AU2021103760A4 - Two-sludge sequencing batch reactor (SBR) denitrifying phosphorous removal device and stoichiometric control method - Google Patents
Two-sludge sequencing batch reactor (SBR) denitrifying phosphorous removal device and stoichiometric control method Download PDFInfo
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- 238000012163 sequencing technique Methods 0.000 title claims abstract description 81
- 239000010802 sludge Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 15
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 title description 8
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 114
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 114
- 239000011574 phosphorus Substances 0.000 claims abstract description 114
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 238000012544 monitoring process Methods 0.000 claims abstract description 27
- 230000000694 effects Effects 0.000 claims abstract description 20
- 230000001276 controlling effect Effects 0.000 claims abstract description 19
- 229910002651 NO3 Inorganic materials 0.000 claims abstract description 18
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims abstract description 17
- 230000001105 regulatory effect Effects 0.000 claims abstract description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 36
- 239000004912 1,5-cyclooctadiene Substances 0.000 claims description 21
- 229910052757 nitrogen Inorganic materials 0.000 claims description 18
- 239000011521 glass Substances 0.000 claims description 2
- 238000005457 optimization Methods 0.000 abstract description 5
- 241000894006 Bacteria Species 0.000 description 17
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 10
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 7
- 238000012360 testing method Methods 0.000 description 6
- 238000009825 accumulation Methods 0.000 description 5
- 230000001546 nitrifying effect Effects 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 238000005273 aeration Methods 0.000 description 3
- 230000001580 bacterial effect Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000002798 spectrophotometry method Methods 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229920003048 styrene butadiene rubber Polymers 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 101100283604 Caenorhabditis elegans pigk-1 gene Proteins 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- NULAJYZBOLVQPQ-UHFFFAOYSA-N N-(1-naphthyl)ethylenediamine Chemical compound C1=CC=C2C(NCCN)=CC=CC2=C1 NULAJYZBOLVQPQ-UHFFFAOYSA-N 0.000 description 1
- WYWFMUBFNXLFJK-UHFFFAOYSA-N [Mo].[Sb] Chemical compound [Mo].[Sb] WYWFMUBFNXLFJK-UHFFFAOYSA-N 0.000 description 1
- 230000021736 acetylation Effects 0.000 description 1
- 238000006640 acetylation reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000007954 hypoxia Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- 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
- C02F3/006—Regulation methods for biological treatment
-
- 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
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- 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
- C02F2209/14—NH3-N
-
- 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
-
- 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
- C02F2209/18—PO4-P
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/121—Multistep treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1263—Sequencing batch reactors [SBR]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The present invention discloses a two-sludge sequencing batch reactor (SBR) denitrifying
phosphorus removal device and a metering control method; the device includes a 1sequencing
batch reactor, a 24 sequencing batch reactor, a nitrate exchanger, and a COD/N/P monitoring and
controlling device; the 1 4 sequencing batch reactor is connected with a first feed water pump via
pipelines, and is further communicated with the nitrate exchanger via pipelines; the COD/N/P
monitoring and controlling device is used for monitoring a COD/N/P concentration of feed water,
regulating and controlling a COD/N/P concentration in the 1 4 sequencing batch reactor; the nitrate
exchanger is connected with the 1 4 sequencing batch reactor via a third feed water pump, and is
further connected with the 2 4 sequencing batch reactor via a second feed water pump; and the 24
sequencing batch reactor is further communicated with the nitrate exchanger via pipelines. The
present invention has an excellent denitrifying phosphorus removal effect through control and
optimization of the COD/N/P stoichiometric ratio of feed water.
FIG. 1
300 j * 100
90
260 8 --- COD outlet water 8
240-*+-Removal rate
-220
-~180 60
0160 55 0
0 eid2Period 4 50E 0140 45 l
120 40 0
100
80 30
80 25
60Period 6 20
15
40
10
10 20 30 40 50 60 70 80 90 100
time(d)
FIG. 2
Description
FIG. 1
300 j * 100 90 260 88 --- COD outlet water 240-*+-Removal rate -220
-~180 60 0160 55 0 0 eid2Period 4 50E 0140 45 l 120 40 0 100
80 30 80 25 60Period 6 20 15 40 10 10 20 30 40 50 60 70 80 90 100 time(d)
FIG. 2
Two-Sludge Sequencing Batch Reactor (SBR) Denitrifying Phosphorous Removal
Device and Stoichiometric Control Method
Technical Field
The present invention belongs to the field of nitrogen and phosphorus-containing wastewater treatment;
and particularly relates to a two-sludge sequencing batch reactor (SBR) denitrifying phosphorous removal
device and a metering control method.
Background
Studies on biological removal of nitrogen started from 1890 internationally. Based on the theory of
traditional biological nitrogen and phosphorus removal, it is believed that ammonia nitrogen in sludge is
discharged for removal in a form of N 2 after through two stages of "aerobic nitrification" and "anaerobic
denitrification"; and phosphorus in sludge is discharged for removal with the sludge after through two stages
of "anaerobic phosphorus release" and "aerobiotic phosphorus accumulation". Since 1978, domestic and
foreign scholars have started to study denitrifying phosphorus removal; and the basic principle is that
denitrifying phosphorus removing bacteria (abbreviated for DPB) are subjected to "anaerobic phosphorus
release", and NO 2 - or NO 3 - substitutes 02 under anoxic conditions as an electron acceptor, thus achieving
simultaneous nitrogen and phosphorous removal; denitrifying phosphorus removal can respectively save 50%
COD and 30% 02 consumption, and accordingly reduce 50% remaining sludge quantity. However, there are
contradictions and controversies in domestic and foreign researches in the aspects that nitrate nitrogen and
nitrite nitrogen substitute oxygen as an electron acceptor for biological phosphorus removal, which one is
more effective, nitrate nitrogen or nitrite nitrogen; which kind of impact does aerobic zone have on the
stability of denitrifying phosphorus removing bacteria; whether the species of denitrifying phosphorus
removing bacteria follows the bacterial genus I theory or bacterial genus II theory. Moreover, most of the
studies are laboratory researches, incapable of achieving engineering application and industrialization. We
have found in the preliminary study that there are four new denitrifying phosphorus removing bacteria DPB in
municipal sewage sludge treatment, and denitrifying phosphorus removing bacteria are proved to have
metabolic characteristics extremely similar to aerobic phosphorus removing bacteria. That is, anoxic
phosphorus accumulation may substitute aerobic phosphorus accumulation. Therefore, directed to the difficulty of low emission reduction efficiency in the sewage nitrogen and phosphorus project, it is in urgent need of efficient, economical and practical key technologies and equipment capable of achieving simultaneous nitrogen and phosphorus removal with project scale and industrial application.
Seneesrisaku, et al., have studied to find that when R1:R2:R3 has a volume ratio of 1:1.5:5, COD
removal rate is up to the maximum (90%), and the extraction efficiency of total energy is up to 66%. The
volume ratio can correspond to the production time ratio of microorganisms in hydrolysis/acid production,
acetylation and methane production steps very well, and can be applied for the enlargement of 3S-ASBR and
3-step/stage up-flow anaerobic sludge blanket (3S-UASB) system (Effects of the reactor volumetric ratio and
recycle ratio on the methane and energy productivity of a three-step anaerobic sequencing batch reactor
(3S-ASBR) treating ethanol wastewater).
Summary
Directed to the shortcomings in the prior art, the objective of the present invention is to provide a
two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device and a stoichiometric
control method. Two SBRs create optimal growing environment respectively using an activated sludge
process and a biofilm process for nitrifying bacteria and denitrifying phosphorus removing bacteria; nitrifying
bacteria and denitrifying phosphorus removing bacteria are respectively cultured in different sludge systems to
respectively achieve ammonia nitrogen nitrification and denitrifying phosphorus removal, thus achieving the
purpose of improving the simultaneous nitrogen and phosphorus removal effect. The present invention has a
COD removal rate of 90% or above, ammonia nitrogen and total phosphorus removal rate of 90% or above;
under optimization conditions, the removal rate of COD, ammonia nitrogen and total phosphorus is up to
100%.
To achieve the above objective of the present invention, the present invention adopts the following
technical solution:
A two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device includes a 1
sequencing batch reactor SBR1, a 2#sequencing batch reactor SBR2, a nitrate exchanger, and a COD/N/P
monitoring and controlling device; the 1#phosphorous removal device SBR1 is connected with a first feed
water pump via pipelines, and is further communicated with the nitrate exchanger via pipelines; the COD/N/P
monitoring and controlling device is used for monitoring a COD/N/P concentration of feed water, regulating and controlling a COD/N/P concentration in the 1#sequencing batch reactor SBR1; the nitrate exchanger is connected with the 1#sequencing batch reactor SBR1 via a third feed water pump, and is further connected with the 2#sequencing batch reactor SBR2 via a second feed water pump; and the 2#sequencing batch reactor
SBR2 is further communicated with the nitrate exchanger via pipelines.
Preferably, the 1# sequencing batch reactor SBR1 and the 2# sequencing batch reactor SBR2 are
respectively provided with a second air blower and a first air blower.
Preferably, the 1 sequencing batch reactor is further provided with a stirrer.
Preferably, the 1#sequencing batch reactor SBR1 and the 2#sequencing batch reactor SBR2 are prepared
by organic glass.
Preferably, the COD/N/P monitoring and controlling device is respectively connected with the first feed
water pump, the 1#sequencing batch reactor SBR1, and a COD/N/P concentration monitoring sensor; and the
COD/N/P concentration monitoring sensor is used for monitoring a COD/N/P concentration of feed water.
Further preferably, the COD/N/P concentration monitoring sensor is arranged in the1#sequencing batch
reactor SBR1 (2).
Preferably, the COD/N/P monitoring and controlling device regulates and controls a COD/N/P
concentration in the 1 sequencing batch reactor SBR1 by additionally adding COD, nitrogen and
phosphorus.
Preferably, the 1#sequencing batch reactor SBR1 and the 2#sequencing batch reactor SBR1 are of a
bilayer cylindrical structure which is provided with a cavity for holding hot water in a middle portion thereof;
a thermostat water bath is respectively communicated with the middle cavity of the bilayer cylinder of the 1
sequencing batch reactor and 2#sequencing batch reactor via pipelines.
A metering control method of the above two-sludge sequencing batch reactor (SBR) denitrifying
phosphorous removal device is used to regulate and control a COD/N/P stoichiometric ratio by additionally
adding COD, nitrogen and phosphorus depending on the sludge having different COD/N/P stoichiometric
ratios of feed water, thus obtaining an efficient denitrifying phosphorus removal effect.
Preferably, the regulated and controlled COD/N/P stoichiometric ratio is as follows: a N/P ratio is 6.0 or above, and a COD/N ratio is 3.0-5.0.
In this present invention, 2 sets of SBR reactors are designed to build a two-sludge film process SBR
system (FIG. 1), where SBR1 is a denitrifying phosphorus removing reactor, SBR2 is a nitrator; 2 SBRs are
used to exchange supernatant, but not exchange activated sludge; and short-time aeration is performed for
nitrogen and phosphorus removal, thus preventing the "secondary release" of phosphorus.
Compared with the prior art, the present invention has the following beneficial effects:
(1) the present invention uses two sets of sequencing batch reactors SBR1 and SBR2, and a nitrate
exchanger, where 2 SBR reactors are only used to exchange supernatant within the reaction period, but not
exchange own activated sludge, which constitutes a two-sludge system. Therefore, the present invention has a
simple structure and convenient operation and maintenance;
(2) the 2# sequencing batch reactor SBR2 is an independent aerobic denitrification tank; a fibrous
membranes is added as a packing, thus facilitating the growth and reproduction of nitrifying bacteria, such that
the reactor is not limited to sludge age, thus creating a stable condition for the growth of nitrifying bacteria;
(3) COD is almost removed completely in the anaerobic stage of the 1# sequencing batch reactor; COD
is removed and separated from a nitration portion to decrease the influence of a C/N ratio on bio-nitrification.
Under normal operation, feed water of the 2#sequencing batch reactor has a very low content of organic
matters, thus inhibiting the growth of heterotrophic bacteria and ensuring the dominant position of bacterial
community of nitrifying bacteria;
(4) the two-sludge reaction equipment in the present invention has a very good effect on COD, ammonia
nitrogen and phosphorus; outlet water has 20 mg/l COD below and 0.5 mg/l phosphorus below, and 3 mg/l
ammonia nitrogen below;
(5) the stoichiometric ratio is controlled and optimized by monitoring the COD/N/P concentration ratio in
feed water; when the N/P ratio is greater than 6.0, it should be ensured that the phosphorus uptake efficiency
under anoxic conditions increases substantially, such that the total phosphorus concentration at the end of
anoxic conditions decreases substantially, and the phosphorus removal efficient approximates to 100%.
Brief Description of the Drawings
FIG. 1 is a structure diagram showing a two-sludge SBR denitrifying phosphorus removal reaction
equipment in the present invention;
FIG. 2 is a sketch map showing the CODGr removal efficiency of the two-sludge SBR denitrifying phosphorus removal reaction equipment in the present invention;
FIG. 3 is a structure diagram showing the ammonia nitrogen removal efficiency of the two-sludge SBR
denitrifying phosphorus removal reaction equipment in the present invention;
FIG. 4 is a structure diagram showing the TP removal efficiency of the two-sludge SBR denitrifying
phosphorus removal reaction equipment in the present invention;
FIG. 5 is a sketch map showing the ammonia nitrogen removal efficiency of the two-sludge SBR
denitrifying phosphorus removal reaction equipment in the present invention;
Symbols in the drawings are described below:
1-first feed water pump, 2-1#sequencing batch reactor SBR1, 3-stirrer, 4-second feed water pump, 5-2#
sequencing batch reactor SBR2, 6-first air blower, 7-third feed water pump, 8-second air blower, 9-nitrate
exchanger, 10-COD/N/P monitoring and controlling device, and 11-COD/N/P concentration monitoring
sensor.
Detailed Description of the Embodiments
The present invention will be further described in combination with the drawings and examples of the
description. But the scope set forth in the present invention is not limited to the scope described in the specific
examples.
Example 1
A two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device and a metering
control method
As shown in FIG. 1, the two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal
device includes a 1"sequencing batch reactor 2, a 2"sequencing batch reactor 5, a nitrate exchanger 9, and a
COD/N/P monitoring and controlling device 10; the 1"phosphorus removal device 2 is connected with a first
feed water pump via pipelines, and is further communicated with the nitrate exchanger 9 via pipelines; the
nitrate exchanger 9 is connected with the 1"sequencing batch reactor 2 via a third feed water pump 7, and is
further connected with the 2"sequencing batch reactor 5 via a second feed water pump 4; and the 2"
sequencing batch reactor 5 is further communicated with the nitrate exchanger 9 via pipelines. The 1"
sequencing batch reactor 2 is connected with the second air blower 8 via a vent pipe, and the second air
blower 8 performs blast aeration to the 1"sequencing batch reactor 2. A stirrer 3 is mounted at the top of the 1
sequencing batch reactor 2; and a mixed liquor in the 1"sequencing batch reactor 2 is stirred in the anaerobic and anoxic stages. The 2"sequencing batch reactor 5 is connected with a second air blower 6 via a vent pipe, and the second air blower 6 performs blast aeration to the 2"sequencing batch reactor 5. Two sets of thermostat water bathes are arranged nearby the reaction unit to respectively transport thermostating water to the middle part of a bilayer cylinder of the 1"sequencing batch reactor 2 and the 2"sequencing batch reactor 5.
To achieve the purpose of controlling and optimizing feed water metering, a feed water N/P monitoring and
controlling device (10) is arranged at a front end of the two-sludge film system to be respectively connected
with the first feed water pump, 1 sequencing batch reactor SBR1, and the nitrogen and phosphorus
concentration monitoring sensor (11). An organic matter COD is additionally added to blend nitrogen and
phosphorus properly, thus controlling the COD/N/P ratio of feed water, and achieving adjustment and
optimization.
Implementation effect:
The first stage in the implementation of the present invention was a test run stage: at a sludge age of 13 d,
after through test run for 32 d and the system treatment effect was stable, the influence of ultra-short sludge
age on the system treatment effect was surveyed at the second stage, namely, the stage that sludge age reduced
to 7 d; the third stage was a system recovery stage; after running for a 3 d short sludge age, the sludge had
more loss, and the system recovered to 13 d sludge age for running for 20 d; the fourth stage was that after the
system treatment effect was stable, the sludge age increased to 22 d to survey the running condition of the
system; the fifth stage was to reduce a COD concentration to 140 mg/L, thus surveying the influence of a low
C/N ratio on the denitrifying phosphorus removal effect. Meanwhile, test wastewater having different
COD/N/P stoichiometric ratios was prepared for a state test with different stoichiometric ratios to survey the
influence of different stoichiometric ratios on the phosphorus accumulation under anoxic conditions.
The test inoculated sludge was taken from a certain sewage treatment plant. Feed water was manually
prepared simulation wastewater; and according to the demands for different test conditions, feed water quality
having different COD/N/P stoichiometric ratios was prepared. Major components included: 250 mg COD/L
NaAc or glucose, 0.028 g/L K 2 HPO4 , 0.022 g/L KH 2 PO4 , 0.115 g/L NH 4 Cl, 0.035 g/L CaC 22H 2 0, 0.15 g/L
MgSO4 7H 2 O, and 0.3 ml/L microelement solution. A COD concentration scope of feed water was controlled
within 100.0-500.0 mg/L; the ammonia nitrogen concentration scope was 20.0-150.0 mg/L; the total
phosphorus was 2.0-13.0 mg/L; thus optimizing and controlling the ratio.
Analysis method: COD: XJ-1 COD digestion instrument was used for digestion; potassium dichromate
method; TP: molybdenum-antimony spectrophotometry; NH4 -N: Pay reagent luminosity law; NO 2
-N:N-(1-naphthyl)-ethylenediamine spectrophotometry; NO 3 _-N: ultraviolet spectrophotometry.
1. COD removal efficiency
As can be seen from FIG. 2, the two-sludge SBR denitrifying phosphorus removal reaction equipment
had a very good treatment effect. For simulated domestic wastewater, the system had a stable COD removal
efficiency; COD of feed water was basically 20 mg/L below, being up to national discharge standards. The
outlet concentration had a smaller fluctuation range, and the removal rate was 90% or above. But when the
sludge age was controlled to 7 d, COD removal rate was only 70% around, this was because the amount of the
discharged sludge was up to 2.0 L or above per day, there was no enough micro-biological degradation COD.
Different from the removal way of traditional nitrogen and phosphorus removal process, most of the organic
matters in the two-sludge system were consumed by denitrifying phosphorus removing bacteria in an
anaerobic pool to be used for synthesizing the storage particles PHB in cells and phosphorus release.
2. Ammonia nitrogen removal
As shown in FIG. 3, ammonia nitrogen in feed water was 302 mg/L around, ammonia nitrogen in outlet
water maintained a lower level, and lower than 3 mg/L basically; and the ammonia nitrogen removal rate was
92% or above. Ammonia nitrogen in outlet water maintained a lower level.
3. P removal
As can be seen from FIG. 4, the phosphorus removal efficiency was up to 95% on the 8th day after
running, the phosphorus content in outlet water was lower than 0.5 mg/L; and in the remaining time of the
first stage, the phosphorus content in outlet water basically maintained 0.5 mg/L below, and the phosphorus
removal effect was good. At the second stage, the sludge age reduced to 7 d, and it could be found that the
phosphorus removal efficiency was up to 98.6%. At the third stage, the sludge age recovered to 13 d around,
when the system had a stable phosphorus removal effect after running for nearly a month, SRT increased to 22
d, and it could be found that the phosphorus removal efficiency rapidly reduced to 50% around, and the outlet
feed contained a high content of phosphorus. This was because the amount of the discharged sludge was too
little, the sludge containing phosphorus stayed in a reactor, which cannot achieve the purpose of phosphorus
removal. Thus, it can be seen that SRT has a significant impact on ensuring the efficient and stable operation
of the system.
It further can be seen from FIG. 4 that the phosphorus removal efficiency at the 5th stage with a lower
COD concentration is obviously lower thn the first and the third stages. This was because when the COD
concentration at the 5th stage reduced to 140 mg/L, the system had less VFA content and also less anaerobic phosphorus release amount, such that there were a large amount of NO3-N residuals at the end of the anoxic zone; and the residual NO3-N would also seriously influence the anaerobic phosphorus release effect in the next period. Therefore, too low COD is against phosphorus removal. Therefore, when the two-sludge SBR denitrifying phosphorus removing device is running in a low temperature condition, it needs to properly extend the phosphorus uptake time under anoxic conditions.
4. Nitrate nitrogen removal
It can be seen from FIG. 5 that the nitrate nitrogen content in outlet water during running in thefirst stage
is basically 3.57 mg/L below. The nitrate nitrogen content in outlet water at the second stage significantly
increased, this was because the more amount of discharged sludge resulted in the decrease of the total amount
of denitrifying phosphorus removing bacteria, and the denitrifying process was influenced. The amount of
discharged sludge reduced in the fourth stage, and the sludge age extended to 22 d, the nitrate nitrogen
concentration in outlet water had a little change, indicating that the denitrifying effect in SBR1 was not
influenced by the long sludge age. As shown in the figure, when the COD concentration reduced to 150 mg/L,
the nitrate nitrogen content in outlet water had a greater increase, this was because the C/N ratio in feed water
was low, such that the amount of PHB synthesized in the anaerobic zone was lower, and the anaerobic
phosphorus release amount was low, incapable of denitrifying the denitrifying solution provided by a biofilm
denitrification tank thoroughly; that is, the electron donor PHB was shortage relative to the electron acceptor
NO3-N, resulting in that there was residual NO3-N after hypoxia reaction, and the amount of NO3-N in
outlet water was slightly higher. Thus, it can be seen that whether COD provided in the anaerobic zone is
directly related to the denitrification and phosphorus removal effect in the anoxic zone, thus finally
determining the nitrogen and phosphorus content in outlet water.
5. Analysis on the anaerobic phosphorus release and anoxic phosphorus uptake effect of a two-sludge
SBR device
The control schemes of COD/N/P stoichiometric ratios were constructed under 9 feed water working
conditions of the two-sludge system to survey the phosphorus release condition of DPB bacteria in the
anaerobic zone and phosphorus accumulation condition thereof at the anoxic zone. Results show that whether
COD provided in the anaerobic zone is directly related to the denitrification and phosphorus removal effect in
the anoxic zone, thus finally determining the nitrogen and phosphorus content in outlet water.
The anaerobic phosphorus release amount and anoxic phosphorus uptake effect are related with each
other closely under different conditions of COD/N/P stoichiometric ratios (tables 1, 2, and 3)
Table 1 Influence of a COD/N/P ratio in feed water on anaerobic phosphorus release
Phosphate in COD in feed P removal COD COD/N/P outlet water water rate % removal rate
% mg/L mg/L
150:20:3 0 100 0 100
150:20:5 0.88 82.47 0 100
150:20:8 1.53 80.80 0 100
150:30:3 0 100 0 100
150:30:5 0.16 96.79 0 100
150:30:8 0.18 97.76 0 100
150:50:3 0 100 0 100
150:50:5 0 100 0 100
150:50:8 0 100 0 100
Table 2 Influence of a COD/N/P ratio in feed water on anoxic phosphorus uptake
Phosphorus Concentratio Anoxic zone Phosphorus uptake rate n of phosphorus COD/N/P Uptake of removal Linear zone at the end of phosphorus mg/L efficiency %
Average zone anoxic condition
150:20:3 7.73 2.27 0.81 0.22 92.79
150:20:5 9.41 3.59 1.05 3.24 35.46
150:20:8 9.09 3.35 1.01 4.67 41.41
150:30:3 7.38 2.56 1.23 0 100
150:30:5 12.78 3.21 1.42 0.48 90.36
150:30:8 13.72 3.55 1.52 0.45 94.40
150:50:3 5.38 2.69 1.79 0 100
150:50:5 12.32 4.63 2.05 0 100
150:50:8 14.02 4.45 1.87 0 100
Table 3 Influence of a COD/N/P ratio in feed water on the optimization of phosphorus uptake and
phosphorous removal under anoxic condition
Phosphorus Concentratio Anoxic zone Phosphorus uptake rate n of phosphorus COD/N/P Uptake of removal Linear zone at the end of phosphorus mg/L efficiency %
Average zone anoxic condition
150:30:3 7.38 2.56 1.23 0 100
150:50:3 5.38 2.69 1.79 0 100
150:50:5 12.32 4.63 2.05 0 100
150:50:8 14.02 4.45 1.87 0 100
250:50:5 16.43 7.26 2.19 0 100
250:50:8 21.35 8.33 2.37 0 100
250:62.5:5 16.23 2.69 1.79 0 100
250:62.5:8 20.08 4.63 2.05 0 100
350:77.8:10 33.98 4.45 1.87 0 100
350:100:8 28.52 - 3.80 0 100
350:100:10 31.79 - 4.24 0 100
At a certain COD concentration (e.g., 150 mg/L) in feed water, the scope of the COD/N ratio was
controlled within 3.0-7.5; the N/P ratio was adjusted, and ammonia nitrogen concentration was controlled to
20.0, 30.0, and 50.0 mg/L, such that the feed water was combined with total phosphorus concentrations of 3.0,
5.0, and 8.0 mg/L respectively, which may substantially increase the consumption of microorganisms to COD,
such that the COD removal rate was up to 100% (table 1). Meanwhile, at a certain COD concentration (e.g.,
150 mg/L) in feed water, the scope of the COD/N ratio was controlled within 3.0-7.5; the N/P ratio was
adjusted, and ammonia nitrogen concentration was controlled to 20.0, 30.0, and 50.0 mg/L, such that the feed
water was combined with total phosphorus concentrations of 3.0, 5.0, and 8.0 mg/L respectively; when the
N/P ratio was 35.46% and 41.4%, when N/P increased to 6.0 or above, the total phosphorous removal rate
increased substantively, being up to 100% (table 2). Further, at different COD concentrations in feed water, the
N/P ratio increased to 6.0 or above, COD/N/P metering optimization was performed; the COD/N ratio was
controlled within a range of 3.0-5.0, capable of reducing the total phosphorus concentration in outlet water;
for example, when COD/N/P was 150:50:3, 150:50:5, 150:50:8 and under other 12 chemometrics conditions, the concentration of phosphorus at the end of anoxic condition was 0 mg/L, and the phosphorus removal rate under anoxic conditions was up to 100% (table 3).
The above examples are preferred embodiments of the present invention. But the embodiments of the
present invention are not limited to the above examples. Moreover, any other alteration, modification,
replacement, combination and simplification made within the spirit and principle of the present invention shall
be equivalent substitution modes, and are included in the protection scope of the present invention.
Claims (10)
1. A two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device, characterized
by comprising a 1"sequencing batch reactor SBR1, a 2"sequencing batch reactor SBR2, a nitrate exchanger,
and a COD/N/P monitoring and controlling device; wherein the 1"phosphorus removal device SBR1 is
connected with a first feed water pump via pipelines, and is further communicated with the nitrate exchanger
via pipelines; the COD/N/P monitoring and controlling device is used for monitoring a COD/N/P
concentration of feed water, regulating and controlling a COD/N/P concentration in the 1"sequencing batch
reactor SBR1; the nitrate exchanger is connected with the 1"sequencing batch reactor SBR1 via a third feed
water pump, and is further connected with the 2"sequencing batch reactor SBR2 via a second feed water
pump; and the 2"sequencing batch reactor SBR2 is further communicated with the nitrate exchanger via
pipelines.
2. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 1, characterized in that the 1 sequencing batch reactor SBR1 and the 2" sequencing batch reactor
SBR2 are respectively provided with a second air blower and a first air blower.
3. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 1, characterized in that the 1 sequencing batch reactor is further provided with a stirrer.
4. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 1, characterized in that the 1"sequencing batch reactor SBR1 and the 2"sequencing batch reactor SBR2
are prepared by organic glass.
5. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 1, characterized in that the COD/N/P monitoring and controlling device is respectively connected with
the first feed water pump, the1"sequencing batch reactor SBR1, and a COD/N/P concentration monitoring
sensor; and the COD/N/P concentration monitoring sensor is used for monitoring a COD/N/P concentration of
feed water.
6. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 5, characterized in that the COD/N/P concentration monitoring sensor is arranged in the1"sequencing
batch reactor SBR1.
7. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 1, characterized in that the COD/N/P monitoring and controlling device regulates and controls a
COD/N/P concentration in the 1 sequencing batch reactor SBR1 by additionally adding COD, nitrogen and
phosphorus.
8. The two-sludge sequencing batch reactor (SBR) denitrifying phosphorus removal device according to
claim 1, characterized in that the 1"sequencing batch reactor SBR1 and the 2"sequencing batch reactor SBR1
are of a bilayer cylindrical structure which is provided with a cavity for holding hot water in a middle portion
thereof; a thermostat water bath is respectively communicated with the middle cavity of the bilayer cylinder of
the 1"sequencing batch reactor and 2"sequencing batch reactor via pipelines.
9. A metering control method of the two-sludge sequencing batch reactor (SBR) denitrifying phosphorus
removal device according to any one of claims 1-8, characterized in that a COD/N/P stoichiometric ratio is
regulated and controlled by additionally adding COD, nitrogen and phosphorus depending on the sludge
having different COD/N/P stoichiometric ratios of feed water, thus obtaining an efficient denitrifying
phosphorus removal effect.
10. The metering control method according to claim 9, characterized in that the regulated and controlled
COD/N/P stoichiometric ratio is as follows: a N/P ratio is 6.0 or above, and a COD/N ratio is 3.0-5.0.
2021103760 1/3
FIG. 1
COD feed water COD outlet water Removal rate
Period 2 COD Removal rate (%） Period 4
Period 1 Period 3 Period 5
Period 6
FIG. 2
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| CN202110707996.X | 2021-06-24 | ||
| CN202110707996.XA CN113461160A (en) | 2021-06-24 | 2021-06-24 | SBR denitrifying phosphorus removal device of double-mud sequencing batch reactor and metering control method |
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