CN106542632A - A kind of method for starting nitration reaction under micro-oxygen conditions - Google Patents
A kind of method for starting nitration reaction under micro-oxygen conditions Download PDFInfo
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- CN106542632A CN106542632A CN201610963763.5A CN201610963763A CN106542632A CN 106542632 A CN106542632 A CN 106542632A CN 201610963763 A CN201610963763 A CN 201610963763A CN 106542632 A CN106542632 A CN 106542632A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
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- 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
- C02F3/1278—Provisions for mixing or aeration of the mixed liquor
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2101/00—Nature of the contaminant
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- C02F2101/206—Manganese or manganese compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/003—Downstream control, i.e. outlet monitoring, e.g. to check the treating agents, such as halogens or ozone, leaving the process
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/15—N03-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C—CHEMISTRY; METALLURGY
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/38—Gas flow rate
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention belongs to ammonia nitrogen waste water process field, discloses a kind of method for starting nitration reaction under micro-oxygen conditions.Described application is wastewater processing technology, is comprised the following steps：(1) plant mud to purchase；(2) plant mud inoculation；(3) bio-film colonization；(4) startup optimization.The present invention is that the steady growth of nitrifier can be still kept under micro-oxygen conditions, strengthens nitration reaction, and significantly reduces the aeration rate during nitrification system running, saves energy input, its operating cost is greatly reduced.
Description
Technical field
The invention belongs to nitrogen-containing wastewater process field, and in particular to start the side of nitration reaction under a kind of micro-oxygen conditions
Method, mainly for the treatment of ammonia nitrogen waste water.
Background technology
China is ammonia nitrogen waste water discharge rich and influential family, and chemical fertilizer, coking, petrochemical industry, pharmacy, food, refuse landfill etc. are that ammonia nitrogen gives up
The main source of water.After these waste water enter water body, body eutrophication can be caused, cause black and odorous water, increase wastewater treatment
Technical difficulty and Financial cost, affect crowd and bioenvironmental environmental health.
Traditional biological denitrificaion mainly adopts nitrification-denitrification denitrogenation technology, specially：In aerobic environment, ammonia nitrogen exists
It is oxidized to cultured water in the presence of aerobic ammonia-oxidizing bacteria, cultured water is oxidized to nitric acid again in the presence of nitrifier
Nitrogen；In anaerobic environment, nitrate nitrogen is reduced to nitrogen in the presence of denitrifying bacterium, so as to ammonia nitrogen is removed from water body.
Wherein, significant difference is existed to the demand of DO in reaction system in nitrification stage, aerobic ammonia-oxidizing bacteria and nitrifier, i.e.,：When
In reaction system during DO >=0.3mg/L, you can nitrosification occurs, and (ammonium oxidation can be nitrous acid by aerobic ammonia-oxidizing bacteria
Nitrogen), as DO >=2.0mg/L in reaction system, Nitrification (cultured water is oxidized to nitrate nitrogen by nitrifier) can just occur.
To realize the synergism of two kinds of biochemical reactions, it will usually require DO >=2.0mg/L in whole reaction system, this will cause in reality
In the running of border, aeration rate is larger, energy consumption is larger, it is higher to the technical requirements of aerator the problems such as.Additionally, nitrobacteria
One of generation time itself is long, and breeding is slow, and the technical bottleneck of whole denitrification process.
The content of the invention
Present invention is primarily targeted at overcoming the shortcoming and deficiency of prior art, there is provided start nitre under a kind of micro-oxygen conditions
The method for changing reaction, the method is while nitrifier steady growth is ensured, it is possible to decrease aeration rate, so as to significantly reduce energy consumption,
And alleviate problem higher to aerator technical requirements at present.
In order to achieve the above object, the present invention is employed the following technical solutions：
The invention provides a kind of method for starting nitration reaction under micro-oxygen conditions, comprises the steps：
A () takes the ordinary activated sludge of urban wastewater treatment firm second pond as kind of a mud, MLSS is in 3000-4000mg/L models
In enclosing, Jing after 24h precipitations, in the range of 14000-14500mg/L, MLVSS is in the range of 8000-8500mg/L for MLSS；
B () is passed through the kind mud in step (a) after air aeration 72h, adjustment sludge concentration is in 14000-14500mg/L models
In enclosing；
C SBAF reactor bottoms in step (b) are passed through pure nitrogen gas by (), air pressure is controlled in the range of 0.1-0.2Mpa,
And it is continually fed into a period of time.After stopping logical nitrogen, excess sludge is discharged from reactor bottom mud discharging mouth；
D () will be intake and be sent in the successful SBAF reactors of Jing steps (c) biofilm, and expose micro sky from the reactor bottom
Gas so that DO is controlled in the range of 0.2-0.3mg/L in reaction system；
Water inlet in (e) step (d) to add the artificial distribution that the pure medicament of chemical analyses is made in tap water, its composition and
Concentration is respectively：NH4Cl 0.37-0.42g/L, KH2PO40.03g/L, MgSO40.02g/L, CaCl20.03g/L, NaHCO3
1.0-1.5g/L, trace element solution 0.30ml/L, wherein, trace element solution composition and concentration are FeCl3·6H2O
3.515g/L, MnCl2·4H2O 0.359g/L, CuSO4·5H2O 0.075g/L, ZnSO4·7H2O 0.300g/L, CoCl2·
6H2O 0.375g/L；
F () continuously enters reactor start-up operation using the artificial distribution in step (e), and periodically arrange bed mud, when the body
When being that water outlet nitrate nitrogen is more than 6.0mg/L, DO is adjusted in the range of 0.1-0.2mg/L, water temperature is controlled in 30-40 DEG C of scope
Interior, hydraulic detention time is controlled to 24h, systems stay operation.
As preferred technical scheme, in step (a), described kind of mud pH is in the range of 7.0-7.2.
Used as preferred technical scheme, step (b) is further included：
Take the 2.5L sludge and pour into and be hung with the submerged bacteria filter reactor that combined stuffing, dischargeable capacity are 3L.
Used as preferred technical scheme, the time that pure nitrogen gas are continually fed in step (c) is 72 hours.
As preferred technical scheme, in step (d), system water temperature control in the range of 30 ± 2 DEG C, during hydraulic retention
Between be controlled to 24h.
As preferred technical scheme, in step (f), artificial distribution continuously enters reactor operation and starts, and the process is needed
Bed mud is arranged periodically.
The present invention compared with prior art, has the advantage that and beneficial effect：
(1) the usual inoculation of activated-sludge of routine techniquess, exposes air manner using a large amount of, starts nitration reaction system.This
Activated sludge is first passed through aeration purification by bright technology, then through pure nitrogen gas biofilm, finally starts nitration reaction using micro- oxygen aeration
System, this will significantly reduce the aeration rate in nitrification system start-up course, save energy input.
(2) routine techniquess need reaction system to remain DO >=2.0mg/L, it is ensured that nitrobacteria in start-up course
Primary demand to DO.The technology of the present invention only need to control DO in reaction system in the range of 0.2-0.3mg/L, you can ensure nitre
Change primary demand of the antibacterial to DO, when the system water outlet nitrate nitrogen is more than 6.0mg/L, then DO is adjusted to into 0.1-0.2mg/L
In the range of, can still strengthen nitration reaction, this by significantly reduce nitrification system running during aeration rate, save energy input,
Operating cost is greatly reduced, and reduction is large-minded to air feed equipment device, improve the technical requirements such as its stable work in work.
Description of the drawings
Fig. 1 is the technical method operation implementing procedure figure of the present invention；
Fig. 2 is the start-up course result data figure of the present invention.
Specific embodiment
With reference to embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited
In this.
Embodiment
Certain nitrogen-containing wastewater water quality parameters is as follows：PH 7.8-8.3, CODcr0-10mg/L, NH4 +-N 80-
120mg/L, NO2 -- N 0.0mg/L, NO3 --N 2.0-2.3mg/L。
The present invention technological process be：
(1) plant mud to purchase.The ordinary activated sludge of urban wastewater treatment firm second pond is taken as kind of a mud, color is pale yellow brown
Color, in the range of 7.0-7.2, MLSS is in the range of 3000-4000mg/L for pH.Jing after 12h precipitations, MLSS is in 14000-
In the range of 14500mg/L, MLVSS is in the range of 8000-8500mg/L；
(2) inoculation kind mud.By the kind mud in step (1) Jing after air aeration 72h, adjustment sludge concentration is in 14000-
In the range of 14500mg/L.Take the 2.5L sludge and pour into and be hung with the SBAF reactors that combined stuffing, dischargeable capacity are 3L；
(3) bio-film colonization.SBAF reactor bottoms in step (2) are passed through into pure nitrogen gas, air pressure is controlled in 0.1-
In the range of 0.2Mpa, and it is continually fed into 72h.Sludge in reactor is gradually adhered to combined stuffing surface, and color by yellowish-brown
Complexion changed is black, after now stopping logical nitrogen and standing 2h, excess sludge is discharged from reactor bottom mud discharging mouth；
(4) startup optimization.To be intake in the successful SBAF reactors of water sample feeding Jing steps (3) biofilm with constant flow pump, and
Micro- oxygen aeration is carried out from the reactor bottom so that DO is controlled in the range of 0.2-0.3mg/L in reaction system.Secondly, the body
Be water temperature control in the range of 30 ± 2 DEG C, hydraulic detention time is controlled to 24h.
(5) start successfully.Reactor continuously runs startup, and bed mud is periodically arranged in start-up course.When the system goes out liquid glauber salt
When sour nitrogen is more than 6.0mg/L, DO is adjusted in the range of 0.1-0.2mg/L, in the range of 30-40 DEG C, waterpower is stopped for water temperature control
Time control is stayed to be 24h.Systems stay runs.
The wastewater effluent technical parameter of Jing present invention process process is as shown in table 1.
1 each parameter comparison table of table
| Parameter | Routine techniquess start method | The technology of the present invention starts method |
| Water temperature (DEG C) | Room temperature | Early stage 30 ± 2, later stage 30-40 |
| DO(mg/L) | ≥2.0 | Early stage 0.2-0.3, later stage 0.1-0.2 |
| Startup cycle (d) | ≥30 | 40 |
Above-described embodiment is the present invention preferably embodiment, but embodiments of the present invention not by above-described embodiment
Limit, other any spirit without departing from the present invention and the change, modification, replacement made under principle, combine, simplification,
Equivalent substitute mode is should be, is included within protection scope of the present invention.
Claims (6)
1. a kind of method for starting nitration reaction under micro-oxygen conditions, it is characterised in that：Comprise the steps：
A () takes the ordinary activated sludge of urban wastewater treatment firm second pond as kind of a mud, MLSS is in 3000-4000mg/L scopes
Interior, Jing after 24h precipitations, in the range of 14000-14500mg/L, MLVSS is in the range of 8000-8500mg/L for MLSS；
B () is passed through the kind mud in step (a) after air aeration 72h, adjustment sludge concentration is in 14000-14500mg/L scopes
It is interior；
C SBAF reactor bottoms in step (b) are passed through pure nitrogen gas by (), air pressure is controlled in the range of 0.1-0.2Mpa, and is held
Continue after being passed through the logical nitrogen of a period of time stopping, excess sludge is discharged from reactor bottom mud discharging mouth；
D () will be intake and be sent in the successful SBAF reactors of Jing steps (c) biofilm, and expose micro-air from the reactor bottom,
So that DO is controlled in the range of 0.2-0.3mg/L in reaction system；
E artificial distribution that the water inlet in () step (d) is made into for the pure medicament of addition chemical analyses in tap water, its composition and concentration
Respectively：NH4Cl 0.37-0.42g/L, KH2PO40.03g/L, MgSO40.02g/L, CaCl20.03g/L, NaHCO3
1.0-1.5g/L, trace element solution 0.30ml/L, wherein, trace element solution composition and concentration are FeCl3·6H2O
3.515g/L, MnCl2·4H2O 0.359g/L, CuSO4·5H2O 0.075g/L, ZnSO4·7H2O 0.300g/L, CoCl2·
6H2O 0.375g/L；
F () continuously enters reactor start-up operation using the artificial distribution in step (e), and periodically arrange bed mud, when the system goes out
When water nitrate nitrogen is more than 6.0mg/L, DO is adjusted in the range of 0.1-0.2mg/L, water temperature control in the range of 30-40 DEG C, water
The power time of staying is controlled to 24h, systems stay operation.
2. the method for starting nitration reaction under micro-oxygen conditions according to claim 1, it is characterised in that：In step (a), institute
Kind of mud pH is stated in the range of 7.0-7.2.
3. the method for starting nitration reaction under micro-oxygen conditions according to claim 1, it is characterised in that：Enter in step (b)
One step includes：
Take the 2.5L sludge and pour into and be hung with the SBAF reactors that combined stuffing, dischargeable capacity are 3L.
4. the method for starting nitration reaction under micro-oxygen conditions according to claim 1, it is characterised in that：Hold in step (c)
The continuous time for being passed through pure nitrogen gas is 72 hours.
5. the method for starting nitration reaction under micro-oxygen conditions according to claim 1, it is characterised in that：In step (d), should
In the range of 30 ± 2 DEG C, hydraulic detention time is controlled to 24h to the control of system water temperature.
6. the method for quick startup whole process autotrophic denitrification according to claim 1, it is characterised in that：In step (f), manually
Water distribution continuously enters reactor operation and starts, and the process needs periodically row's bed mud.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445603A (en) * | 2013-09-16 | 2015-03-25 | 中国石油化工股份有限公司 | Method for rapidly starting up-flow reactor through denitrification |
| CN103663679B (en) * | 2012-09-19 | 2015-08-19 | 中国石油化工股份有限公司 | Pure oxygen aeration is utilized to carry out the method for low-carbon high-nitrogen sewage nitration reaction |
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- 2016-10-28 CN CN201610963763.5A patent/CN106542632B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103663679B (en) * | 2012-09-19 | 2015-08-19 | 中国石油化工股份有限公司 | Pure oxygen aeration is utilized to carry out the method for low-carbon high-nitrogen sewage nitration reaction |
| CN104445603A (en) * | 2013-09-16 | 2015-03-25 | 中国石油化工股份有限公司 | Method for rapidly starting up-flow reactor through denitrification |
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