CN104098172A - Culture method of sulfur synergy denitrification simultaneous nitrogen and phosphorous removal granular sludge - Google Patents
Culture method of sulfur synergy denitrification simultaneous nitrogen and phosphorous removal granular sludge Download PDFInfo
- Publication number
- CN104098172A CN104098172A CN201410326806.XA CN201410326806A CN104098172A CN 104098172 A CN104098172 A CN 104098172A CN 201410326806 A CN201410326806 A CN 201410326806A CN 104098172 A CN104098172 A CN 104098172A
- Authority
- CN
- China
- Prior art keywords
- sludge
- source
- phosphorus
- stage
- sulphur
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- Y02W10/12—
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention belongs to the technical field of biological treatment of wastewater and particularly relates to a culture method of sulfur synergy denitrification simultaneous nitrogen and phosphorous removal granular sludge. The culture method of the sulfur synergy denitrification simultaneous nitrogen and phosphorous removal granular sludge is divided into three stages as follows: a sludge acclimation stage, a granular sludge growth stage and a granular sludge mature stage. According to the culture method, mechanical stirring is adopted, the stirring speed is controlled, and activated sludge is evenly distributed, so that the formed granular sludge is stable in performance, good in impact resistance and high in adaptability to external environment change, organic matters, nitrogen and phosphorus are effectively removed in one reactor, and sulfate radicals are involved in the whole process to play a synergistic role.
Description
Technical field
The invention belongs to biological wastewater treatment technology field, be specifically related to the cultural method of the collaborative denitrification synchronous denitrification dephosphorizing granule sludge of a kind of sulphur.
Background technology
21 century, facing mankind some serious global problems, and wherein water quality and quantity problem is particularly outstanding.By various waste water treatment process, removing nutritive substance to alleviate body eutrophication problem, is the measure of having to take in each department.The most frequently used is enhanced biological phosphorus removal technique, and this technique adopts nitrate radical as electron acceptor(EA) in subordinate phase, can reach the effect of synchronous denitrification dephosphorizing.Therefore but the exploitation of coastland to seawater, have caused the generation of a large amount of brine wastes, a kind of brine waste treatment process arises at the historic moment, and sulfate reduction, supports denitrification and nitrated integral process in vain and (is called for short
technique), this technique can effectively reduce the output of excess sludge, has positive effect to removing organism and nitrogen simultaneously, but slightly not enough aspect dephosphorization.
Granule sludge is due to its outstanding settling property, high-biomass level, high organic loading and tolerance of toxic substance etc. has been obtained to increasing concern.In sequencing batch activated sludge reactor, have the research of successfully turning out poly-phosphorus microbe granular, but most employing is the processing condition that anaerobic and aerobic replace.
Therefore, under the processing condition that how replace in anaerobism and anoxic, turn out the collaborative denitrification nitrogen and phosphorus removal granule sludge of sulphur, and reach good treatment effect, become the difficult problem that must first capture in this technique granulating application.
Summary of the invention
The shortcoming that the object of the invention is to overcome prior art, with not enough, provides the cultural method of the collaborative denitrification synchronous denitrification dephosphorizing granule sludge of a kind of sulphur.
Object of the present invention is achieved through the following technical solutions:
A cultural method for the collaborative denitrification synchronous denitrification dephosphorizing granule sludge of sulphur, comprises following steps:
(1) the sludge acclimatization stage: add the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur in reactor, intake as containing the waste water of carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion, start reactor and start the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add nitrate as nitrogenous source, reactor enters anoxic and inhales the phosphorus stage; When phosphorus source, clearance reaches more than 20%, and nitrate removal rate reaches 80～100%, sludge volume index SVI
5lower than 80mL/g, SVI
30during lower than 35mL/g, the domestication stage finishes;
(2) the granule sludge stage of growth: after the domestication stage finishes, continue to add the waste water that contains carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion in reactor, reactor enters the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add and start anoxic after nitrate and inhale the phosphorus stage, the median size of periodic measurement active sludge, when its median size reaches 85～100 μ m, can think that the Granular sludge formation stage finishes;
(3) the granule sludge stage of maturity: after the Granular sludge formation stage finishes, continue to add the waste water that contains carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion in reactor, carry out the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add nitrate reaction device and enter the anoxic suction phosphorus stage, granule sludge is mutually assembled and is formed larger particles mud in reactor, measure its median size and reach 110～120 μ m, the clearance in phosphorus source is higher than 70%, nitrate removal rate higher than 90% time, can think that granule sludge is tending towards ripe;
Described carbon source is organic carbon source, by sodium-acetate, is provided; In described waste water, acetate starting point concentration is 150mg C/L;
Described sulphur source is provided by sodium sulfate, and described sulfate radical in waste water starting point concentration is 200mg S/L;
Described phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate; The starting point concentration of described Phosphorus From Wastewater acid group is 20mg P/L;
Described calcium ion is provided by calcium chloride, and in described waste water, the starting point concentration of calcium ion is 18～20mgCa
2+/ L;
Described magnesium ion is provided by magnesium chloride, and in described waste water, the starting point concentration of magnesium ion is 9～10mgMg
2+/ L;
Nitrate described in step (1), (2) and (3) is provided by saltpetre, adds after nitrate, and the final concentration of nitrate in reactor is 20～50mg N/L;
Described reactor is sequencing batch reactor activated sludge reaction device (Sequencing Batch Reactor is called for short SBR), material is synthetic glass, by sampling valve, stopple coupon, excess sludge pipe, excess sludge valve, go out bucket, water inlet bucket, intake pump, rising pipe, outlet valve, water intaking valve, water inlet pipe, stirring rake, stirring host, ORP probe, pH probe, ORP main frame, pH main frame and reactor body and form;
The reaction volume of described reactor is preferably 1.4L;
The dosage of the waste water described in step (1), (2) and (3) is 0.7L;
Process conditions in step (1) is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 150rpm mechanical stirring, 20～25 ℃ of temperature of reaction, and water inlet pH6.8～7.3, hydraulic detention time remains on 12～16h;
In step (2), process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 120rpm mechanical stirring, makes stirring rake in reactor be positioned at bottom position, and active sludge keeps mixing completely state at reactor; 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time remains on 12～16h;
In step (3), process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts the slow speed of revolution 120～150rpm mechanical stirring, makes stirring rake in reactor be positioned at bottom position, and active sludge keeps mixing completely state at reactor; 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time remains on 10～12h;
The collaborative denitrification nitrogen and phosphorus removal seed sludge of described sulphur is mud mixture, and its sludge concentration is 9～12g SS/L, and the dosage in reactor is 1.4L, then through precipitating the supernatant liquor 0.7L that drains;
The collaborative denitrification nitrogen and phosphorus removal seed sludge of described sulphur, its preparation method comprises following concrete steps:
1. in reactor, add anaerobic activated sludge to carry out sludge acclimatization, the situation of intaking and existing with acclimated microorganism adaptation phosphorus source for the waste water that contains carbon source, He Lin source, sulphur source; The domestication initial stage, the adding of nitrate-free, main purpose is improving the changing effect, particularly sulfate reduction effect of sulphur;
2. when sulfide generation reach system total sulfur 15% time, adopt anaerobic phosphorus release-anoxic to inhale phosphorus mode and carry out the further domestication of active sludge and cultivate; Wherein, the waste water that contains carbon source, He Lin source, sulphur source enters reactor and starts the anaerobic phosphorus release stage, and the anaerobic phosphorus release stage is consistent with first stage method is adding of anaerobism section nitrate-free; When carbon source concentration drops to zero, start to add nitrate as nitrogenous source, start anoxic and inhale the phosphorus stage, and the concentration after nitrate adds in reactor is increased to 20mg N/L gradually by 5mg N/L, the object of progressively taming to reach microorganism, and then obtain the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur;
Step 1., the carbon source described in is 2. organic carbon source, by sodium-acetate, provided; In the described waste water that contains carbon source, He Lin source, sulphur source, acetate starting point concentration is 150mg C/L; Described sulphur source is provided by sodium sulfate, and the described sulfate radical in waste water starting point concentration that contains carbon source, He Lin source, sulphur source is 200mg S/L; Described phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate; The starting point concentration of the described Phosphorus From Wastewater acid group that contains carbon source, He Lin source, sulphur source is 20mg P/L; Described nitrate is preferably saltpetre;
Step 1., the reactor described in is 2. sequencing batch reactor activated sludge reaction device (Sequencing Batch Reactor is called for short SBR), material is synthetic glass, by sampling valve, stopple coupon, excess sludge pipe, excess sludge valve, go out bucket, water inlet bucket, intake pump, rising pipe, outlet valve, water intaking valve, water inlet pipe, stirring rake, stirring host, ORP probe, pH probe, ORP main frame, pH main frame and reactor body and form; Step 1., the reaction volume of the reactor described in is 2. preferably 10L;
The anaerobic activated sludge of step described in is 1. that muddy water mixes, and its sludge concentration is 5.98g SS/L, and dosage is 10L, then through the precipitation supernatant liquor 5L that drains;
Step 1., the influent waste water described in is 2. preferably 5L;
Step process conditions is 1.: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, stirring velocity 400rpm, 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time 100～136h;
Step process conditions is 2.: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, stirring velocity 400rpm, 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time 68～100h; The step reaction times is 1. 0.5～1 month, and the step reaction times is 2. 1.5～3 months;
Principle of the present invention:
Microorganism in described reactor assembly first utilizes organism and cell content glycogen as electron donor in the anaerobic phosphorus release stage, vitriol carries out metabolism as electron acceptor(EA), discharge polymeric phosphate in biomass cells simultaneously, generate the poly-β hydroxy fatty acid of sulfide, carbonic acid gas and cell content, polymerised sulphur particle; In the anoxic suction phosphorus stage, add after nitrate subsequently, in system, microorganism utilizes nitrate to carry out autotrophic metabolism as electron acceptor(EA), sulfide in oxidation system, generate vitriol, carry out excessive suction phosphorus, now the poly-β hydroxy fatty acid of cell content, polymerised sulphur particle provide energy for excessive suction phosphorus process simultaneously.Each material in stable system transforms under microbial process, entering organic matter of water is degraded to carbonic acid gas, sulfate radical is first converted into sulfide and then is oxidized to sulfate radical and completes a circulation, and the nitrate radical adding in the situation that organism runs out of is converted into nitrogen simultaneously;
The present invention, on the principle basis of above microbial metabolism, adds calcium ions and magnesium ions in water inlet, and in the process of active sludge formation particle, as grain skeleton, calcium ions and magnesium ions concentration in water inlet is respectively 9～10mgCa
2+/ L and 18～20mg Mg
2+/ L.The operation of simultaneous reactions device adopts mechanical stirring, and stirring rake is that standard four leaves are spiral, and stirring velocity remains on 120～150rpm, and stirring velocity is controlled at and reaches the stagnation point that muddy water mixes, to reduce the destruction of stirring rake to particle.
The present invention has following advantage and effect with respect to prior art:
The inventive method adopts mechanical stirring, controls stirring velocity, and active sludge is uniformly distributed, and makes the granule sludge stable performance of formation, and impact resistance is good, adapts to external environment changing capability strong.Realized in a reactor and effectively to have removed organism, nitrogen phosphorus, and sulfate radical participates in whole process and plays synergy.Concrete advantage is:
(1) processing efficiency is high, and the clearance of organism and nitrate radical is more than 90%, and the clearance of phosphate radical also reaches 80% left and right;
(2) non-secondary pollution, sulfate radical participates in whole process and plays synergy, although there is intermediate product hydrogen sulfide to produce, in subordinate phase, is oxidized to sulfate radical;
(3) sludge yield is low, produces, without carrying out excess sludge processing without excess sludge;
(4) small accommodation area, the removal of organism, nitrogen phosphorus completes in a reactor;
(5) settling property of granule sludge is good, has obviously shortened the treatment time, has improved processing efficiency.
Accompanying drawing explanation
Fig. 1 is the structural representation of sbr reactor device of the present invention, wherein, and 1 sampling valve; 2 stopple coupons; 3 excess sludge pipes; 4 excess sludge valves; 5 go out bucket; 6 water inlet buckets; 7 intake pumps; 8 rising pipes; 9 outlet valves; 10 water intaking valves; 11 water inlet pipes; 12 stirring rakes; 13 stirring hosts; 14ORP probe; 15pH probe; 16ORP main frame; 17pH main frame; 18 reactor bodies.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited to this.
The cultivation of the collaborative denitrification synchronous denitrification dephosphorizing granule sludge of embodiment 1 sulphur
1. in sequencing batch reactor activated sludge reaction device (reaction volume 10L), adding the initial sludge concentration of 10L is the muddy water mixed solution of the anaerobic activated sludge (picking up from Shatian, Hong Kong sewage work) of 5.98g SS/L, precipitation is removed after supernatant liquor 5L, enter 5L synthetic waste water (its component content is in Table 1) and carry out sludge acclimatization, the environment existing with acclimated microorganism adaptation phosphate radical improves its microorganism active simultaneously; Described synthetic waste water contains carbon source, sulphur source and phosphorus source, and described carbon source is for being provided by sodium-acetate; In synthetic waste water, acetate starting point concentration is 150mg C/L; Described sulphur source is provided by sodium sulfate, and synthetic sulfate radical in waste water starting point concentration is 200mg S/L, and described phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate; The starting point concentration of synthetic Phosphorus From Wastewater acid group is 20mg P/L; The startup first stage of reactor is for strengthening sulphur cycle synergy, in whole process, do not add saltpetre, process conditions: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, stirring velocity remains on 400rpm, and temperature of reaction is at 20～25 ℃, and pH is 6.8～7.3 in water inlet, hydraulic detention time is 100～136h, and this elementary reaction time overall length is 0.5～1 month;
2. when sulfide generation reach system total sulfur 15% time, can enter startup subordinate phase; Subordinate phase is acclimated microorganism denitrification dephosphorization effect on the synergistic basis of sulphur cycle, this stage is divided into the anaerobic phosphorus release stage and anoxic is inhaled the phosphorus stage, synthetic waste water enters reactor and starts the anaerobic phosphorus release stage, and the anaerobic phosphorus release stage is anaerobism section adding without nitrate radical with starting first stage method consistent; In waste water acetate gradually by microbial consumption until concentration reduces to zero, now add saltpetre and enter the anoxic suction phosphorus stage, concentration after saltpetre adds in reactor is increased to 20mg N/L gradually by 5mg N/L, the object of progressively taming to reach microorganism, and then obtain the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur; Process conditions: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, and stirring velocity remains on 400rpm, temperature of reaction is at 20～25 ℃, pH is 6.8～7.3 in water inlet, and hydraulic detention time is 68～100h, and this elementary reaction time overall length is 1.5～3 months.
Embodiment 2
(1) the sludge acclimatization stage: to sequencing batch reactor activated sludge reaction device (SBR, reaction volume 1.4L) in, add the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur of embodiment 1 preparation, wherein, seed sludge concentration is 9.45g SS/L, dosage is 1.4L, add to postprecipitation in reactor to remove supernatant liquor 0.7L, then to the 0.7L of intaking in reactor, contain carbon source, sulphur source, phosphorus source, the synthetic waste water of calcium ion and magnesium ion starts the anaerobic phosphorus release stage, described carbon source is provided by sodium-acetate, sulphur source is provided by sodium sulfate, phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate, its starting point concentration in synthetic waste water is respectively 150mgC/L, 200mg S/L, 20mg P/L, described calcium ion, magnesium ion is respectively by calcium chloride, magnesium chloride provides, its starting point concentration in synthetic waste water is respectively 18～20mg Ca
2+/ L and 9～10mg Mg
2+/ L, after acetate concentration drops to zero, add saltpetre and start the anoxic suction phosphorus stage, the dosage of nitrate radical is 20～50mg N/L, above-mentioned process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 150rpm mechanical stirring, 20～25 ℃ of temperature of reaction, and water inlet pH6.8～7.3, hydraulic detention time remains on 12～16h, assaying reaction device water outlet acetate, phosphate radical, nitrate radical content, when phosphate radical clearance reaches more than 20%, nitrate radical clearance reaches 80～100%, sludge volume index SVI
5lower than 80mL/g, SVI
30during lower than 35mL/g, the domestication stage finishes,
(2) the granule sludge stage of growth: after the domestication stage finishes, continue to add the synthetic waste water that contains carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion in reactor, start the anaerobic phosphorus release stage; Described carbon source is provided by sodium-acetate, sulphur source is provided by sodium sulfate, phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate, its starting point concentration in synthetic waste water is respectively 150mg C/L, 200mg S/L, 20mg P/L, described calcium ion, magnesium ion are provided by calcium chloride, magnesium chloride respectively, and its starting point concentration in synthetic waste water is respectively 18～20mg Ca
2+/ L and 9～10mg Mg
2+/ L; After acetate concentration drops to zero, add saltpetre and start the anoxic suction phosphorus stage, the dosage of saltpetre is 20～50mg N/L; Above-mentioned process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 120rpm mechanical stirring, makes stirring rake in reactor be positioned at bottom position, and active sludge keeps mixing completely state at reactor; 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time remains on 12～16h; By Ma Erwen laser particle analyzer, measure the median size of active sludge, when its median size reaches 85～100 μ m, can think that the Granular sludge formation stage finishes;
(3) the granule sludge stage of maturity: after the Granular sludge formation stage finishes, continue to add the synthetic waste water that contains carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion in reactor, start the anaerobic phosphorus release stage; Described carbon source is provided by sodium-acetate, sulphur source is provided by sodium sulfate, phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate, its starting point concentration in synthetic waste water is respectively 150mg C/L, 200mg S/L, 20mgP/L, described calcium ion, magnesium ion are provided by calcium chloride, magnesium chloride respectively, and its starting point concentration in synthetic waste water is respectively 18～20mg Ca
2+/ L and 9～10mg Mg
2+/ L; After acetate concentration drops to zero, add saltpetre and start the anoxic suction phosphorus stage, the dosage of nitrate radical is 20～50mg N/L; Above-mentioned process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 150rpm mechanical stirring, makes stirring rake in reactor be positioned at bottom position, and active sludge keeps mixing completely state at reactor; 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time remains on 10～12h; Granule sludge is mutually assembled and is formed larger particles mud in reactor, by Ma Erwen laser particle analyzer, measure its median size and reach 110～120 μ m, the clearance of phosphate radical reaches 70%, when nitrate removal rate reaches 90%, can think that granule sludge is tending towards ripe;
The collaborative denitrification nitrogen and phosphorus removal technique integration apparatus of sulphur described in present embodiment is topmost processing unit in this technique, and reactor body 18 is primary members of described equipment, and main body 18 is made by synthetic glass, internal diameter 100mm, high 190mm, cubic capacity is 1.5L, useful volume 1.4L.After reaction finishes, staticly settle generation solid-liquid separation, open afterwards outlet valve 9 and discharge water outlet.Water inlet is pumped into by water intaking valve 10 the synthetic waste water preparing in water inlet bucket in reactor by intake pump 7.Simultaneous reactions device has connected ORP and pH on-Line Monitor Device 16 and 17.Reactor blending manner adopts mechanical stirring 13, and stirring rake 12 is quadruple formula.
The stock solution composition following table 1 of the synthetic wastewater of present embodiment.Its dosage is that every 1L water inlet adds 10mL waste water dope and 2mL micro solution.
The stock solution composition of table 1 synthetic waste water
This technique can be used as a processing unit and is applied in the treating processes containing the sulfate wastewater of organism and nitrogen phosphorus, and ammonia nitrogen enters in this process system and further removes again after can being converted into nitrate by digestion reaction, thereby reaches purification of waste water effect.
Embodiment 3
(1) the sludge acclimatization stage: add the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur prepared by embodiment 1 in reactor, sludge concentration is 9.00mg SS/L, take synthetic waste water (table 1) as water inlet, starts reactor and starts the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add saltpetre 20mg N/L (final concentration in reactor) as nitrogenous source, reactor enters anoxic and inhales the phosphorus stage; The condition of operation is: stirring velocity 150rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 16h; When mud granule median size 50 μ m, the clearance of acetate reaches 100%, and the clearance of nitrate radical reaches 90%, and the clearance of phosphate radical reaches 30%, SVI
5for 50mL/g, SVI
30for 30mL/g, the domestication stage finishes;
(2) the granule sludge stage of growth: after the domestication stage finishes, take synthetic waste water (table 1) as water inlet, reactor enters the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add and start anoxic after nitrate radical and inhale the phosphorus stage, anoxic is inhaled phosphorus section nitrate dosage 30mg N/L (final concentration in reactor); The condition of operation is: stirring velocity 120rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 16h, the clearance of this stage acetate and nitrate radical all can reach 100%, and the clearance of phosphate radical reaches 70%, granule sludge median size 86.5 μ m, SVI
5for 44.3mL/g, SVI
30for 24.5mL/g;
(3) the granule sludge stage of maturity: after the granule sludge stage of maturity completes, take synthetic waste water (table 1) as water inlet, carry out the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add saltpetre reactor and enter the anoxic suction phosphorus stage, anoxic is inhaled phosphorus section nitrate dosage 40mg N/L (final concentration in reactor); The condition of steady running is: stirring velocity 120rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 12h; When granule sludge median size is 110.3 μ m, SVI
5for 19.44mL/g, SVI
30for 15.59mL/g; The clearance of acetate and nitrate radical all can reach 100%, and the clearance of phosphate radical reaches 80%.
Embodiment 4
(1) the sludge acclimatization stage: add the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur prepared by embodiment 1 in reactor, sludge concentration is 10.24mg SS/L, take synthetic waste water (table 1) as water inlet, starts reactor and starts the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add saltpetre 30mg N/L (final concentration in reactor) as nitrogenous source, reactor enters anoxic and inhales the phosphorus stage; The condition of operation is: stirring velocity 150rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 14h; When mud granule median size 60 μ m, the clearance of acetate reaches 100%, and the clearance of nitrate radical reaches 90%, and the clearance of phosphate radical reaches 30%, SVI
5for 50mL/g, SVI
30for 30mL/g, the domestication stage finishes;
(2) the granule sludge stage of growth: after the domestication stage finishes, take synthetic waste water (table 1) as water inlet, reactor enters the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add and start anoxic after saltpetre and inhale the phosphorus stage, anoxic is inhaled phosphorus section nitrate dosage 40mg N/L (final concentration in reactor); The condition of operation is: stirring velocity 120rpm, 20～25 ℃ of temperature, water inlet pH=7,, hydraulic detention time 14h, the clearance of this stage acetate and nitrate radical all can reach 100%, the clearance of phosphate radical reaches 75%, granule sludge median size 92.3 μ m, SVI
5for 31.97mL/g, SVI
30for 23.15mL/g;
(3) the granule sludge stage of maturity: after the granule sludge stage of maturity completes, take synthetic waste water (table 1) as water inlet, carry out the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add saltpetre reactor and enter the anoxic suction phosphorus stage, anoxic is inhaled phosphorus section nitrate dosage 50mg N/L (final concentration in reactor); The condition of steady running is: stirring velocity 120rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 11h; When granule sludge median size is 117.8 μ m, SVI
5for 15.39mL/g, SVI
30for 13.25mL/g; The clearance of acetate and nitrate radical all can reach 100%, and the clearance of phosphate radical reaches 85%.
Embodiment 5
(1) the sludge acclimatization stage: add the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur prepared by embodiment 1 in reactor, sludge concentration is 12mg SS/L, take synthetic waste water (table 1) as water inlet, starts reactor and starts the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add saltpetre 30mg N/L (final concentration in reactor) as nitrogenous source, reactor enters anoxic and inhales the phosphorus stage; The condition of operation is: stirring velocity 150rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 12h; When mud granule median size 60 μ m, the clearance of acetate and nitrate radical reaches 90%, and the clearance of phosphate radical reaches 30%, SVI
5for 50mL/g, SVI
30for 30mL/g, the domestication stage finishes;
(2) the granule sludge stage of growth: after the domestication stage finishes, take synthetic waste water (table 1) as water inlet, reactor enters the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add and start anoxic after nitrate radical and inhale the phosphorus stage, anoxic is inhaled phosphorus section saltpetre dosage 40mg N/L (final concentration in reactor); The condition of operation is: stirring velocity 120rpm, and 20～25 ℃ of temperature, water inlet pH=7,, hydraulic detention time 12h, the clearance of this stage acetate and nitrate radical all can reach 100%, and the clearance of phosphate radical reaches 80%, granule sludge median size 98 μ m, SVI
5for 31.97mL/g, SVI
30for 23.15mL/g;
(3) the granule sludge stage of maturity: after the granule sludge stage of maturity completes, take synthetic waste water (table 1) as water inlet, carry out the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add saltpetre reactor and enter the anoxic suction phosphorus stage, anoxic is inhaled phosphorus section nitrate dosage 50mg N/L (final concentration in reactor); The condition of steady running is: stirring velocity 120rpm, 20～25 ℃ of temperature, water inlet pH=7, hydraulic detention time 10h; When granule sludge median size is 120 μ m, SVI
5for 15.39mL/g, SVI
30for 13.25mL/g; The clearance of acetate and nitrate radical all can reach 100%, and the clearance of phosphate radical reaches 90%.
Above-described embodiment is preferably embodiment of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and principle, substitutes, combination, simplify; all should be equivalent substitute mode, within being included in protection scope of the present invention.
Claims (10)
1. sulphur is worked in coordination with a cultural method for denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that specifically comprising following steps:
(1) the sludge acclimatization stage: add the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur in reactor, intake as containing the waste water of carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion, start reactor and start the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add nitrate as nitrogenous source, reactor enters anoxic and inhales the phosphorus stage; When phosphorus source, clearance reaches more than 20%, and nitrate removal rate reaches 80～100%, sludge volume index SVI
5lower than 80mL/g, SVI
30during lower than 35mL/g, the domestication stage finishes;
(2) the granule sludge stage of growth: after the domestication stage finishes, continue to add the waste water that contains carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion in reactor, reactor enters the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add and start anoxic after nitrate and inhale the phosphorus stage, the median size of periodic measurement active sludge, when its median size reaches 85～100 μ m, can think that the Granular sludge formation stage finishes;
(3) the granule sludge stage of maturity: after the Granular sludge formation stage finishes, continue to add the waste water that contains carbon source, sulphur source, phosphorus source, calcium ion and magnesium ion in reactor, carry out the anaerobic phosphorus release stage; After carbon source concentration drops to zero, add nitrate reaction device and enter the anoxic suction phosphorus stage, granule sludge is mutually assembled and is formed larger particles mud in reactor, measure its median size and reach 110～120 μ m, the clearance in phosphorus source is higher than 70%, nitrate removal rate higher than 90% time, can think that granule sludge is tending towards ripe.
2. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
Described carbon source is organic carbon source, by sodium-acetate, is provided; In described waste water, acetate starting point concentration is 150mg C/L;
Described sulphur source is provided by sodium sulfate, and described sulfate radical in waste water starting point concentration is 200mg S/L;
Described phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate; The starting point concentration of described Phosphorus From Wastewater acid group is 20mg P/L.
3. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
Described calcium ion is provided by calcium chloride, and in described waste water, the starting point concentration of calcium ion is 18～20mgCa
2+/ L;
Described magnesium ion is provided by magnesium chloride, and in described waste water, the starting point concentration of magnesium ion is 9～10mgMg
2+/ L.
4. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
Nitrate described in step (1), (2) and (3) is provided by saltpetre, adds after nitrate, and the final concentration of nitrate in reactor is 20～50mg N/L.
5. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
Process conditions in step (1) is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 150rpm mechanical stirring, 20～25 ℃ of temperature of reaction, and water inlet pH6.8～7.3, hydraulic detention time remains on 12～16h.
6. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
In step (2), process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts slow speed of revolution 120rpm mechanical stirring, 20～25 ℃ of temperature of reaction, and water inlet pH6.8～7.3, hydraulic detention time remains on 12～16h.
7. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
In step (3), process conditions is: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, adopts the slow speed of revolution 120～150rpm mechanical stirring, 20～25 ℃ of temperature of reaction, and water inlet pH6.8～7.3, hydraulic detention time remains on 10～12h.
8. sulphur according to claim 1 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
Described reactor is sequencing batch reactor activated sludge reaction device;
The collaborative denitrification nitrogen and phosphorus removal seed sludge of described sulphur is mud mixture, and its sludge concentration is 9～12g SS/L.
9. sulphur according to claim 8 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
The collaborative denitrification nitrogen and phosphorus removal seed sludge of described sulphur, its preparation method comprises following concrete steps:
1. in reactor, add anaerobic activated sludge to carry out sludge acclimatization, the situation of intaking and existing with acclimated microorganism adaptation phosphorus source for the waste water that contains carbon source, He Lin source, sulphur source; The domestication initial stage, the adding of nitrate-free;
2. when sulfide generation reach system total sulfur 15% time, adopt anaerobic phosphorus release-anoxic to inhale phosphorus mode and carry out the further domestication of active sludge and cultivate; Wherein, the waste water that contains carbon source, He Lin source, sulphur source enters reactor and starts the anaerobic phosphorus release stage, and the anaerobic phosphorus release stage is consistent with first stage method is adding of anaerobism section nitrate-free; When carbon source concentration drops to zero, start to add nitrate as nitrogenous source, start anoxic and inhale the phosphorus stage, and the concentration after nitrate adds in reactor is increased to 20mg N/L gradually by 5mg N/L, the object of progressively taming to reach microorganism, and then obtain the collaborative denitrification nitrogen and phosphorus removal seed sludge of sulphur.
10. sulphur according to claim 9 is worked in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge, it is characterized in that:
Step 1., the carbon source described in is 2. organic carbon source, by sodium-acetate, provided; In the described waste water that contains carbon source, He Lin source, sulphur source, acetate starting point concentration is 150mg C/L; Described sulphur source is provided by sodium sulfate, and the described sulfate radical in waste water starting point concentration that contains carbon source, He Lin source, sulphur source is 200mg S/L; Described phosphorus source is provided by dipotassium hydrogen phosphate and potassium primary phosphate; The starting point concentration of the described Phosphorus From Wastewater acid group that contains carbon source, He Lin source, sulphur source is 20mg P/L; Described nitrate is saltpetre;
The anaerobic activated sludge of step described in is 1. that muddy water mixes, and its sludge concentration is 5.98g SS/L;
Step process conditions is 1.: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, stirring velocity 400rpm, 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time 100～136h;
Step process conditions is 2.: adopt mechanical stirring, stirring rake is that standard four leaves are spiral, stirring velocity 400rpm, 20～25 ℃ of temperature of reaction, water inlet pH6.8～7.3, hydraulic detention time 68～100h;
The step reaction times is 1. 0.5～1 month, and the step reaction times is 2. 1.5～3 months.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410326806.XA CN104098172B (en) | 2014-07-09 | 2014-07-09 | A kind of sulphur works in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410326806.XA CN104098172B (en) | 2014-07-09 | 2014-07-09 | A kind of sulphur works in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104098172A true CN104098172A (en) | 2014-10-15 |
| CN104098172B CN104098172B (en) | 2015-10-28 |
Family
ID=51666768
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410326806.XA Active CN104098172B (en) | 2014-07-09 | 2014-07-09 | A kind of sulphur works in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104098172B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105540834A (en) * | 2015-12-29 | 2016-05-04 | 杭州师范大学 | Culture method of anaerobic denitrification granular sludge |
| CN107673466A (en) * | 2017-09-29 | 2018-02-09 | 广州市香港科大霍英东研究院 | A kind of method of quick domestication sulfur cycle coupling denitrification dephosphorization system |
| CN111138055A (en) * | 2020-01-10 | 2020-05-12 | 重庆市环卫集团有限公司 | Method for cultivating high-temperature anaerobic granular sludge for kitchen waste treatment |
| CN116062884A (en) * | 2023-02-02 | 2023-05-05 | 华中科技大学 | Method for strengthening denitrification dephosphorization efficiency of low-carbon source sewage by using elemental sulfur |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302058A (en) * | 2008-07-04 | 2008-11-12 | 哈尔滨工业大学 | Method for removing sulphur and nitrogen in inorganic waste water synchronously |
| CN101781019A (en) * | 2010-01-08 | 2010-07-21 | 河海大学 | Anaerobic dephosphorizing method based on methanation, anaerobic ammonium oxidation and denitrification coupling process |
-
2014
- 2014-07-09 CN CN201410326806.XA patent/CN104098172B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302058A (en) * | 2008-07-04 | 2008-11-12 | 哈尔滨工业大学 | Method for removing sulphur and nitrogen in inorganic waste water synchronously |
| CN101781019A (en) * | 2010-01-08 | 2010-07-21 | 河海大学 | Anaerobic dephosphorizing method based on methanation, anaerobic ammonium oxidation and denitrification coupling process |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105540834A (en) * | 2015-12-29 | 2016-05-04 | 杭州师范大学 | Culture method of anaerobic denitrification granular sludge |
| CN107673466A (en) * | 2017-09-29 | 2018-02-09 | 广州市香港科大霍英东研究院 | A kind of method of quick domestication sulfur cycle coupling denitrification dephosphorization system |
| CN111138055A (en) * | 2020-01-10 | 2020-05-12 | 重庆市环卫集团有限公司 | Method for cultivating high-temperature anaerobic granular sludge for kitchen waste treatment |
| CN116062884A (en) * | 2023-02-02 | 2023-05-05 | 华中科技大学 | Method for strengthening denitrification dephosphorization efficiency of low-carbon source sewage by using elemental sulfur |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104098172B (en) | 2015-10-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112250180B (en) | Device and method for realizing deep denitrification of domestic sewage by coupling half-shortcut nitrification-anaerobic ammonia oxidation with sulfur autotrophic denitrification | |
| JP5685265B2 (en) | Sludge treatment method using sludge biological treatment method, and sludge treatment apparatus and apparatus | |
| CN104098177B (en) | A kind of sulphur works in coordination with the method for wastewater treatment of denitrification synchronous denitrification dephosphorizing | |
| CN101891343B (en) | Method for biologically purifying municipal sewage and recovering resources | |
| CN104961305B (en) | A kind of processing method of livestock breeding wastewater anaerobic fermented liquid | |
| CN103241908B (en) | Large-scale pig farm wastewater treatment method | |
| CN104230097A (en) | Breeding sewage treatment method | |
| CN101759338B (en) | Method for reducing biological sludge by using ozone oxidation | |
| CN111137973A (en) | Denitrification functional filler, filler ball, filling method and application | |
| CN102775019A (en) | Coupling type sewage de-phosphorization purification regeneration treatment technique | |
| CN103896442A (en) | Pig farm wastewater treatment method | |
| CN103121754A (en) | Denitrification and dephosphorization technique | |
| CN105417687A (en) | Method and device for performing combined treatment on sewage and bottom mud in black-odor riverway | |
| CN104098172B (en) | A kind of sulphur works in coordination with the cultural method of denitrification synchronous denitrification dephosphorizing granule sludge | |
| CN102344197A (en) | Method for rapidly starting anaerobic ammonium oxidation reactor | |
| CN107522367A (en) | A kind of processing method of city black and odorous water and application | |
| CN105036489A (en) | Livestock/poultry culture wastewater deep denitrification and dephosphorization standard treatment device and process | |
| CN110723812B (en) | Method for improving pH impact resistance of anaerobic ammonium oxidation particles | |
| CN104609651B (en) | A kind of Large-scale pig farm advanced waste treatment system | |
| CN109867352B (en) | Method for realizing autotrophic deep denitrification of nitrogen-containing wastewater by utilizing anaerobic MBR (membrane bioreactor) | |
| CN113716689B (en) | Mixed nutrition type denitrification method based on sulfur reduction and sulfur autotrophic denitrification | |
| CN108793656B (en) | Method for improving purity of methane in biogas generated by anaerobic digestion of sludge | |
| CN105366889B (en) | A kind of town sewage high standard denitrification dephosphorization system without additional carbon | |
| CN113023871A (en) | Device and method for synchronously treating domestic sewage and late-stage landfill leachate by virtue of shortcut nitrification-anaerobic ammonia oxidation coupling denitrification process | |
| CN102126813B (en) | System and process for treating oxytetracycline waste water by anaerobic bio-treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |