrogen and phosphorus wastewater |
| CN114349257A (en) * | 2020-10-13 | 2022-04-15 | 同济大学 | Sewage treatment method based on MBR process |
| CN115677069B (en) * | 2021-07-23 | 2024-09-13 | 中国石油天然气股份有限公司 | Treatment method of excess sludge |
| CN117534258B (en) * | 2023-12-25 | 2024-05-14 | 知和环保科技有限公司 | Preparation method of efficient carbon source |
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| CN1030902A (en) * | 1983-05-06 | 1989-02-08 | 伏尔加-乌拉尔硫化氢气体开挖加工科学研究设计院 | Remove the biological purification method of methyl alcohol in the sewage |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4331927C2 (en) * | 1992-09-17 | 1995-07-13 | Mannesmann Ag | Process for the biochemical removal of nitrogen and phosphorus from waste water |
| DE4239184C1 (en) * | 1992-11-21 | 1993-10-07 | Burghardt Dipl Chem Elster | Biological sewage phosphate removal - has initial stripper centrally in the stripper basin with separate zones for sludge to move in opposite directions |
-
1996
- 1996-12-21 KR KR1019960069931A patent/KR100231084B1/en not_active IP Right Cessation
-
1997
- 1997-08-27 DE DE1997137373 patent/DE19737373B4/en not_active Expired - Fee Related
- 1997-09-03 CN CN97116878A patent/CN1102130C/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1030902A (en) * | 1983-05-06 | 1989-02-08 | 伏尔加-乌拉尔硫化氢气体开挖加工科学研究设计院 | Remove the biological purification method of methyl alcohol in the sewage |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100377968C (en) * | 2003-11-11 | 2008-04-02 | 哈曼股份公司 | Process and assembly for the treatment of waste water on ships |
Also Published As
| Publication number | Publication date |
|---|---|
| KR19980051067A (en) | 1998-09-15 |
| DE19737373A1 (en) | 1998-06-25 |
| DE19737373B4 (en) | 2011-12-22 |
| KR100231084B1 (en) | 1999-11-15 |
| CN1186050A (en) | 1998-07-01 |
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