CN107010781A - The biochemical processing method and its process system of high ammonia nitrogen organic wastewater - Google Patents
The biochemical processing method and its process system of high ammonia nitrogen organic wastewater Download PDFInfo
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Abstract
The present invention provides a kind of biochemical processing method and its process system of high ammonia nitrogen organic wastewater.The process system includes：It is sequentially connected logical anoxic pond, Aerobic Pond, first stage precipitation tank, contact-oxidation pool and second-level settling pond；The activated sludge outlet of first stage precipitation tank is connected with anoxic pond；The mixture export of contact-oxidation pool is connected with anoxic pond.This method is as follows：The activated sludge of one-level precipitation process returns to anoxic treatment with 200%~500% reflux ratio；Nitrification processing is catalytic oxidation form, and the mixed liquor of nitrification processing returns to anoxic treatment with 200%~400% reflux ratio；The salt content of waste water is less than 1%, B/C and is more than 0.35.This method and system can by ammonia-nitrogen content below 1000mg/L wastewater treatment to below 15mg/L, reduce by 40% and 20% respectively compared to dilution biochemical process base amount and oxygen-supplying amount, can significantly reduce biochemistry pool volume, reduction construction cost and operating cost.
Description
Technical field
The present invention relates to a kind of biochemical processing method and its process system of high ammonia nitrogen organic wastewater.
Background technology
Typically it is divided to for treatment of Organic Wastewater containing ammonia nitrogen from the aspect of two：In a first aspect, for high ammonia nitrogen organic wastewater one
As pre-processed using the processing method of materialization, mainly have stripping, evaporative crystallization, stripping, break oxychloride, MAP methods, typically
In the case of stripping, evaporative crystallization or break oxychloride method ammonia nitrogen in high density can be directly down to very low level, direct satisfaction
Requirement of the discharge standard to ammonia nitrogen, and ammonia nitrogen can only be typically down to than relatively low level by stripping or MAP methods, it is impossible to meet straight
Emission request is connect, it is necessary to follow-up further processing；Second aspect is general using work for the ammonia nitrogen organic wastewater of low concentration
Property sludge biochemical process is handled, and traditional handling process has A/O techniques, SBR techniques, oxidation ditch process.
At present, typically take the processing method that " materialization+biochemistry " is combined to carry out for high ammonia nitrogen organic wastewater, first use
Ammonia nitrogen in waste water is down to below 200mg/L by the processing means of materialization, then carries out biochemical treatment.And physical chemistry method handles high ammonia nitrogen and had
The cost of machine waste water is very high, and can produce secondary pollution, the ammoniacal liquor of such as low concentration, abraum salt, Waste Sulfuric Acid ammonium, ammonium magnesium phosphate, useless
Gas pollution etc., causes business burden weight, environmental protection pressure big.
The content of the invention
The technical problems to be solved by the invention are to overcome the processing cost of high ammonia nitrogen organic wastewater in the prior art
Height, and the defect of secondary pollution can be produced, and a kind of biochemical treatment side of more economical, more environmentally friendly high ammonia nitrogen organic wastewater is provided
Method and its process system.
The present invention provides a kind of biochemical processing method of high ammonia nitrogen organic wastewater, and it comprises the following steps：High ammonia nitrogen is organic
Waste water carries out anoxic treatment, Aerobic Process for Treatment, one-level precipitation process, nitrification processing and two-stage precipitation processing successively, you can；Wherein,
Activated sludge obtained by the one-level precipitation process is back to the anoxic treatment with 200%~500% reflux ratio；The nitrification
The form of catalytic oxidation is processed as, the mixed liquor of the nitrification processing is back to the anoxic with 200%~400% reflux ratio
Processing；The salt content of the high ammonia nitrogen organic wastewater is less than 1%, B/C and is more than 0.35.
In the present invention, activated sludge obtained by the one-level precipitation process is preferably returned with 250%~350% reflux ratio
To the anoxic treatment；The mixed liquor of the nitrification processing is preferably back to the anoxic with 200%~250% reflux ratio
Processing.
In the present invention, the high ammonia nitrogen organic wastewater is carried out before biochemical treatment, and activity is first carried out according to this area is conventional
Culturing sludge, for example：Bacterium is added in anoxic treatment, Aerobic Process for Treatment and nitrification processing, is cultivated.At the anoxic
The dosage of bacterium is preferably 2000mg/L in reason, the Aerobic Process for Treatment and the nitrification processing.The activated sludge culture
Time be preferably 20d.
In the present invention, the high ammonia nitrogen organic wastewater is that described in routine, general COD is 4000~4500mg/L, total nitrogen
In below 1000mg/L, pH value is 7.5~8.The total nitrogen of the high ammonia nitrogen organic wastewater is preferably 750~850mg/L.It is described
The C/N of high ammonia nitrogen organic wastewater is preferably 5:1~6:1.For high ammonia nitrogen organic wastewater when being handled using biochemical method, this
Art personnel, which know, should not contain the toxicant for suppressing microorganism normal growth, such as heavy metal, bactericide in waste water；
If, can be according to the conventional pre-treatment side in this area and those skilled in the art know that high ammonia nitrogen organic wastewater is unsatisfactory for These parameters
Method is allowed to meet These parameters, for example：The materials such as SS, oil slick class in waste water can be removed using air supporting or coagulation, can be using mixed
Retrogradation shallow lake removes the heavy metal in waste water, Fenton oxidation can be used simply to crack the molecular structure of useless Organic substance in water useless to remove
Suppress the toxicant of microorganism normal growth in water；If can directly make without SS or floating oily substances in high ammonia nitrogen organic wastewater
Handled with the method for the present invention.
In the present invention, coagulation and mud-water separation are preferably comprised before the anoxic treatment, it is mixed that the coagulation is used
Solidifying agent is preferably aluminium polychloride and PAMA.The time of the coagulation is preferably 15~20min, described
The time of mud-water separation is preferably 1.5~2h.
In the present invention, the anoxic treatment is this area routine operation.The time of the anoxic treatment is preferably 24h.
The hybrid mode of the anoxic treatment is preferably using boring aeration with stirring the hybrid mode being combined.The anoxic treatment
In waste water system, the ORP of the waste water system is preferably less than -100mv.The regulative mode of the ORP is that this area is conventional, when
The ORP of waste water system is higher than -100mv, can be adjusted in the following manner, for example:Anoxic treatment middle punch can suitably be reduced
The aeration intensity of aeration；The oxygen being back in the amount for nitrifying mixed liquor in anoxic treatment or reduction mixed liquor can be suitably reduced to contain
Amount；It can properly increase into water organic loading.The pH value of the waste water system is preferably 7.5~8.The temperature of the waste water system
Preferably 25~35 DEG C.The activated sludge concentration of the waste water system is preferably 5000~6000mg/L.The activity is dirty
In mud, heterotrophic bacterium is preferably 2 with autotroph mass ratio:1.The heterotrophic bacterium and the autotroph
Species can be selected according to kind of waste water.
In the present invention, the Aerobic Process for Treatment is this area routine operation.The time of the Aerobic Process for Treatment is preferably 48h.
In the waste water system of the Aerobic Process for Treatment, the dissolved oxygen of the waste water system is preferably 1~5mg/L, more preferably for 1.5~
3mg/L.The pH value of the waste water system is preferably 7.5~8.The temperature of the waste water system is preferably 25~35 DEG C.Institute
The sludge concentration for stating waste water system is preferably 5000~6000mg/L.In the activated sludge, heterotrophic bacterium and autotrophic type
Bacteriological quality ratio preferably 2:1.The heterotrophic bacterium and the species of the autotroph can be selected according to kind of waste water
Select.
In the present invention, the one-level precipitation process is this area routine operation.The time of the one-level precipitation process is preferable
Ground is 12~14h.The surface loading of the one-level precipitation process is preferably 1~1.2m3/ (m2·h).The one-level place of settling
Reason gained activated sludge is preferably back to the anoxic treatment with 300% reflux ratio.
In the present invention, the nitrification processing is this area routine operation.The time of the nitrification processing is preferably 24h.
In the waste water system of the nitrification processing, the dissolved oxygen of the waste water system is preferably 2~5mg/L, is more preferably 3~4mg/
L.The pH value of the waste water system is preferably 7.0~7.5.The temperature of the waste water system is preferably 25~35 DEG C.It is described
In waste water system, heterotrophic bacterium is preferably 1 with autotrophic type nitrobacteria mass ratio:4.The heterotrophic bacterium with it is described from
The species of the type of supporting bacterium can be selected according to kind of waste water.The mixed liquor of the nitrification processing is preferably with 200% reflux ratio
It is back to the anoxic treatment
In the present invention, the two-stage precipitation is processed as this area routine operation.The time of the two-stage precipitation processing is preferable
Ground is 3~4h.The surface loading of the two-stage precipitation processing is preferably 1.5~2m3/(m2·h)。
The present invention also provides the process system of above-mentioned biochemical processing method, and it includes：Be sequentially connected logical anoxic pond, it is aerobic
Pond, first stage precipitation tank, contact-oxidation pool and second-level settling pond；Activated sludge outlet and the anoxic pond of the first stage precipitation tank
It is connected；The mixture export of the contact-oxidation pool is connected with the anoxic pond.
In the present invention, pre-treatment pond can be also provided with before the anoxic pond, the pre-treatment pond is logical including being sequentially connected
Coagulation reaction tank and coagulative precipitation tank, the coagulation reaction tank are connected with the water inlet pipe of the high ammonia nitrogen organic wastewater, described
Coagulative precipitation tank is connected with residing anoxic pond.
In the present invention, the anoxic pond preferably is provided with boring aeration pipe and agitating paddle.
In the present invention, the first stage precipitation tank is preferably tube settler.
In the present invention, the second-level settling pond is preferably tube settler.
On the basis of common sense in the field is met, above-mentioned each optimum condition can be combined, and produce each preferable reality of the present invention
Example.
Agents useful for same and raw material of the present invention are commercially available.
The positive effect of the present invention is：The biochemical processing method and its technique of the high ammonia nitrogen organic wastewater of the present invention
System, this method and system can by ammonia-nitrogen content below 1000mg/L wastewater treatment to below 15mg/L, compared to dilution life
Change method base amount and oxygen-supplying amount reduce by 40% and 20% respectively, can significantly reduce biochemistry pool volume, reduction construction cost and operation
Cost.This method is used to handle the waste water that influent ammonia nitrogen is below 1000mg/L, and it is comprehensive that water outlet ammonia-nitrogen content can meet national sewage
Close the first grade discharging requirement of discharge standard (GB8978-1996).This method is useless more than 0.4 more than 4, B/C for handling C/N
Water, nitrogen removal rate is up to more than 80%.
Brief description of the drawings
Fig. 1 is the process system schematic diagram of the biochemical processing method of high ammonia nitrogen organic wastewater of the invention.
Fig. 2 is the biochemical processing method schematic diagram of high ammonia nitrogen organic wastewater of the invention.
Embodiment
The present invention is further illustrated below by the mode of embodiment, but does not therefore limit the present invention to described reality
Apply among a scope.The experimental method of unreceipted actual conditions in the following example, conventionally and condition, or according to business
Product specification is selected.
In following embodiments, COD method of testing is used《Water and effluent monitoring analysis method》Fourth edition the 211st~213
The potassium dichromate method that page is recorded；The method of testing of ammonia nitrogen is used《Water and effluent monitoring analysis method》Fourth edition page 278~281
Distillation processing+Berthelot spectrophotometry of record；The method of testing of kjeldahl nitrogen is used《Water and effluent monitoring analysis method》
Distillation processing+Berthelot spectrophotometry of the fourth edition record of page 250~252；The measuring method of total nitrogen uses Hash mistake
Oxide sulfate method, method number 10072.
In following embodiments, high ammonia nitrogen organic wastewater comes from certain benzoguanamine manufacturer, the salt content of the waste water
More than 0.35, C/N it is 5 less than 1%, B/C:1~6:1, COD is 4000~4500mg/L, and total nitrogen is 750~850mg/L, processing
Measure as 500m3/d。
The consumption of autotroph and heterotrophic bacterium is such as in following embodiments, in anoxic pond, Aerobic Pond, contact-oxidation pool
Shown in following table.All bacteriums are Shanghai Mei Jing Ingegneria Ambientale SRL commercially available prod in following table.
Embodiment 1
As shown in figure 1, the process system of the biochemical processing method of the high ammonia nitrogen organic wastewater of the present embodiment, including：Successively
Anoxic pond, Aerobic Pond, first stage precipitation tank, contact-oxidation pool and the second-level settling pond being connected；The activated sludge of first stage precipitation tank
Outlet is connected with anoxic pond；The mixture export of contact-oxidation pool is connected with anoxic pond.Phase successively is additionally provided with before anoxic pond
The coagulation reaction tank and coagulative precipitation tank of connection, coagulation reaction tank are connected with the water inlet pipe of high ammonia nitrogen organic wastewater, and coagulation sinks
Shallow lake pond is connected with residing anoxic pond.
As shown in Fig. 2 the biochemical processing method of the high ammonia nitrogen organic wastewater of the present embodiment, comprises the following steps：
(1) bacterial strain and consumption in upper table are pressed, is added into anoxic pond, Aerobic Pond and contact-oxidation pool, 20d is cultivated, i.e.,
Obtain ripe activated sludge.
(2) pH value of adjustment waste water is to 7.5~8；
(3) waste water is pumped into coagulation reaction tank, aluminium polychloride, PAMA is successively added, in stirring
In the case of carry out coagulation, flocculation reaction, reaction time 20min, after reaction terminates, waste water carries out mud from coagulative precipitation tank is flowed into
Water is separated；
(4) coagulative precipitation tank water outlet is ORP in 24h, control anoxic pond from anoxic pond, anoxic pond hydraulic detention time is flowed into
Less than -100mv, pH is 7.5~8, and temperature is 25~28 DEG C, and activated sludge concentration is in 6000mg/L；
(5) anoxic pond water outlet is 48h from Aerobic Pond, Aerobic Pond hydraulic detention time is flowed into, and control Aerobic Pond dissolved oxygen exists
2mg/L, pH are 7.5~8, and temperature is 25~28 DEG C, and activated sludge concentration is in 6000mg/L；
(6) Aerobic Pond water outlet is from first stage precipitation tank is flowed into, and the surface area of first stage precipitation tank is 60m2, activated sludge with
300% reflux ratio returns to anoxic pond；
(7) first stage precipitation tank water outlet is 24h from contact-oxidation pool, contact-oxidation pool hydraulic detention time is flowed into, and is controlled molten
Oxygen is solved in 4mg/L, temperature is 25~28 DEG C, and mixed liquor returns to anoxic pond with 200% reflux ratio；
(8) contact-oxidation pool water outlet is from second-level settling pond is flowed into, and the surface area of second-level settling pond is 15m2, standard water discharge row
Put.
Effect data：Water outlet COD is 200mg/L, and ammonia nitrogen is 2mg/L, and kjeldahl nitrogen is in 14mg/L, and total nitrogen is 141mg/L, alkali
Consumption is 4.5t/d (30% sodium hydroxide), meets locality and receives pipe emission request.
Embodiment 2
(1) bacterial strain and consumption in upper table are pressed, is added into anoxic pond, Aerobic Pond and contact-oxidation pool, 20d is cultivated, i.e.,
Obtain ripe activated sludge.
(2) pH value of adjustment waste water is to 7.5~8；
(3) waste water is pumped into coagulation reaction tank, aluminium polychloride, PAMA is successively added, in stirring
In the case of carry out coagulation, flocculation reaction, reaction time 15min, after reaction terminates, waste water carries out mud from coagulative precipitation tank is flowed into
Water is separated；
(4) coagulative precipitation tank water outlet is ORP in 24h, control anoxic pond from anoxic pond, anoxic pond hydraulic detention time is flowed into
Less than -100mv, pH is 7.5~8, and temperature is 28~32 DEG C, and activated sludge concentration is in 5000mg/L；
(5) anoxic pond water outlet is 48h from Aerobic Pond, Aerobic Pond hydraulic detention time is flowed into, and control Aerobic Pond dissolved oxygen exists
1.5mg/L, pH are 7.5~8, and temperature is 28~32 DEG C, and activated sludge concentration is in 5000mg/L；
(6) Aerobic Pond water outlet is from first stage precipitation tank is flowed into, and the surface area of first stage precipitation tank is 60m2, activated sludge with
250% reflux ratio returns to anoxic pond；
(7) first stage precipitation tank water outlet is 24h from contact-oxidation pool, contact-oxidation pool hydraulic detention time is flowed into, and is controlled molten
Oxygen is solved in 3mg/L, pH is 7.0~7.5, and temperature is 28~32 DEG C, and mixed liquor returns to anoxic pond with 250% reflux ratio；
(8) contact-oxidation pool water outlet is from second-level settling pond is flowed into, and the surface area of second-level settling pond is 15m2, standard water discharge row
Put.
Effect data：Water outlet COD is 186mg/L, and ammonia nitrogen is 2.5mg/L, and kjeldahl nitrogen is in 13mg/L, and total nitrogen is 132mg/L,
Base amount is 4.2t/d (30% sodium hydroxide), meets locality and receives pipe emission request.
Embodiment 3
(1) bacterial strain and consumption in upper table are pressed, is added into anoxic pond, Aerobic Pond and contact-oxidation pool, 20d is cultivated, i.e.,
Obtain ripe activated sludge.
(2) pH value of adjustment waste water is to 7.5~8；
(3) waste water is pumped into coagulation reaction tank, aluminium polychloride, PAMA is successively added, in stirring
In the case of carry out coagulation, flocculation reaction, reaction time 20min, after reaction terminates, waste water carries out mud from coagulative precipitation tank is flowed into
Water is separated；
(4) coagulative precipitation tank water outlet is ORP in 24h, control anoxic pond from anoxic pond, anoxic pond hydraulic detention time is flowed into
Less than -100mv, pH is 7.5~8, and temperature is 30~35 DEG C, and activated sludge concentration is in 5000mg/L；
(5) anoxic pond water outlet is 48h from Aerobic Pond, Aerobic Pond hydraulic detention time is flowed into, and control Aerobic Pond dissolved oxygen exists
3mg/L, pH are 7.5~8, and temperature is 30~35 DEG C, and activated sludge concentration is in 5000mg/L；
(6) Aerobic Pond water outlet is from first stage precipitation tank is flowed into, and the surface area of first stage precipitation tank is 60m2, activated sludge with
350% reflux ratio returns to anoxic pond；
(7) first stage precipitation tank water outlet is 24h from contact-oxidation pool, contact-oxidation pool hydraulic detention time is flowed into, and is controlled molten
Oxygen is solved in 3mg/L, pH is 7.0~7.5, and temperature is 30~35 DEG C, and mixed liquor returns to anoxic pond with 200% reflux ratio；
(8) contact-oxidation pool water outlet is from second-level settling pond is flowed into, and the surface area of second-level settling pond is 15m2, standard water discharge row
Put.
Effect data：Water outlet COD is 221mg/L, and ammonia nitrogen is 1.4mg/L, and kjeldahl nitrogen is in 11mg/L, and total nitrogen is 127mg/L,
Base amount is 4.4t/d (30% sodium hydroxide), meets locality and receives pipe emission request.
Claims (10)
1. a kind of biochemical processing method of high ammonia nitrogen organic wastewater, it is characterised in that it comprises the following steps：High ammonia nitrogen organic waste
Water carries out anoxic treatment, Aerobic Process for Treatment, one-level precipitation process, nitrification processing and two-stage precipitation processing successively, you can；Wherein, institute
Activated sludge obtained by stating one-level precipitation process is back to the anoxic treatment with 200%~500% reflux ratio；At the nitrification
The form for catalytic oxidation is managed, the mixed liquor of the nitrification processing is back at the anoxic with 200%~400% reflux ratio
Reason；The salt content of the high ammonia nitrogen organic wastewater is less than 1%, B/C and is more than 0.35.
2. biochemical processing method as claimed in claim 1, it is characterised in that activated sludge obtained by the one-level precipitation process with
250%~350% reflux ratio is back to the anoxic treatment；The mixed liquor of the nitrification processing is with 200%~250% time
Stream is than being back to the anoxic treatment.
3. biochemical processing method as claimed in claim 1, it is characterised in that the C/N of the high ammonia nitrogen organic wastewater is 5:1~
6:1, the COD of the high ammonia nitrogen organic wastewater is 4000~4500mg/L, and the total nitrogen of the high ammonia nitrogen organic wastewater is in 1000mg/
Below L, the pH value of the high ammonia nitrogen organic wastewater is 7.5~8；The total nitrogen of the high ammonia-nitrogen wastewater is preferably 750~
850mg/L。
4. biochemical processing method as claimed in claim 1, it is characterised in that include coagulation and muddy water before the anoxic treatment
Separation, the coagulant that the coagulation is used is aluminium polychloride and PAMA, and the time of the coagulation is 15
~20min, the time of the mud-water separation is 1.5~2h.
5. biochemical processing method as claimed in claim 1, it is characterised in that the time of the anoxic treatment is 24h, described to lack
The hybrid mode of oxygen processing is using boring aeration with stirring the hybrid mode being combined；In the waste water system of the anoxic treatment,
The ORP of the waste water system is less than -100mv；The pH value of the waste water system is 7.5~8；The temperature of the waste water system is 25
~35 DEG C；The activated sludge concentration of the waste water system is 5000~6000mg/L；In the activated sludge, heterotrophic bacterium with
Autotroph mass ratio is 2:1；Or,
The time of the Aerobic Process for Treatment is 48h；In the waste water system of the Aerobic Process for Treatment, the dissolved oxygen of the waste water system is 1
~5mg/L, preferably 1.5~3mg/L；The pH value of the waste water system is 7.5~8；The temperature of the waste water system is 25
~35 DEG C；The sludge concentration of the waste water system is 5000~6000mg/L；In the activated sludge, heterotrophic bacterium and autotrophy
Type bacteriological quality ratio is 2:1.
6. biochemical processing method as claimed in claim 1, it is characterised in that the time of the one-level precipitation process is 12~
14h；The surface loading of the one-level precipitation process is 1~1.2m3/(m2·h)；Or,
The time of the two-stage precipitation processing is 3~4h；The surface loading of the two-stage precipitation processing is 1.5~2m3/(m2·
h)。
7. biochemical processing method as claimed in claim 1, it is characterised in that the time of the nitrification processing is 24h；The nitre
In the waste water system for changing processing, the dissolved oxygen of the waste water system is 2~5mg/L, preferably 3~4mg/L；The waste water body
The pH value of system is 7.0~7.5；The temperature of the waste water system is 25~35 DEG C；In the waste water system, heterotrophic bacterium with from
It is 1 to support type nitrobacteria mass ratio:4.
8. a kind of process system of the biochemical processing method described in use claim any one of 1-7, it is characterised in that the work
Process system includes：It is sequentially connected logical anoxic pond, Aerobic Pond, first stage precipitation tank, contact-oxidation pool and second-level settling pond；Described one
The activated sludge outlet of level sedimentation basin is connected with the anoxic pond；The mixture export of the contact-oxidation pool and the anoxic
Pond is connected.
9. process system as claimed in claim 8, it is characterised in that pre-treatment pond is additionally provided with before the anoxic pond, described
The pre-treatment pond coagulation reaction tank logical including being sequentially connected and coagulative precipitation tank, the coagulation reaction tank and the high ammonia nitrogen are organic
The water inlet pipe of waste water is connected, and the coagulative precipitation tank is connected with residing anoxic pond.
10. process system as claimed in claim 8, it is characterised in that the anoxic pond is provided with boring aeration pipe and agitating paddle；
The first stage precipitation tank is tube settler；The second-level settling pond is preferably tube settler.
Priority Applications (1)
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