CN113415899B - Device and method for deep denitrification based on adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation of slow degradation organic matters - Google Patents

Device and method for deep denitrification based on adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation of slow degradation organic matters Download PDF

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CN113415899B
CN113415899B CN202110708531.6A CN202110708531A CN113415899B CN 113415899 B CN113415899 B CN 113415899B CN 202110708531 A CN202110708531 A CN 202110708531A CN 113415899 B CN113415899 B CN 113415899B
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CN113415899A (en
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彭永臻
解宸
石亮亮
吴蕾
秦璐阳
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Beijing University of Technology
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Abstract

An apparatus and a method for deep denitrification based on slow degradation organic matter adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation belong to the field of sewage biological treatment, and the apparatus comprises a raw water tank and NO-containing devices 3 ‑ -N wastewater tank, bio-adsorption/hydrolytic acidification/short range denitrification SBR reactor, intermediate tank I, intermediate tank II, anaerobic ammoxidation UASB reactor. Firstly, pumping domestic sewage raw water into an SBR reactor, adsorbing soluble slow degradation organic matters in the domestic sewage raw water to the surface of sludge through short aeration, sedimentation and drainage, and sedimentating the soluble slow degradation organic matters together with the granular slow degradation organic matters, and converting the soluble slow degradation organic matters into soluble easily degradable organic matters through anaerobic hydrolysis acidification; then NO is added 3 ‑ Pumping the N wastewater into an SBR reactor for short-range denitrification; NO accumulated for the second time 2 ‑ And mixing the N effluent with the treated domestic sewage raw water discharged for the first time, and feeding the mixture into a UASB reactor connected in series for anaerobic ammoxidation reaction, thereby realizing deep denitrification.

Description

Device and method for deep denitrification based on adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation of slow degradation organic matters
Technical Field
The invention relates to a device and a method for deep denitrification based on adsorption, hydrolysis, short-range denitrification and serial anaerobic ammoxidation of slowly degraded organic matters, belongs to the technical field of sewage biological treatment, and is a technical method for effectively utilizing the solubility and the granularity of slowly degraded organic matters, solving the technical problem of insufficient carbon sources in the biological treatment of low-carbon-nitrogen-ratio domestic sewage and synchronously realizing the deep denitrification.
Background
Along with advocating the sustainable development concept in the modern society, aiming at the increasingly prominent water environment pollution problem, the existing town sewage treatment plant reaches the corresponding emission standard, and the newly built town sewage treatment facility needs to execute the first-level A standard of pollutant emission standard of town sewage treatment plant (GB 18918-2002). However, the problem of low C/N of the inlet water in the current urban sewage treatment plant generally exists, if the traditional nitrification-denitrification biological denitrification treatment technology is still utilized, a large amount of aeration energy consumption and a large amount of additional carbon source are required to be consumed in order to achieve the strict emission standard, so that the novel biological denitrification technology needs to be developed and applied.
Wherein, the anaerobic ammonia oxidation technology can be used for converting NO by anaerobic ammonia oxidation bacteria 2 - N as electron acceptor with NH 4 + N as electron donor, N is produced without the need of dissolved oxygen 2 . Therefore, this technique is widely favored because of its high efficiency of denitrification and good energy saving effect. However, in practical engineering application, the important substrate NO of the anaerobic ammonia oxidation process 2 - The source of N remains a major challenge.
At present, two technical approaches of short-cut nitrification and short-cut denitrification mainly provide substrates for anaerobic ammoxidation. In short-cut nitrification systems, ammonia Oxidizing Bacteria (AOB) oxidize NH 4 + Oxidation of N to NO 2 - N, but due to the presence of Nitrite Oxidizing Bacteria (NOB), NH is readily available 4 + -N is further oxidized to NO 2 - And N, so the shortcut nitrification has the characteristics of easy damage and difficult recovery. In short-cut denitrification system, NO 3 - -N is reduced to NO 2 - N, this process can be achieved by various means of controlling the reaction carbon nitrogen ratio, controlling the reaction time, etc., and is more hopefully applied to engineering practice.
Based on the current research, NO in short-cut denitrification system 2 - The accumulation of N is closely related to the type of carbon source, and the rapid degradation of organic matters (RBOM), such as sodium acetate, glucose, methanol, ethanol and other soluble small molecular organic matters are more beneficial to NO 2 - -N generation. However, compared with RBOM, in the actual domestic sewage, the organic matters (SBOM) are slowly degraded, the proportion of the organic matters is larger, and the organic matters account for 30% -85% of the total organic carbon source, and are mainly divided into dissolubility and particle slow degradation organic matters. Thus in order to stabilize NO stabilized in short-cut denitrification systems 2 - N production ofThe ratio, in actual operation, a large amount of easily degradable carbon source is still needed to be added, SBOM cannot be effectively utilized by microorganisms, and the SBOM is not effectively consumed in the subsequent aeration process. The process consumes additional resources, wastes carbon sources contained in raw water, and simultaneously discharges more CO 2 Not only increases the sewage treatment cost, but also is unfavorable for energy conservation and emission reduction of greenhouse gases.
Therefore, in order to further reduce the energy consumption of the system and respond to the targets of carbon peak and carbon neutralization, a technology for realizing the effective utilization of SBOM and ensuring the deep denitrification of sewage based on the short-range denitrification and anaerobic ammonia oxidation technology is needed to be proposed.
Disclosure of Invention
The invention provides a device and a method for deep denitrification by coupling adsorption hydrolysis with short-range denitrification and serial anaerobic ammoxidation based on slow degradation organic matters, and aims to provide an effective scheme for realizing effective utilization of SBOM in domestic sewage raw water based on biological adsorption and hydrolytic acidification technology under the condition of ensuring efficient deep denitrification of sewage by utilizing short-range denitrification and anaerobic ammoxidation technology, thereby providing a reference thinking for practical application of the short-range denitrification-anaerobic ammoxidation technology.
The technical principle of the invention is as follows: the method comprises the steps of enabling the soluble and granular slow-degradation organic matters in the domestic sewage raw water to be adsorbed to the surface of sludge through short aeration, sedimentation and drainage stages, settling together with the granular slow-degradation organic matters, and then decomposing the soluble and granular slow-degradation organic matters into soluble and easily-degradable organic matters through an anaerobic hydrolysis acidification coupling short-range denitrification technology, and using the soluble and granular slow-degradation organic matters for NO 2 - -N generation; and the anaerobic ammoxidation is connected in series to realize further deep denitrification.
The invention aims at solving the problems by the following technical scheme: the following device is utilized, comprising: raw water tank (1) and NO-containing 3 - -N wastewater tank (2), bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3), intermediate tank I (4), intermediate tank II (5), anaerobic ammonia oxidation UASB reactor (6) and on-line feedback and control system (7);
wherein the raw materialThe object adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is provided with: raw water inlet pump (3.1), raw water inlet (3.2) and NO 3 - -N wastewater inlet pump (3.3), NO 3 - -N wastewater inlet (3.4), aeration pump (3.5), gas flow meter (3.6), aeration disc (3.7), stirrer (3.8), SBR pH/DO meter (3.9), water outlet (3.10), drain valve I (3.11), drain valve II (3.12), sludge outlet (3.13), sludge outlet valve (3.14), wherein water outlet (3.10) is connected with drain valve I (3.11), drain valve II (3.12) through connecting pipe and tee joint; wherein the anaerobic ammonia oxidation UASB reactor (6) is configured with: UASB water inlet pump I (6.1), UASB water inlet pump II (6.2), UASB water inlet (6.3), UASB pH/DO determinator (6.4), UASB water outlet (6.5), UASB reflux inlet (6.6) and reflux pump (6.7); the online feedback and control system (7) comprises a programmable controller (7.1) and a computer (7.2); wherein the programmable controller (7.1) is internally provided with an aeration pump relay (7.3) and NO 3 - -N wastewater intake pump relay (7.4), raw water intake pump relay (7.5), stirrer relay (7.6), reflux pump relay (7.7), UASB intake pump I relay (7.8), UASB intake pump II relay (7.9), drain valve I relay (7.10), drain valve II relay (7.11), mud valve relay (7.12), a/D signal converter conversion interface (7.13), D/a signal converter conversion interface (7.14);
domestic sewage raw water in the raw water tank (1) is pumped into the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet pump (3.1) through a raw water inlet (3.2), and then pumped into an intermediate water tank I (4) from a water outlet (3.10) through a drain valve I (3.11); the NO-containing 3 - -NO in the N wastewater tank (2) 3 - -N pollutant wastewater pass through NO 3 - -N wastewater inlet pump (3.3) through NO 3 - -N wastewater inlet (3.4) is pumped into the bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) and then from water outlet (3.10) into intermediate water tank II (5) through drain valve II (3.12); wherein a UASB water inlet (6.3) configured by the anaerobic ammonia oxidation UASB reactor (6) is respectively connected with an intermediate water tank I (4) and an intermediate water tank II (5) through a UASB water inlet pump I (6.1) and a UASB water inlet pump II (6.2); the UASB reflux port (6.6) is passed through a reflux pump (6). 7) Is connected with a UASB water inlet (6.3) for backflow;
in the on-line feedback and control system (7), an aeration pump relay (7.3) is connected with an aeration pump (3.5); NO (NO) 3 - -N wastewater inlet pump relay (7.4) and NO 3 - -N wastewater inlet pump (3.3) connected; the raw water inlet pump relay (7.5) is connected with the raw water inlet pump (3.1); the stirrer relay (7.6) is connected with the stirrer (3.8); the reflux pump relay (7.7) is connected with the reflux pump (6.7); the UASB water inlet pump I relay (7.8) is connected with the UASB water inlet pump I (6.1); a UASB water inlet pump II relay (7.9) and a UASB water inlet pump II (6.2); the drain valve I relay (7.10) is connected with the drain valve I (3.11); the drain valve II relay (7.11) is connected with the drain valve II (3.12); the mud valve relay (7.12) is connected with the mud valve (3.14); the programmable controller (7.1) is connected to the computer (7.2) through the A/D signal converter conversion interface (7.13) and converts the sensor signal into a digital signal to be transmitted to the computer (7.2); the computer (7.2) is connected with the programmable controller (7.1) through the D/A signal converter conversion interface (7.14) and transmits the digital signal to the programmable controller (7.1).
The method for realizing in-situ coupling biological adsorption/hydrolytic acidification/short-range denitrification tandem anaerobic ammonia oxidation and deep denitrification by utilizing solubility and particle slow degradation organic matters by using the device as claimed in claim 1, which is characterized by comprising the following steps:
1) And (3) starting a system:
1.1 Start-up of the biosorption/hydrolytic acidification/short-cut denitrification SBR reactor: adding excess sludge of a sewage plant into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) so that the concentration of the volatile sludge in the reactor is MLVSS=2500-5000 mg/L; controlling the residence time of the sludge to be 25-50 days; the reactor runs for 2 cycles each day, and each cycle starts from a raw water inlet stage and sequentially goes through an aeration adsorption stage, a first precipitation stage, a first drainage stage, an anaerobic stirring stage and an NO-containing stage 3 - -N wastewater inlet stage, anoxic stirring stage, sludge discharge stage, second precipitation stage, and ending the second water discharge stage for 10 stages; the related operation is controlled by an on-line feedback and control system (7); within each periodPumping the simulated domestic sewage raw water into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet pump (3.1), starting an agitator (3.8) and an aeration pump (3.5) to start aeration adsorption, controlling the aeration quantity of a system through a gas flowmeter (3.6), keeping the dissolved oxygen concentration displayed by an SBR pH/DO tester (3.9) at 1.0-1.5 mg/L, and precipitating for 20-30 min after the process lasts for 20-30 min, and discharging water; after the drainage is completed, the sludge is precipitated and concentrated, a stirrer (3.8) is started for anaerobic stirring, and when the increase rate of the concentration of SCOD is detected to be lower than 0.1mg (L.h) -1 And when the time lasts for more than 5min, the stirrer (3.8) is turned off, and the anaerobic stirring is stopped; then turn on NO 3 - -N wastewater inlet pump (3.3) through NO 3 - The N wastewater inlet (3.4) is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) to be subjected to anoxic stirring, and when NO 3 - -when the N concentration is lower than 5mg/L, the stirrer (3.8) is turned off, stopping the anoxic stirring; when the concentration increment of the initial end SCOD of the anaerobic section reaches more than 50% of the inflow TCOD, the end NO of the anoxic section 3 - And when the N concentration is less than 5mg/L and the stable operation is carried out for more than 10 cycles, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is considered to be successfully started.
1.2 Start-up of anaerobic ammoxidation UASB reactor: adding sludge with ammonia oxidation activity into an anaerobic ammonia oxidation UASB reactor (6) to ensure that the sludge concentration in the reactor is MLSS=2500 mg/L-3000 mg/L; when NH in effluent 4 + -N concentration, NO 2 - And when the N concentration is less than 1mg/L and the stable operation is performed for more than 40 hours, the anaerobic ammonia oxidation UASB reactor (6) is considered to be successfully started.
2) Setting the parameters of a reactor:
according to the set drainage ratio R, SBR of the SBR reactor, the effective volume V of the reactor 0 Raw water intake volume V of domestic sewage 1 Containing NO 3 - N wastewater inlet volume V 2 Containing NO 3 - NO in N wastewater 3 - -N concentration C N Concentration C of total organic matter (TCOD) in domestic sewage raw water C The sewage flow rate through the UASB water inlet pump I (6.1) is q 1 Enter through UASBThe sewage flow of the water pump II (6.2) is q 2 UASB hydraulic retention time is HRT UASB The respective parameter relationships satisfy the following formulas (1), (2), (3), (4):
V 0 ×R＝V 1 ＝V 2 formula (1)
(C C ×V 1 )/(C N ×V 2 ) =3.5 to 6.0 formula (2)
q 1 ×HRT UASB ＝V 1 Formula (3)
q 2 ×HRT UASB ＝V 2 Formula (4)
The drainage ratio initial value is set to r=20%;
UASB hydraulic retention time is set to be HRT UASB ＝1.0～4.0h；
3) Runtime adjustment operation:
3.1 Operation of the biosorption/hydrolytic acidification/short-cut denitrification SBR reactor): the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) sequentially goes through an aeration adsorption stage, a first precipitation stage, a first drainage stage, an anaerobic stirring stage and an NO-containing stage from a raw water inlet stage every cycle 3 - -N wastewater inlet stage, anoxic stirring stage, sludge discharge stage, second precipitation stage, and ending the second water discharge stage for 10 stages; the related operation is controlled by an on-line feedback and control system (7);
(1) starting from a raw water inlet stage, starting a raw water inlet pump (3.1) to pump domestic sewage raw water into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet (3.2), wherein the raw water inlet amount of the domestic sewage raw water is V 1 ；
(2) Starting an aeration adsorption stage by starting a stirrer (3.8) and an aeration pump (3.5) after raw water inflow is completed, controlling the aeration quantity of a system through a gas flowmeter (3.6), keeping the dissolved oxygen concentration displayed by an SBR pH/DO tester (3.9) at 1.0-1.5 mg/L, and after the process lasts for 20-30 min, fully adsorbing soluble macromolecular organic matters on the surface of sludge, and closing the stirrer (3.8) and the aeration pump (3.5);
(3) precipitating for 20-30 min to enable the granular macromolecular organic matters and the sludge attached with the soluble macromolecular organic matters to be settled and separated from the supernatant;
(4) the first water discharge stage opens the water discharge valve I (3.11) to discharge V 1 The supernatant liquid in volume is discharged into an intermediate water tank I (4);
(5) after the drainage is finished, the sludge is precipitated and concentrated, a stirrer (3.8) is started to perform anaerobic stirring, and the dissolved oxygen concentration displayed by an SBR pH/DO determinator (3.9) is kept below 0.2 mg/L; at this time, the hydrolytic acidification bacteria contained in the sludge decompose the particle/soluble macromolecular organic matters and convert the particle/soluble macromolecular organic matters into soluble small-molecular organic matters (SCOD), and when the increase rate of the SCOD concentration is detected to be lower than 0.1mg (L.h) -1 And when the time lasts for more than 5min, the stirrer (3.8) is turned off, and the anaerobic stirring is stopped;
(6) containing NO 3 - -N wastewater inlet stage, NO is started 3 - -N wastewater inlet pump (3.3) through NO 3 - The N wastewater inlet (3.4) is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) and contains NO 3 - N waste water volume V 2 ；
(7) Containing NO 3 - After the water inflow of the N wastewater is completed, starting a stirrer (3.8) to start an anoxic stirring stage, wherein the dissolved oxygen concentration displayed by the SBR pH/DO determinator (3.9) is maintained below 0.2 mg/L; at the moment, denitrifying bacteria in the sludge carry out short-range denitrification reaction by utilizing SCOD generated by the anaerobic stirring section, and NO is generated 3 - Conversion of N to NO 2 - -N; when NO 3 - -when the N concentration is lower than 5mg/L, the stirrer (3.8) is turned off, stopping the anoxic stirring;
(8) opening a sludge discharge valve (3.14) within 3-5 min before the stirrer is closed in the anoxic stirring stage, and discharging sludge, so that the concentration of the volatile sludge in the SBR reactor is maintained at MLVSS=2500-5000 mg/L for a long time;
(9) precipitating for 20-30 min to finish mud-water separation;
is started in the second draining stage, the drain valve II (3.12) is opened, and V is calculated 2 The supernatant of the volume is discharged into the middleA water tank II (5) and the period is ended;
3.2 Operation of anaerobic ammoxidation UASB reactor: the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) pump the sewage in the intermediate water tank I (4) and the intermediate water tank II (5) into an anaerobic ammonia oxidation UASB reactor (6) respectively; wherein the sewage flows through the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) are respectively q 1 And q 2 The method comprises the steps of carrying out a first treatment on the surface of the The UASB reflux port (6.6) is connected with the UASB water inlet (6.3) through a reflux pump (6.7) to reflux, and the reflux ratio is set to be 100-150%; the effluent of the anaerobic ammoxidation UASB reactor (6) is discharged through a UASB water outlet (6.5).
4) When the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is used for carrying out SCOD at the end of an anaerobic section and NO at the end of an anoxic section 3 - -the fluctuation range of the N concentration for more than 10 periods does not exceed 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the water discharge ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) can be improved to R=30% by continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step 3);
5) When the drainage ratio is increased to 30%, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) has SCOD at the end of the anaerobic section and NO at the end of the anoxic section 3 - -the fluctuation range of the N concentration for more than 10 periods does not exceed 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the water discharge ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) can be improved to R=40% by continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step 3);
6) When the drainage ratio is increased to 40%, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) has SCOD at the end of the anaerobic section and NO at the end of the anoxic section 3 - -N concentration for 10 cyclesThe upper fluctuation range is not more than 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the water discharge ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) can be improved to R=50% by continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step 3);
7) When the drainage ratio is increased to 50%, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) has SCOD at the end of the anaerobic section and NO at the end of the anoxic section 3 - -the fluctuation range of the N concentration for more than 10 periods does not exceed 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the water discharge ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) can be improved to R=60% by continuing to operate according to the time length of each stage in the period described in the step 3), the valve opening mode and the device connection mode.
The device and the method for deep denitrification based on the adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation of the slow degradation organic matters have the following advantages:
1) The trapped slow degradation organic matters are converted into easily degradable organic matters by aeration, sedimentation, drainage trapping and trapping of the soluble and particle slow degradation organic matters and in-situ coupling hydrolysis acidification and short-range denitrification technologies, so that the problem that the slow degradation organic matters in domestic sewage raw water cannot be effectively utilized in NO in the denitrification process is solved 2 - The difficult problem of N accumulation does not need to add an external carbon source, and the adding amount of the carbon source in the short-cut denitrification system is further saved.
2) In the invention, two main devices are connected in series: the front-stage SBR reactor carries out biological adsorption, hydrolytic acidification and short-range denitrification processes, and the rear-end UASB reactor carries out anaerobic ammonia oxidation reaction, so that competition of denitrifying bacteria and anaerobic ammonia oxidation bacteria is avoided, growth of two bacterial groups is facilitated, growth is carried out under proper conditions, and stable operation of the whole system is ensured.
3) According to the invention, the sludge with short-range denitrification activity does not need to be inoculated, and the strain for realizing the short-range denitrification function can be enriched through the domestication of the common excess sludge of the sewage treatment plant.
4) Through condition control, stable NO in the front-stage SBR reactor can be realized 2 - The accumulation of N provides a stable substrate source for anaerobic ammonia oxidation bacteria in the back end UASB reactor, and provides a reference for the practical application and process regulation of the short-range denitrification-anaerobic ammonia oxidation technology.
5) The invention can realize domestic sewage raw water and NO-containing water 3 - The synchronous treatment process of the N wastewater provides a design idea.
Drawings
FIG. 1 is a schematic diagram of the structure of the device and method for deep denitrification by coupling adsorption hydrolysis and short-range denitrification and serial anaerobic ammoxidation based on slow degradation of organic matters.
In FIG. 1, (1) is a raw water tank, and (2) is a water tank containing NO 3 - An N wastewater tank, (3) a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor, (4) an intermediate tank I, (5) an intermediate tank II, (6) an anaerobic ammonia oxidation UASB reactor, and (7) an online feedback and control system; (3.1) raw water inlet pump, (3.2) raw water inlet, and (3.3) NO 3 - N wastewater inlet pump (3.4) is NO 3 - -N wastewater inlet, (3.5) aeration pump, (3.6) gas flow meter, (3.7) aeration disc, (3.8) stirrer, (3.9) SBR pH/DO meter, (3.10) water outlet, (3.11) drain valve I, (3.12) drain valve II, (3.13) sludge outlet, (3.12) sludge outlet valve; the water inlet pump I (6.1) for UASB (6.2) is UASB water inlet pump II (6.3) is UASB water inlet, (6.4) is UASB pH/DO tester, (6.5) is UASB water outlet, (6.6) is UASB reflux port, and (6.7) is reflux pump; (7.1) is a programmable controller, (7.2) is a computer, (7.3) is an aeration pump relay, and (7.4) is NO 3 - N wastewater inlet pump relay (7.5) is raw water inlet pump relay (7.6) is stirrerThe relay (7.7) is a reflux pump relay, (7.8) is a UASB water inlet pump I relay, a UASB water inlet pump II relay (7.9), (7.10) is a drain valve I relay, (7.11) is a drain valve II relay, (7.12) is an A/D signal converter conversion interface, and (7.13) is a D/A signal converter conversion interface.
FIG. 2 is a schematic diagram of the system operation flow of the present invention (device and method for deep denitrification by coupling adsorption hydrolysis with short-range denitrification and serial anaerobic ammoxidation based on slow degradation of organic matters).
Detailed Description
Embodiments of the present invention are described in detail below with reference to the attached drawing figures and examples:
as shown in fig. 1, the device for deep denitrification by coupling adsorption hydrolysis and short-range denitrification and serial anaerobic ammoxidation based on slow degradation organic matters is characterized by comprising: raw water tank (1) and NO-containing 3 - -N wastewater tank (2), bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3), intermediate tank I (4), intermediate tank II (5), anaerobic ammonia oxidation UASB reactor (6) and on-line feedback and control system (7);
wherein the bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is configured with: raw water inlet pump (3.1), raw water inlet (3.2) and NO 3 - -N wastewater inlet pump (3.3), NO 3 - -N wastewater inlet (3.4), aeration pump (3.5), gas flow meter (3.6), aeration disc (3.7), stirrer (3.8), SBR pH/DO meter (3.9), water outlet (3.10), drain valve I (3.11), drain valve II (3.12), sludge outlet (3.13), sludge outlet valve (3.14), wherein water outlet (3.10) is connected with drain valve I (3.11), drain valve II (3.12) through connecting pipe and tee joint; wherein the anaerobic ammonia oxidation UASB reactor (6) is configured with: UASB water inlet pump I (6.1), UASB water inlet pump II (6.2), UASB water inlet (6.3), UASB pH/DO determinator (6.4), UASB water outlet (6.5), UASB reflux inlet (6.6) and reflux pump (6.7); the online feedback and control system (7) comprises a programmable controller (7.1) and a computer (7.2); wherein the programmable controller (7.1) is internally provided with an aeration pump relay (7.3) and NO 3 - -N wastewater inlet pump relay (7.4), raw water inlet pump relay (7.5), stirringThe device comprises a device relay (7.6), a reflux pump relay (7.7), a UASB water inlet pump I relay (7.8), a UASB water inlet pump II relay (7.9), a drain valve I relay (7.10), a drain valve II relay (7.11), a mud valve relay (7.12), an A/D signal converter conversion interface (7.13) and a D/A signal converter conversion interface (7.14);
domestic sewage raw water in the raw water tank (1) is pumped into the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet pump (3.1) through a raw water inlet (3.2), and then pumped into an intermediate water tank I (4) from a water outlet (3.10) through a drain valve I (3.11); the NO-containing 3 - -NO in the N wastewater tank (2) 3 - -N pollutant wastewater pass through NO 3 - -N wastewater inlet pump (3.3) through NO 3 - -N wastewater inlet (3.4) is pumped into the bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) and then from water outlet (3.10) into intermediate water tank II (5) through drain valve II (3.12); wherein a UASB water inlet (6.3) configured by the anaerobic ammonia oxidation UASB reactor (6) is respectively connected with an intermediate water tank I (4) and an intermediate water tank II (5) through a UASB water inlet pump I (6.1) and a UASB water inlet pump II (6.2); the UASB reflux port (6.6) is connected with a UASB water inlet (6.3) through a reflux pump (6.7) for reflux;
In the on-line feedback and control system (7), an aeration pump relay (7.3) is connected with an aeration pump (3.5); NO (NO) 3 - -N wastewater inlet pump relay (7.4) and NO 3 - -N wastewater inlet pump (3.3) connected; the raw water inlet pump relay (7.5) is connected with the raw water inlet pump (3.1); the stirrer relay (7.6) is connected with the stirrer (3.8); the reflux pump relay (7.7) is connected with the reflux pump (6.7); the UASB water inlet pump I relay (7.8) is connected with the UASB water inlet pump I (6.1); a UASB water inlet pump II relay (7.9) and a UASB water inlet pump II (6.2); the drain valve I relay (7.10) is connected with the drain valve I (3.11); the drain valve II relay (7.11) is connected with the drain valve II (3.12); the mud valve relay (7.12) is connected with the mud valve (3.14); the programmable controller (7.1) is connected to the computer (7.2) through the A/D signal converter conversion interface (7.13) and converts the sensor signal into a digital signal to be transmitted to the computer (7.2); the computer (7.2) is connected with the programmable controller through the D/A signal converter conversion interface (7.14)(7.1) connecting and transmitting the digital signal to the programmable controller (7.1);
in the test process, the domestic sewage raw water is diluted to 20L by adopting 18L of the septic tank effluent of the family member region of the Beijing industrial university after sedimentation, and then 600ml of primary sludge (MLSS=7000-12000 mg/L) of a small red gate sewage treatment plant is mixed for simulation, and the relevant water quality characteristics are as follows: NH (NH) 4 + The concentration of the-N is 50-70 mg/L, NO 2 - The concentration of the-N is 0 to 1.0mg/L, NO 3 - The concentration of the-N is 0 to 1.0mg/L, the concentration of the soluble organic matters SCOD is 150 to 250mg/L, the concentration of the total organic matters TCOD is 320 to 480mg/L, and PO 4 3- The P concentration is 2.0-4.0 mg/L, pH and the water temperature is 7.2-7.7, and the water temperature is 13-28 ℃. By NaNO 3 Water distribution simulation NO 3 - -N waste water, NO 3 - The concentration of the-N is 70mg/L, and the concentration of the suspended substance SS is 200-350 mg/L. As shown in FIG. 1, each reactor is made of organic glass, the total volume of the reactor is 11L, and the effective volume is 7.5L. An anaerobic ammoxidation UASB reactor (6) with a total volume of 5L and an effective volume of 3L.
The specific operation is as follows:
1) And (3) starting a system:
1.1 Start-up of the biosorption/hydrolytic acidification/short-cut denitrification SBR reactor: the inoculation of sludge is to add excess sludge of a sewage plant, and the sludge concentration of the SBR reactor is MLVSS=2500-5000 mg/L; controlling the residence time of the sludge to be 25-50 days; two cycles are operated each day, each cycle being 12 hours; in each period, the simulated domestic sewage raw water in the raw water tank (1) is pumped into the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through the raw water inlet pump (3.1), the stirrer (3.8) and the aeration pump (3.5) are started to perform aeration adsorption, the aeration quantity of the system is controlled through the gas flowmeter (3.6), the dissolved oxygen concentration displayed by the SBR pH/DO tester (3.9) is maintained at 1.0-1.5 mg/L, after the process lasts for 20min, the sediment is carried out for 20min, and then the water is discharged, and the water discharge ratio is 20%; after the drainage is finished, the sludge is precipitated and concentrated, a stirrer (3.8) is started to perform anaerobic stirring for 7.5 hours, and the temperature of an anaerobic section is controlled at 28-30 ℃; then turn on NO 3 - -N wasteThe water inlet pump (3.3) is through NO 3 - The N wastewater inlet (3.4) is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3), anoxic stirring is carried out for 60 minutes, and the anoxic section does not control the temperature; when the concentration increment of the initial end SCOD of the anaerobic section reaches more than 50% of the inflow TCOD, the end NO of the anoxic section 3 - And when the N concentration is less than 5mg/L and the stable operation is carried out for more than 10 cycles, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is considered to be successfully started.
1.2 Start-up of anaerobic ammoxidation UASB reactor: the inoculated sludge is short-cut nitrification-anaerobic ammonia oxidation (PNA) pilot-scale granular sludge of a sewage treatment plant of a high-stele store, so that the concentration of the sludge in the reactor is MLSS=2500 mg/L-3000 mg/L, the hydraulic retention time is 4h, the sludge is not actively discharged, and the reaction temperature is controlled to be 25-28 ℃; the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) pump the sewage in the intermediate water tank I (4) and the intermediate water tank II (5) into an anaerobic ammonia oxidation UASB reactor (6) respectively; when NH in effluent 4 + -N concentration, NO 2 - And when the N concentration is less than 1mg/L and the stable operation is performed for more than 40 hours, the anaerobic ammonia oxidation UASB reactor (6) is considered to be successfully started.
2) Operation of the system
2.1 Operation of the biosorption/hydrolytic acidification/short-cut denitrification SBR reactor): the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) operates for two cycles each day, each cycle is 12 hours, and the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor sequentially undergoes domestic sewage raw water inflow for 5min, aeration adsorption for 20min, a first precipitation stage for 20min, a first drainage stage for 5min, anaerobic stirring for 450min and NO-containing reaction kettle 3 - -N wastewater is fed for 5min, subjected to anoxic stirring for 60min (including 3min of mud discharge at the end of the stage), subjected to a second precipitation stage for 30min, subjected to a drainage stage for 5min, and left idle for 120min; in each period, the simulated domestic sewage raw water in the raw water tank (1) is pumped into the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through the raw water inlet pump (3.1), the stirrer (3.8) and the aeration pump (3.5) are started to perform aeration adsorption, the aeration quantity of the system is controlled through the gas flowmeter (3.6), the dissolved oxygen concentration displayed by the SBR pH/DO tester (3.9) is maintained at 1.0-1.5 mg/L, after the process lasts for 20min, the sediment is carried out for 20min, and then the water is discharged, and the water discharge ratio is 20%; the discharged water enters an intermediate water tank I (4) and is dischargedNH 4 + The concentration of the-N is 10-14 mg/L, the concentration of the soluble organic matters SCOD is 25-40 mg/L, and the concentration of the total organic matters TCOD is 40-65 mg/L; after the water drainage is finished, the sludge is precipitated and concentrated, a stirrer (3.8) is started to perform anaerobic stirring for 7.5 hours, and the reaction temperature is controlled to be 28-30 ℃ in an anaerobic section; then turn on NO 3 - -N wastewater inlet pump (3.3) through NO 3 - The N wastewater inlet (3.4) is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3), anoxic stirring is carried out for 60 minutes, and the anoxic section does not control the temperature; opening a sludge discharge valve (3.14) within 3min before the anoxic stirring is finished, and discharging sludge to ensure that the concentration of the volatile sludge in the SBR reactor is maintained at MLVSS=2500-5000 mg/L for a long time; then sediment drainage is carried out, the anoxic section drainage enters an intermediate water tank II (5), and the effluent NO 3 - The concentration of the-N is less than 1mg/L, and the effluent NO 2 - The concentration of the-N is 7-12 mg/L.
2.2 Operation of anaerobic ammoxidation UASB reactor: the hydraulic retention time is 4 hours, the mud is not actively discharged, the reflux ratio is set to be 100%, and the reaction temperature is controlled to be 25-28 ℃; the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) pump sewage in the intermediate water tank I (4) and the intermediate water tank II (5) into the anaerobic ammonia oxidation UASB reactor (6), and a reflux port (6.6) at the upper part of the UASB reactor is connected with the UASB water inlet (6.3) through a reflux pump (6.7) for reflux; wherein the sewage flow rate through the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) is 0.125L/h, and the mud-water mixture flow rate through the reflux pump (6.7) is 0.25L/h; the effluent of the anaerobic ammoxidation UASB reactor (6) is discharged through a UASB water outlet (6.5).
3) The system increases the drainage ratio R by: when the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is used for carrying out SCOD at the end of an anaerobic section and NO at the end of an anoxic section 3 - -the range of fluctuation within 10 cycles or more of the N concentration does not exceed 10% of the mean value of the detection; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the biological adsorption can be improved by continuing to operate according to the time length of each stage in the period, the valve opening mode and the device connection mode described in 2.1) The drainage ratio of the hydrolytic acidification/short-cut denitrification SBR reactor (3) is up to R=30%;
after the drainage ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) is increased to R=30%, when the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) has an anaerobic end SCOD and an anoxic end NO 3 - -the range of fluctuation within 10 cycles or more of the N concentration does not exceed 10% of the mean value of the detection; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the water discharge ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) can be improved to R=40% by continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in 2.1);
after the drainage ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) is increased to R=40%, when the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) has an anaerobic end SCOD and an anoxic end NO 3 - -the range of fluctuation within 10 cycles or more of the N concentration does not exceed 10% of the mean value of the detection; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; the water discharge ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) can be improved to R=50% by continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in 2.1);
after the drainage ratio of the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) is increased to R=50%, when the biological adsorption/hydrolytic acidification/short-cut denitrification SBR reactor (3) has an anaerobic end SCOD and an anoxic end NO 3 - -the range of fluctuation within 10 cycles or more of the N concentration does not exceed 10% of the mean value of the detection; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; according to 2.1)The described period duration, valve opening mode and device connection mode continue to run, so that the drainage ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) can be improved to R=60%;
the key parameters mentioned in the operation of the system at different drainage ratios R are shown in the following table:
TABLE 1 different drainage ratios R System Key parameters
Figure BDA0003132269030000131
Figure BDA0003132269030000141
The long-term operation result of the test system shows that: after the system is stable in operation, the solubility and particle slow degradation organic matter trapping rate of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) reaches more than 82%, and 60% -85% of NO is realized 2 - -N accumulation rate; the total organic matter (TCOD) removal rate of the system is over 85 percent, and effluent NH is discharged 4 + The concentration of N is less than 5mg/L, the total nitrogen concentration is less than 15mg/L, the first-level A standard of pollutant emission standard of urban sewage treatment plant (GB 18918-2002) is met, and the effective utilization of the dissolubility and particle slow degradation organic matters and the deep denitrification of the domestic sewage with low carbon nitrogen ratio are realized.
The specific implementation manner of the invention is used for facilitating the better understanding of the application of the invention by those skilled in the art; the practice of the invention is not limited thereto and simple modifications made by those skilled in the art are within the scope of the invention.

Claims (1)

1. The method for deep denitrification based on the adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation of slow degradation organic matters is characterized by comprising the following steps: raw water tank (1) and NO-containing 3 - -N wastewater tank (2), biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3),An intermediate water tank I (4), an intermediate water tank II (5), an anaerobic ammonia oxidation UASB reactor (6) and an online feedback and control system (7);
wherein the bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is configured with: raw water inlet pump (3.1), raw water inlet (3.2) and NO 3 - -N wastewater inlet pump (3.3), NO 3 - -N wastewater inlet (3.4), aeration pump (3.5), gas flow meter (3.6), aeration disc (3.7), stirrer (3.8), SBR pH/DO meter (3.9), water outlet (3.10), drain valve I (3.11), drain valve II (3.12), sludge outlet (3.13), sludge outlet valve (3.14), wherein water outlet (3.10) is connected with drain valve I (3.11), drain valve II (3.12) through connecting pipe and tee joint; wherein the anaerobic ammonia oxidation UASB reactor (6) is configured with: UASB water inlet pump I (6.1), UASB water inlet pump II (6.2), UASB water inlet (6.3), UASB pH/DO determinator (6.4), UASB water outlet (6.5), UASB reflux inlet (6.6) and reflux pump (6.7); the online feedback and control system (7) comprises a programmable controller (7.1) and a computer (7.2); wherein the programmable controller (7.1) is internally provided with an aeration pump relay (7.3) and NO 3 - -N wastewater intake pump relay (7.4), raw water intake pump relay (7.5), stirrer relay (7.6), reflux pump relay (7.7), UASB intake pump I relay (7.8), UASB intake pump II relay (7.9), drain valve I relay (7.10), drain valve II relay (7.11), mud valve relay (7.12), a/D signal converter conversion interface (7.13), D/a signal converter conversion interface (7.14);
Domestic sewage raw water in the raw water tank (1) is pumped into the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet pump (3.1) through a raw water inlet (3.2), and then pumped into an intermediate water tank I (4) from a water outlet (3.10) through a drain valve I (3.11); the NO-containing 3 - -NO in the N wastewater tank (2) 3 - -N pollutant wastewater pass through NO 3 - -N wastewater inlet pump (3.3) through NO 3 - -N wastewater inlet (3.4) is pumped into the bio-adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) and then from water outlet (3.10) into intermediate water tank II (5) through drain valve II (3.12); wherein the anaerobic ammoxidation UASB reactor (6) is configuredThe UASB water inlet (6.3) is respectively connected with the intermediate water tank I (4) and the intermediate water tank II (5) through the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2); the UASB reflux port (6.6) is connected with a UASB water inlet (6.3) through a reflux pump (6.7) for reflux;
in the on-line feedback and control system (7), an aeration pump relay (7.3) is connected with an aeration pump (3.5); NO (NO) 3 - -N wastewater inlet pump relay (7.4) and NO 3 - -N wastewater inlet pump (3.3) connected; the raw water inlet pump relay (7.5) is connected with the raw water inlet pump (3.1); the stirrer relay (7.6) is connected with the stirrer (3.8); the reflux pump relay (7.7) is connected with the reflux pump (6.7); the UASB water inlet pump I relay (7.8) is connected with the UASB water inlet pump I (6.1); a UASB water inlet pump II relay (7.9) and a UASB water inlet pump II (6.2); the drain valve I relay (7.10) is connected with the drain valve I (3.11); the drain valve II relay (7.11) is connected with the drain valve II (3.12); the mud valve relay (7.12) is connected with the mud valve (3.14); the programmable controller (7.1) is connected to the computer (7.2) through the A/D signal converter conversion interface (7.13) and converts the sensor signal into a digital signal to be transmitted to the computer (7.2); the computer (7.2) is connected with the programmable controller (7.1) through a D/A signal converter conversion interface (7.14) and transmits digital signals to the programmable controller (7.1);
The method comprises the following steps:
1) And (3) starting a system:
1.1 Start-up of the biosorption/hydrolytic acidification/short-cut denitrification SBR reactor: adding excess sludge of a sewage plant into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) so that the concentration of the volatile sludge in the reactor is MLVSS=2500-5000 mg/L; controlling the residence time of the sludge to be 25-50 days; the reactor is operated for 2 cycles per day, and each cycle is started from a raw water inlet stage and sequentially goes through an aeration adsorption stage, a first precipitation stage, a first water discharge stage, an anaerobic stirring stage and an NO-containing stage 3 - -N wastewater inlet stage, anoxic stirring stage, sludge discharge stage, second precipitation stage, and ending the second water discharge stage for 10 stages; the related operation is controlled by an on-line feedback and control system (7); in each period, the raw water tank (1) simulates domestic sewageRaw water is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet pump (3.1), a stirrer (3.8) and an aeration pump (3.5) are started to start aeration adsorption, the aeration quantity of the system is controlled through a gas flowmeter (3.6), the concentration of dissolved oxygen displayed by an SBR pH/DO tester (3.9) is maintained at 1.0-1.5 mg/L, the process lasts for 20-30 min, and then precipitation is carried out for 20-30 min and water is discharged; after the drainage is completed, the sludge is precipitated and concentrated, a stirrer (3.8) is started for anaerobic stirring, and when the increase rate of the concentration of SCOD is detected to be lower than 0.1mg (L.h) -1 And when the time lasts for more than 5min, the stirrer (3.8) is turned off, and the anaerobic stirring is stopped; then turn on NO 3 - -N wastewater inlet pump (3.3) through NO 3 - The N wastewater inlet (3.4) is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) to be subjected to anoxic stirring, and when NO 3 - -when the N concentration is lower than 5mg/L, the stirrer (3.8) is turned off, stopping the anoxic stirring; when the concentration increment of the initial end SCOD of the anaerobic section reaches more than 50% of the inflow TCOD, the end NO of the anoxic section 3 - When the N concentration is less than 5mg/L and the stable operation is carried out for more than 10 cycles, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is considered to be successfully started;
1.2 Start-up of anaerobic ammoxidation UASB reactor: adding sludge with ammonia oxidation activity into an anaerobic ammonia oxidation UASB reactor (6) to ensure that the sludge concentration in the reactor is MLSS=2500 mg/L-3000 mg/L; when NH in effluent 4 + -N concentration, NO 2 - When the N concentration is less than 1mg/L and the stable operation is carried out for more than 40 hours, the anaerobic ammonia oxidation UASB reactor (6) is considered to be successfully started;
2) Setting the parameters of a reactor:
according to the set drainage ratio R, SBR of the SBR reactor, the effective volume V of the reactor 0 Raw water intake volume V of domestic sewage 1 Containing NO 3 - N wastewater inlet volume V 2 Containing NO 3 - NO in N wastewater 3 - -N concentration C N Concentration C of total organic matter (TCOD) in domestic sewage raw water C The sewage flow rate through the UASB water inlet pump I (6.1) is q 1 The sewage flow rate through the UASB water inlet pump II (6.2) is q 2 、UASB hydraulic retention time is HRT UASB The respective parameter relationships satisfy the following formulas (1), (2), (3), (4):
V 0 ×R ＝ V 1 ＝ V 2 formula (1)
(C C ×V 1 )/( C N ×V 2 ) =3.5 to 6.0 formula (2)
q 1 ×HRT UASB ＝ V 1 Formula (3)
q 2 ×HRT UASB ＝ V 2 Formula (4)
The drainage ratio initial value is set to r=20%;
UASB hydraulic retention time is set to be HRT UASB ＝1.0～4.0h；
3) Runtime adjustment operation:
3.1 Operation of the biosorption/hydrolytic acidification/short-cut denitrification SBR reactor): the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) sequentially goes through an aeration adsorption stage, a first precipitation stage, a first drainage stage, an anaerobic stirring stage and an NO-containing stage from a raw water inlet stage every cycle 3 - -N wastewater inlet stage, anoxic stirring stage, sludge discharge stage, second precipitation stage, and ending the second water discharge stage for 10 stages; the related operation is controlled by an on-line feedback and control system (7);
(1) starting from a raw water inlet stage, starting a raw water inlet pump (3.1) to pump domestic sewage raw water into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) through a raw water inlet (3.2), wherein the raw water inlet amount of the domestic sewage raw water is V 1 ；
(2) Starting an aeration adsorption stage by starting a stirrer (3.8) and an aeration pump (3.5) after raw water inflow is completed, controlling the aeration quantity of a system through a gas flowmeter (3.6), keeping the dissolved oxygen concentration displayed by an SBR pH/DO tester (3.9) at 1.0-1.5 mg/L, and after the process lasts for 20-30 min, fully adsorbing soluble macromolecular organic matters on the surface of sludge, and closing the stirrer (3.8) and the aeration pump (3.5);
(3) precipitating for 20-30 min to enable the granular macromolecular organic matters and the sludge attached with the soluble macromolecular organic matters to be settled and separated from the supernatant;
(4) the first water discharge stage opens the water discharge valve I (3.11) to discharge V 1 The supernatant liquid in volume is discharged into an intermediate water tank I (4);
(5) after the drainage is finished, the sludge is precipitated and concentrated, a stirrer (3.8) is started to perform anaerobic stirring, and the dissolved oxygen concentration displayed by an SBR pH/DO determinator (3.9) is kept below 0.2 mg/L; at this time, the hydrolytic acidification bacteria contained in the sludge decompose the particle/soluble macromolecular organic matters and convert the particle/soluble macromolecular organic matters into soluble small-molecular organic matters (SCOD), and when the increase rate of the SCOD concentration is detected to be lower than 0.1mg (L.h) -1 And when the time lasts for more than 5min, the stirrer (3.8) is turned off, and the anaerobic stirring is stopped;
(6) containing NO 3 - -N wastewater inlet stage, NO is started 3 - -N wastewater inlet pump (3.3) through NO 3 - The N wastewater inlet (3.4) is pumped into a biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) and contains NO 3 - N waste water volume V 2 ；
(7) Containing NO 3 - After the water inflow of the N wastewater is completed, starting a stirrer (3.8) to start an anoxic stirring stage, wherein the dissolved oxygen concentration displayed by the SBR pH/DO determinator (3.9) is maintained below 0.2 mg/L; at the moment, denitrifying bacteria in the sludge carry out short-range denitrification reaction by utilizing SCOD generated by the anaerobic stirring section, and NO is generated 3 - Conversion of N to NO 2 - -N；
When NO 3 - -when the N concentration is lower than 5mg/L, the stirrer (3.8) is turned off, stopping the anoxic stirring;
(8) opening a sludge discharge valve (3.14) within 3-5 min before the stirrer is closed in the anoxic stirring stage to discharge sludge, so that the concentration of the volatile sludge in the SBR reactor is maintained at MLVSS=2500-5000 mg/L for a long time
(9) Precipitating for 20-30 min to finish mud-water separation;
is started in the second draining stage, the drain valve II (3.12) is opened, and V is calculated 2 The volume of supernatant is discharged into an intermediate water tank II (5),
ending the period;
3.2 Operation of anaerobic ammoxidation UASB reactor: the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) pump the sewage in the intermediate water tank I (4) and the intermediate water tank II (5) into an anaerobic ammonia oxidation UASB reactor (6) respectively; wherein the sewage flows through the UASB water inlet pump I (6.1) and the UASB water inlet pump II (6.2) are respectively q 1 And q 2 The method comprises the steps of carrying out a first treatment on the surface of the The UASB reflux port (6.6) is connected with the UASB water inlet (6.3) through a reflux pump (6.7) to reflux, and the reflux ratio is set to be 100-150%; the effluent of the anaerobic ammonia oxidation UASB reactor (6) is discharged through a UASB water outlet (6.5);
4) When the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) is used for carrying out SCOD at the end of an anaerobic section and NO at the end of an anoxic section 3 - -the fluctuation range of the N concentration for more than 10 periods does not exceed 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step 3), and improving the drainage ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) to R=30%;
5) When the drainage ratio is increased to 30%, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) has SCOD at the end of the anaerobic section and NO at the end of the anoxic section 3 - -the fluctuation range of the N concentration for more than 10 periods does not exceed 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step 3), and improving the drainage ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) to R=40%;
6) When the drainage ratio is increased to 40%, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) has SCOD at the end of the anaerobic section and NO at the end of the anoxic section 3 - -N concentration ranges from 10 cycles or moreNot more than 10% of the average value of the detection; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; continuing to operate according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step 3), and improving the drainage ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) to R=50%;
7) When the drainage ratio is increased to 50%, the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) has SCOD at the end of the anaerobic section and NO at the end of the anoxic section 3 - -the fluctuation range of the N concentration for more than 10 periods does not exceed 10% of the detection average value; and the anaerobic ammonia oxidation UASB reactor (6) outputs water NH 4 + The concentration of N is not higher than 5mg/L for more than 10 periods, and the NO is discharged 3 - -N concentration not higher than 10mg/L for more than 10 cycles; and (3) continuously operating according to the time length, the valve opening mode and the device connection mode of each stage in the period described in the step (3), and improving the drainage ratio of the biological adsorption/hydrolytic acidification/short-range denitrification SBR reactor (3) to R=60%.
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