CN107540095B - Method for rapidly recovering sulfur cycle coupling denitrification dephosphorization system - Google Patents
Method for rapidly recovering sulfur cycle coupling denitrification dephosphorization system Download PDFInfo
- Publication number
- CN107540095B CN107540095B CN201610499405.3A CN201610499405A CN107540095B CN 107540095 B CN107540095 B CN 107540095B CN 201610499405 A CN201610499405 A CN 201610499405A CN 107540095 B CN107540095 B CN 107540095B
- Authority
- CN
- China
- Prior art keywords
- sulfur
- sulfate
- cycle
- phosphorus
- reducing bacteria
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention provides a method for quickly recovering a sulfur cycle coupled denitrifying phosphorus removal system, so that the phosphorus removal and sulfur cycle capability of the system after breakdown can be quickly recovered. Each operation cycle of the system comprises the following steps in sequence: a water intake phase, an anaerobic phase, an anoxic phase, a sedimentation phase, a drainage phase, and optionally an idle phase. The method comprises the following specific operations: when the phosphorus and sulfur removal circulation capacity of the sulfur circulation coupling denitrification phosphorus removal system is collapsed, activated sludge enriched by sulfate reducing bacteria is added to the system at one time in a water inlet stage or an anaerobic stage, so that the phosphorus and sulfur removal circulation capacity of the system is recovered. The method can quickly recover the collapsed sulfur cycle coupling denitrification dephosphorization system in a short time, has low investment, simple and convenient operation and practical value, and simultaneously has reference significance for the treatment of the activated sludge method under extreme water quality conditions, such as high-temperature, high-salinity and high-sulfate-content sewage.
Description
Technical Field
The invention belongs to the technical field of environmental protection, particularly relates to a biological treatment technology of wastewater, and more particularly relates to a method for rapidly recovering the capacity of a sulfur cycle coupling denitrification dephosphorization system after breakdown.
Background
The technology for removing phosphorus by coupling sulfur cycle with denitrification is characterized in that under the condition of water quality with high sulfate content, sulfate reducing bacteria and sulfur oxidizing bacteria participate together, the sulfur cycle is used as an electron carrier, nitrate is used as an electron acceptor, and intracellular storage polysulfide (poly S) and poly beta hydroxyalkanoate (PHA) are used as electron donors, so that the aims of removing carbon, removing nitrogen and absorbing phosphorus are synchronously realized by the principle of one-carbon dual use. The technology of sulfur cycle coupling denitrification dephosphorization has the advantages of carbon source saving, aeration amount saving, low sludge yield and the like, so the technology is known as a novel sustainable sewage treatment technology and becomes one of the hot spots of competitive research in the field of sewage treatment.
However, sulfur cycle coupled denitrification phosphorus removal systems lack effective strain capacity for environmental changes under certain conditions. For example, the operating conditions of the system may fluctuate or even deteriorate due to the fluctuation of the quality and quantity of inlet water, the change of environmental influence factors, improper control of the process flow, and the like, and the operating conditions of the system cannot reach the discharge standard of the quality of sewage. One of the solutions to cope with the above problems is to re-acclimate the cultured activated sludge, but it takes a long time (at least 50 days (d)). Therefore, effective solution is to develop a method capable of rapidly recovering the capacity of the sulfur cycle coupled denitrification phosphorus removal system after breakdown, but a method for rapidly recovering the deteriorated system is rarely reported.
Disclosure of Invention
In order to solve the problems, the invention researches a sulfur cycle coupling denitrification dephosphorization system, and finds that a certain relation exists between the sulfur cycle amount (including the reduction amount and the generation amount of sulfate) and the dephosphorization rate (also called as the phosphate removal rate) in the long-term operation process of the system. Through further intensive research, the invention provides a method for recovering the capacity of a sulfur-cycle-coupled denitrifying phosphorus removal system after breakdown, wherein the sulfur-cycle-coupled denitrifying phosphorus removal system utilizes sludge containing wastewater treatment microorganisms to treat sulfur-containing wastewater, and each operation cycle of the system sequentially comprises the following steps: a water intake phase, an anaerobic phase, an anoxic phase, a sedimentation phase, a drainage phase, and optionally an idle phase. The method is characterized in that when the phosphorus removal and sulfur circulation capacity of the sulfur circulation coupling denitrification phosphorus removal system is collapsed, activated sludge enriched by sulfate reducing bacteria is added at one time in a water inlet stage or an anaerobic stage, so that the system recovers the capacity.
The operation effect of the sulfur cycle coupling denitrification dephosphorization system before deterioration (namely breakdown) is compared with the operation effect of the sulfur cycle coupling denitrification dephosphorization system after recovery, and the reason is specifically researched and analyzed, so that the stable operation condition of the system is provided, and the optimization condition and the theoretical basis are provided for specifically putting the sulfur cycle coupling denitrification dephosphorization process into application. The method can lead the collapsed sulfur cycle coupling denitrification dephosphorization system to be quickly recovered in a shorter time. The method has the advantages of low investment and simple and convenient operation, can quickly improve and recover the treatment effect of the sulfur cycle coupling denitrification dephosphorization system, quickly recover and restart deteriorated processes, has practical value and is beneficial to popularization and use. In addition, the method of the invention has reference significance for the treatment of the activated sludge process under extreme water quality conditions, such as high temperature, high salinity and high sulfate content sewage.
Drawings
FIG. 1 is a schematic diagram of an exemplary batch reactor that may be used in the present invention.
Fig. 2 shows the operational effect of embodiment 1.
Fig. 3 shows the operational effect of embodiment 2.
Detailed Description
In order that those skilled in the art will better understand the invention, a more detailed description is provided below with reference to specific embodiments and the accompanying drawings, but the invention is not limited thereto.
The method provided by the invention can be used for recovering the capacity of a sulfur cycle coupling denitrification phosphorus removal system after breakdown, wherein the sulfur cycle coupling denitrification phosphorus removal system utilizes sludge containing microorganisms for wastewater treatment to remove phosphorus from sulfur-containing wastewater, and each operation period of the system sequentially comprises the following steps: a water intake phase, an anaerobic phase, an anoxic phase, a sedimentation phase, a drainage phase, and optionally an idle phase. The method is characterized in that when the phosphorus removal and sulfur circulation capacity of the sulfur circulation coupling denitrification phosphorus removal system is collapsed, activated sludge enriched by sulfate reducing bacteria is added at one time in a water inlet stage or an anaerobic stage, so that the phosphorus removal and sulfur circulation capacity of the system is recovered.
The sulfur cycle coupled denitrifying phosphorus removal system may employ any suitable reactor, such as a batch reactor, for treating high salinity sulfur-containing wastewater with sludge containing wastewater treatment microorganisms. An exemplary sequencing batch reactor useful in the present invention is shown in FIG. 1 and comprises a reaction vessel 1 having a volume, the reaction vessel being equipped with an agitator 2 and a pH probe 4, the pH probe being connected to a pH controller 5 which allows the pH within the reaction vessel to be controlled within a range (e.g., pH controlled to 7.2-8.4) by adjusting the addition of an acid solution 6 (e.g., aqueous HCl, for example, at a concentration of 0.5mol/L) or a base solution 7 (e.g., aqueous NaOH, for example, at a concentration of 0.5 mol/L). The reaction vessel 1 is connected with a water inlet tank 9 and a water outlet pipeline 3. Nitrate is added to the reaction vessel 1 by a pump 10. Activated sludge enriched by sulfate reducing bacteria which is added at one time is added into the reaction vessel 1 through a sampling port 8.
The functional microorganisms in the sludge containing the microorganisms for wastewater treatment include a combination of sulfate-reducing bacteria and sulfur-oxidizing bacteria. Suitable sulfate-reducing bacteria and sulfur-oxidizing bacteria may be populations commonly used in the art, for example, sulfate-reducing bacteria may be selected from the genera desulfobacterium (Desulfobacter), desulfobulfobacter (desulfobulbulbus), desulfomonas (Desulfuromonas), and sulfur-oxidizing bacteria may be selected from the genera settlementa (Sedimenticola), Thialomonad (Thiohalomonas), Thiotrichaceae (Thiotrichaceae). The pH value of the sulfur circulation coupling denitrification dephosphorization system can be controlled within the range of 7.2-8.4 during operation, and is preferably controlled within the range of 7.2-7.8.
Each operation period of the sulfur cycle coupling denitrification dephosphorization system sequentially comprises: a water intake phase, an anaerobic phase, an anoxic phase, a sedimentation phase, a drainage phase, and optionally an idle phase. In the water inlet stage, sulfur-containing wastewater to be dephosphorized is added into the system. The anaerobic stage is an operation stage of the sulfur cycle coupling denitrification dephosphorization system (reactor) from the beginning of stirring the sewage to the stage before the anoxic stage under the condition of stopping the contact with the air after the water inlet stage. In the anaerobic stage, the functional population hydrolyzes the intracellular polyphosphate into phosphate and releases the phosphate to the outside of cells, utilizes the energy generated by hydrolysis to rapidly absorb a carbon source and uses glycolysis to provide reducing power to synthesize an internal carbon source PHA, and simultaneously generates polysulfide along with sulfate reduction and stores the polysulfide in the cells. And after the anaerobic stage, adding water-soluble nitrate into the system to start the anoxic stage, so that an anoxic environment is formed in the reactor until the nitrate in the water body is completely consumed or phosphate is completely removed. In the anoxic stage, the functional population provides electrons by using intracellular PHA and polysulphide, takes nitrate as an electron acceptor to carry out oxidative phosphorylation to generate energy, one part provides cell synthesis and life activity maintenance, the other part is used for excessively absorbing inorganic phosphate in sewage and synthesizing polyphosphate to be stored in cells, and simultaneously, the nitrate is reduced to nitrogen, thereby achieving the aim of nitrogen and phosphorus removal coupled with sulfur cycle. The nitrate added to the sulfur cycle coupled denitrifying phosphorus removal system (reactor) during the anoxic stage is a water-soluble nitrate, which can be selected from sodium nitrate, potassium nitrate, magnesium nitrate, for example. After the anoxic phase, the agitation is stopped and the precipitation phase is entered. The treated water is then discharged from the system. The system may also experience an idle period of time, as the case may be, before proceeding to the next operational cycle.
Generally, the collapse of the phosphorus removal and sulfur cycle capacity of a sulfur cycle coupled denitrifying phosphorus removal system means that the system has a phosphate removal rate of 20% or less and a sulfur cycle capacity of 5mg S/L or less. In some embodiments, when the sulfur cycle coupled denitrification phosphorus removal system crashes, the sludge concentration in the system may drop below 4.6 g/L.
When the phosphorus removal and sulfur cycle capabilities of the sulfur cycle coupled denitrification phosphorus removal system collapse, the method of the invention can be implemented so that the capabilities are restored. Specifically, during the operation period when the system is about to be recovered from the collapse, the system is recovered from the phosphorus removal and sulfur circulation capacity by once adding the activated sludge enriched with sulfate reducing bacteria during the water feeding stage or the anaerobic stage.
The enrichment degree of the activated sludge enriched with the sulfate-reducing bacteria may be, for example, 40% or more, preferably 50% or more, and more preferably 60% or more. The enrichment degree of sulfate-reducing bacteria can be detected by a microorganism detection method (16S rRNA gene sequencing method) by the ratio (%) of the number of sulfate-reducing bacteria to the total number of all bacteria in the activated sludge. The activated sludge enriched by the sulfate reducing bacteria has higher activity, and the organic load rate can be 1.2kg COD/m 3 More than d, even 1.6kg COD/m 3 And/d or more. The activated sludge enriched by the sulfate reducing bacteria has higher sludge concentration, for example, more than 8g/L, even more than 10g/LIn addition, the hydraulic retention time of the corresponding reactor may be 6 to 8 hours (h). The activated sludge enriched with the sulfate reducing bacteria mainly comprises functional populations of the sulfate reducing bacteria, but in the sulfur circulation coupling denitrification phosphorus removal system, the sulfur oxidizing bacteria and the sulfate reducing bacteria are in a symbiotic relationship, and the sulfur oxidizing bacteria in the system can be recovered again by adding the activated sludge enriched with the sulfate reducing bacteria. The sulfate-reducing bacteria in the activated sludge enriched with the sulfate-reducing bacteria may be the same as or different from the sulfate-reducing bacteria in the sludge containing the microorganisms for wastewater treatment, and may be selected from the group consisting of desulfobacterium (Desulfobacter), desulfobulexis (Desulfobulbus), and desulfomonas (desulffuromonas).
The activated sludge enriched with the sulfate reducing bacteria can be added into the system at one time in a water inlet stage or an anaerobic stage, and the two modes can recover the activity of the sulfate reducing bacteria in the system. Preferably, the activated sludge enriched in sulfate-reducing bacteria is added in the water intake stage, which is beneficial to shortening the whole reaction period.
The sulfate-reducing bacteria-enriched activated sludge may be prepared in the following manner. Activated sludge in an anaerobic fermentation tank of a sewage plant is inoculated by using another sequencing batch reactor as shown in figure 1. Under the condition that the reactor is isolated from air (namely under anaerobic condition), adding artificial simulated sulfur-containing wastewater into the reaction container, stirring (for example for about 2-4 h), after the reaction is finished, standing and settling for a period of time, discharging supernatant, restarting the next period, and repeating the operation, thereby improving the enrichment degree of sulfate reducing bacteria in the activated sludge. The artificial simulated sulfur-containing wastewater can be prepared by mixing seawater and water, and appropriate trace elements can be added for supplement.
In the method of the present invention, each operation cycle of the sulfur cycle coupled denitrifying phosphorus removal system during recovery may include a water intake phase, an anaerobic phase, an anoxic phase, a precipitation phase, a water discharge phase, and optionally an idle phase. For example, each cycle may last 8-13 hours, where the anaerobic phase may be 3-5 hours and the anoxic phase may be 3-6 hours. If there is an idle period, this period may be, for example, 1 h. The remaining stages may amount to 0.5-1.5 h, for example about 1 h.
The dosage of the sulfate-reducing bacteria-enriched activated sludge may be set to: so that the total sludge concentration of the system reaches 6.0-8.0 g/L (such as 6.0, 6.5, 7.0, 7.5 and 8.0 g/L). After the system recovers the phosphorus removal and sulfur circulation capacity by adding the activated sludge enriched with the sulfate reducing bacteria once, the phosphate removal rate of the system reaches more than 60% (such as more than 65%, 70%, 75%, 80%, 85%, or 90%), and the sulfur circulation amount of the system reaches 20-50 mg S/L (such as 20, 25, 30, 35, 40, 45, 50mg S/L). The sulfur cycle amount includes a sulfate reduction amount and a sulfate production amount, and in some embodiments, the sulfate reduction amount is from 20 to 50mg S/L. The dosage of the activated sludge enriched by the sulfate-reducing bacteria added at one time is preferably set as follows: so that the total sludge concentration of the system reaches 6.0-8.0 g/L (such as 6.0, 6.5, 7.0, 7.5, 8.0g/L), preferably so that the total sludge concentration reaches 7.0-7.5 g/L; simultaneously, the reduction amount of the sulfate is recovered to 20-50 mg S/L, preferably to 30-40 mg S/L.
Herein, the phosphate removal rate, phosphate release amount, phosphate absorption amount, sulfur circulation amount, sulfate reduction amount, and sulfate production amount are defined as follows:
1) removal rate of phosphate
Phosphate removal (%) - (P) 0 -P 2 )/P 0 ；
Wherein P is 0 : phosphate concentration (mgP/L) at the start of anaerobic phase; p 2 : phosphate concentration (mgP/L) at the end of the anoxic phase.
2) Amount of phosphate released
Phosphate Release amount (mgP/L) ═ P 1 -P 0 ；
Wherein P is 0 : phosphate concentration (mgP/L) at the start of anaerobic phase; p 1 : phosphate concentration (mgP/L) at the end of the anaerobic phase or at the beginning of the anoxic phase.
3) Absorption of phosphate
Phosphate absorption (mgP/L) ═ P 2 -P 1 ；
Wherein P is 1 : phosphate concentration (mgP/L) at the end of the anaerobic phase or at the start of the anoxic phase; p 2 : phosphate concentration (mgP/L) at the end of the anoxic phase.
4) Amount of sulfur circulating
Sulfur circulation amount (mgS/L) ═ S 1 +S 2 )/2；
Wherein S 1 : sulfate reduction (mgS/L); s 2 : amount of sulfate produced (mgS/L).
5) Reduction amount of sulfate
Reduction of sulfate (mgS/L) ═ S 1b -S 1a )/2；
Wherein S 1a : the concentration of sulfate at the start of the anaerobic phase (mgS/L); s 1b : the concentration of sulfate at the end of the anaerobic phase (mgS/L).
6) Amount of sulfate produced
Amount of sulfate produced (mgS/L) ═ S 2b -S 1b )/2；
Wherein S 1b : the concentration of sulfate at the end of the anaerobic phase (mgS/L); s. the 2b : concentration of sulfate at the end of the anoxic stage (mgS/L).
The invention provides a method for recovering the capacity of a sulfur cycle coupled denitrifying phosphorus removal system after breakdown, wherein the phosphorus removal and sulfur cycle capacity of the sulfur cycle coupled denitrifying phosphorus removal system can be recovered to at least 80% within at most 20d, even within 15 d. In contrast, with the conventional method of re-acclimating the cultured activated sludge, at least 50 days are required to recover the system from collapse. Therefore, the method can quickly recover the collapsed sulfur cycle coupling denitrification dephosphorization system in a short time, has low investment and simple and convenient operation, and has practical value. Meanwhile, the method of the present invention may be applicable to unfavorable water quality conditions of high temperature, high salinity, and high sulfate, for example, the total salinity of the treated wastewater may be in the range of 0.35-0.7%, the sulfate concentration thereof may be in the range of 150-200 mgS/L, and/or the temperature of the wastewater may be in the range of 25-35 ℃. Therefore, the invention also has reference significance for sewage treatment under the extreme water quality condition by an activated sludge process.
As used herein, the term "and/or" one or more "refers to one or all of the listed elements, or a combination of any two or more of the listed elements. "optional" means that the element may or may not be present, as the case may be. "sequentially" means in the order listed, but not necessarily in close proximity. Unless otherwise indicated, all numbers expressing feature sizes, quantities, and physical characteristics used herein are to be understood as being modified in all instances by the term "about. Accordingly, unless indicated to the contrary, the numerical parameters set forth herein are approximations that can vary depending upon the desired properties sought to be obtained by those skilled in the art utilizing the teachings disclosed herein. As used herein, a numerical range by endpoints includes all numbers within that range and any sub-range within that range (e.g., 60% or more includes 60%, 65%, 70%, 80%, 90%, 72-85%, etc.).
Example 1
In this example, an operation test was conducted using a sequencing batch reactor as shown in FIG. 1. The effective working volume of the reactor is 5L, and the reactor is made of PVC materials.
Preparing artificial synthetic simulated sulfur-containing wastewater: is prepared from 20% seawater and 80% water by mixing, and contains 60mg NH 4 + -N/L，20mg PO 4 3- P/L, 400mg COD/L, 150-200 mgS/L sulfate (value 165mgS/L), and adding the following trace elements as supplements, FeCl 3 ·6H 2 O(1.5mg/L)、CuSO 4 ·5H 2 O(0.03mg/L)、KI(0.18mg/L)、MnCl 2 ·4H 2 O(0.12mg/L)、NaMoO 4 ·2H 2 O(0.06mg/L)、ZnSO 4 ·7H 2 O(0.12mg/L)、CoCl 2 ·6H 2 O (0.15mg/L), EDTA (10 mg/L); the carbon source is mixed by sodium acetate and sodium propionate, and the simulated sulfur-containing wastewater contains 267mg of acetic acid-COD/L and 133mg of propionic acid-COD/L; the salinity of the simulated sulfur-containing wastewater is 0.7 percent.
The reactor is operated in an alternating anaerobic and anoxic mode. Each cycle runs for 8-13h and comprises the following steps: 2.5L of simulated wastewater is fed in 2 min; 3-5 h anaerobic stage; 3-6 h in an anoxic stage, wherein 2g N/L sodium nitrate solution is added into the reactor in the first 2-2.5 min to ensure that the concentration of nitrate in the reactor reaches 45-50 mg N/L; precipitating for 55 min; draining 2.5L supernatant for 3 min; 1h of idle period.
During the operation of the reactor, the temperature was controlled to 30. + -. 1 ℃ by heating in a water bath and the pH was controlled to 7.2-7.8 by adding 0.5N HCl or 0.5N NaOH. In the experimental operation process, the operation effect of the reactor is monitored by sampling periodically.
The reactor is operated for 50 days in total, and the phosphorus removal and sulfur circulation capacities of the sulfur circulation coupling denitrification phosphorus removal system have collapse phenomena due to mud loss and the like, for example, the phosphate removal rate of the system is reduced to be below 20%, the sulfur circulation amount is reduced to be below 5mg S/L, and the sludge concentration is reduced to be 4.6 g/L. In the operation period beginning at the 5d, activated sludge with the enrichment degree of sulfate reducing bacteria of about 45 percent is added into the reactor at one time in the water inlet stage, so that the sludge concentration in the reactor reaches 7.0 g/L. In subsequent operations, the reactor was operated as usual, with the results described below.
The preparation process of the activated sludge with the enrichment degree of the sulfate reducing bacteria of about 45 percent is as follows: inoculating activated sludge in an anaerobic fermentation tank of a sewage plant of the sand field of hong Kong by using another sequencing batch reactor (as shown in FIG. 1); and (3) adding the artificial simulated sulfur-containing wastewater into a reaction container under the condition of air isolation (namely under the anaerobic condition), stirring for 3 hours, after the reaction is finished, standing and settling for a period of time, discharging supernatant, restarting the next period, and repeating the operation until the enrichment degree of sulfate reducing bacteria in the activated sludge reaches about 45%. The activated sludge has high activity, and the organic load rate reaches 1.4kg COD/m 3 And/d, and has higher sludge concentration (above 8.6 g/L), and the corresponding hydraulic retention time of the reactor is about 7 h.
FIG. 2 shows the removal rate of phosphate, the amount of phosphate released and the amount of sulfate reduced in the anaerobic stage, the amount of phosphate absorbed and the amount of sulfate produced in the anoxic stage.
1-5 d, due to the loss of the sludge in the reactor and other reasons, the operation condition of the sulfur circulation coupling denitrification dephosphorization system is seriously deteriorated, which is also a problem that the actual operation process of the sewage plant may face. During the deterioration time of the system, the removal rate of phosphate is reduced to below 10%, and the circulating amount of sulfur is reduced to 0-5 mg S/L. The change of these parameters indicates that the system has basically crashed and needs to find the method to deal with.
In the operation period beginning at the 5d, according to the method of the present invention, the deteriorated system is recovered by once adding activated sludge having an enrichment degree of about 45% of sulfate-reducing bacteria to the reactor at the water inlet stage so that the sludge concentration in the reactor reaches 7.0 g/L. As a result, the circulating sulfur amount was rapidly recovered to 20-30 mg S/L within 20d, and the phosphate removal rate was rapidly recovered to 60% or more. In the subsequent operation, the removal rate of phosphate is continuously improved and stabilized to be more than 80%, and the sulfur circulation amount is kept stable. Therefore, the deteriorated sulfur circulation coupling denitrification dephosphorization system can be quickly recovered by adding the activated sludge enriched by the sulfate reducing bacteria into the reactor at one time.
Example 2
In this example, the operational test was still carried out using a sequencing batch reactor as shown in FIG. 1. The formulation of example 1 was still used to artificially synthesize a simulated sulfur-containing wastewater. The reactor operating conditions were identical to example 1.
The reactor still runs for 50d totally, and in the running period from the 5d, activated sludge with the enrichment degree of sulfate reducing bacteria of about 56 percent is added into the reactor at one time in the water inlet stage, so that the sludge concentration in the reactor reaches 7.5 g/L. In the subsequent operation, the reactor was operated as usual, and the operation results were as follows.
The preparation process of the activated sludge with the enrichment degree of the sulfate reducing bacteria of about 56 percent is as follows: using another sequencing batch reactor (as shown in FIG. 1, taking activated sludge from anaerobic fermentation tank of Hongkong Shatian sewage plant)Inoculating; and (3) adding the artificial simulated sulfur-containing wastewater into a reaction container under the condition of air isolation (namely under the anaerobic condition), stirring for 2 hours, after the reaction is finished, standing and settling for a period of time, discharging supernatant, restarting the next period, and repeating the operation until the enrichment degree of sulfate reducing bacteria in the activated sludge reaches about 56%. The activated sludge has high activity, and the organic load rate reaches 1.6kg COD/m 3 And/d, and has higher sludge concentration (above 9.5 g/L), and the corresponding hydraulic retention time of the reactor is about 6 h.
FIG. 3 shows the removal rate of phosphate, the released amount of phosphate and the reduced amount of sulfate in the anaerobic stage, the absorbed amount of phosphate and the generated amount of sulfate in the anoxic stage.
1-5 d, the running condition of the sulfur circulation coupling denitrification dephosphorization system is seriously deteriorated due to the loss of the sludge amount in the reactor and the like. During the deterioration time of the system, the removal rate of phosphate is reduced to below 10%, and the circulating amount of sulfur is reduced to 0-5 mg S/L. The change of these parameters indicates that the system has basically crashed, and the search method is urgently needed to deal with.
In the operation period starting at the 5d, according to the method of the present invention, the deteriorated system is recovered by once feeding activated sludge having an enrichment degree of sulfate-reducing bacteria of about 56% into the reactor so that the sludge concentration in the reactor reaches 7.5 g/L. As a result, the circulating sulfur amount was rapidly recovered to 25 to 50mg S/L within 12d, and the phosphate removal rate was rapidly recovered to 80% or more. In the subsequent operation, the removal rate of phosphate is continuously improved and stabilized to be more than 90%, and the sulfur circulation amount is kept stable. Therefore, by increasing the enrichment degree of the sulfate reducing bacteria and the sludge concentration in the reactor, the deteriorated sulfur circulation coupling denitrification dephosphorization system can be quickly recovered, and the operation effect is better.
Compared with other reported methods for recovering the sulfur cycle coupled denitrifying phosphorus removal degradation system (such as a method for adding sulfide at the initial stage of an anoxic stage of each operation period), the method can not only rapidly recover the degraded sulfur cycle coupled denitrifying phosphorus removal system within at most 20 days (the removal rate of phosphate can be recovered to be more than 80% within at most 20 days, and the sulfur cycle amount is increased to be 20-50 mg S/L), but also recover main functional populations in the system, such as sulfate reducing bacteria and sulfur oxidizing bacteria, so that a microbial ecosystem in the system can be reconstructed, and the operation is more sustainable. In addition, the method only needs to add the activated sludge enriched by the sulfate reducing bacteria once, does not need repeated operation, is simpler and more convenient to operate, has practical value, and is beneficial to popularization and use.
It will be understood that the above embodiments are merely exemplary embodiments taken to illustrate the principles of the present invention, which is not limited thereto. The various aspects, features of the invention may be combined with each other. It will be apparent to those skilled in the art that various changes and modifications can be made therein without departing from the spirit and scope of the invention, and these changes and modifications are also within the scope of the invention.
Claims (15)
1. A method for restoring the capacity of a sulfur cycle coupled denitrification phosphorus removal system after breakdown, wherein the sulfur cycle coupled denitrification phosphorus removal system removes phosphorus from sulfur-containing wastewater using sludge containing wastewater treatment microorganisms, and each operating cycle of the system comprises: a water inlet stage, an anaerobic stage, an anoxic stage, a precipitation stage, a water discharge stage and an optional idle stage, wherein when the phosphorus and sulfur removal cycle capability of the sulfur cycle coupled denitrifying phosphorus removal system collapses, activated sludge enriched with sulfate reducing bacteria is added to the system in one step in the water inlet stage or the anaerobic stage so that the system recovers the phosphorus and sulfur removal cycle capability, wherein the collapse of the phosphorus and sulfur removal cycle capability of the sulfur cycle coupled denitrifying phosphorus removal system means that the phosphate removal rate of the system is below 20% and the sulfur cycle amount is below 5mg S/L, and wherein when the collapse of the phosphorus and sulfur removal cycle capability of the sulfur cycle coupled denitrifying phosphorus removal system, the sludge concentration in the system falls below 4.6g/L, and the sludge concentration in the system falls below the phosphorus and sulfur removal cycle capability of the sulfur cycle coupled denitrifying phosphorus removal system
Wherein the sulfate-reducing bacteria enriched activated sludge has the following characteristics:
a) the enrichment degree of the sulfate reducing bacteria is as follows: the proportion of the number of the sulfate reducing bacteria to the total number of all bacteria in the activated sludge is more than 45 percent;
b) the organic loading rate was 1.4kg COD/m 3 D is more than;
c) the sludge concentration is more than 8.6 g/L; and
d) the corresponding hydraulic residence time of the reactor is 7 to 8 hours.
2. The method of claim 1, wherein each of the operational periods lasts 8-13 hours.
3. The method according to claim 1, wherein the sulfate-reducing bacteria-enriched activated sludge is added to the system at one time so that the total sludge concentration of the system reaches 6.0-8.0 g/L.
4. The method according to claim 1, wherein after the system recovers the phosphorus removal and sulfur circulation capacity by adding the activated sludge enriched with the sulfate reducing bacteria at one time, the phosphate removal rate of the system reaches more than 60%, more than 70%, or more than 80%, and the sulfur circulation amount reaches 20-50 mg S/L.
5. The method of claim 4, wherein the sulfur cycle amount comprises a sulfate reduction amount and a sulfate production amount, wherein the sulfate reduction amount is 20-50 mg S/L.
6. A method according to claim 1, wherein the wastewater treatment microorganisms comprise a combination of sulfate-reducing bacteria and sulfur-oxidizing bacteria, and the pH of the system is controlled in the range of 7.2-8.4 when in operation.
7. The method of claim 6, wherein the sulfate-reducing bacteria are selected from the group consisting of Desulfobacter (Desulfobacter), Desulfobulbus (Desulfobulbus), Desulfomonas (Desulfuromonas), and the sulfur-oxidizing bacteria are selected from the group consisting of Sedixicola (Sedimenticola), Thialomonas (Thiohalomonas), Thiotrichaceae (Thiotrichaceae).
8. The method of claim 2, wherein the anaerobic phase is 3-5 hours, the anoxic phase is 3-6 hours, and the influent, sediment, and effluent phases are 0.5-1.5 hours in total.
9. The method of claim 1, wherein the wastewater has any one or more characteristics selected from the group consisting of:
a) the total salinity of the wastewater is in the range of 0.35-0.7%;
b) the sulfate concentration of the wastewater is in the range of 150-200 mg-S/L;
c) the temperature of the waste water is in the range of 25-35 ℃.
10. The method of any one of claims 1-9, wherein the phosphate removal rate of the sulfur cycle coupled denitrification phosphorus removal system is restored to at least 80% in up to 20 days, while the amount of the sulfur cycle reaches 20-50 mg S/L.
11. The method according to claim 1, wherein the proportion of the number of sulfate-reducing bacteria to the total number of all bacteria in the activated sludge is 50% or more.
12. The method according to claim 1, wherein the proportion of the number of sulfate-reducing bacteria to the total number of all bacteria in the activated sludge is 60% or more.
13. The method according to claim 1, wherein the organic loading rate is 1.6kg COD/m 3 And/d or more.
14. The method according to claim 1, wherein the sludge concentration is 10g/L or more.
15. A method according to claim 1, wherein the wastewater treatment microorganisms comprise a combination of sulfate-reducing bacteria and sulfur-oxidizing bacteria, and the pH of the system is controlled in the range of 7.2-7.8 when in operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610499405.3A CN107540095B (en) | 2016-06-29 | 2016-06-29 | Method for rapidly recovering sulfur cycle coupling denitrification dephosphorization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610499405.3A CN107540095B (en) | 2016-06-29 | 2016-06-29 | Method for rapidly recovering sulfur cycle coupling denitrification dephosphorization system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107540095A CN107540095A (en) | 2018-01-05 |
| CN107540095B true CN107540095B (en) | 2022-09-13 |
Family
ID=60965605
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610499405.3A Active CN107540095B (en) | 2016-06-29 | 2016-06-29 | Method for rapidly recovering sulfur cycle coupling denitrification dephosphorization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107540095B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107673466A (en) * | 2017-09-29 | 2018-02-09 | 广州市香港科大霍英东研究院 | A kind of method of quick domestication sulfur cycle coupling denitrification dephosphorization system |
| CN112299497A (en) * | 2019-07-26 | 2021-02-02 | 黄耀辉 | Method for treating biological wastewater |
-
2016
- 2016-06-29 CN CN201610499405.3A patent/CN107540095B/en active Active
Non-Patent Citations (1)
| Title |
|---|
| Simultaneous nitrogen and phosphorus removal in;Di Wu 等;《WATER RESEARCH》;20140228(第49期);第251页摘要，第252页第1栏最后1段至第2栏最后1段，第261页第1栏第1段至第2页最后1段 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107540095A (en) | 2018-01-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102557356B (en) | Process and method for denitrification and phosphorus removal of municipal sewage by half shortcut nitrification and anaerobic ammonium oxidation | |
| CN108946944A (en) | The method that short-cut denitrification promotes the removal of waste water total nitrogen | |
| WO2014146439A1 (en) | Biochemical method for treating synthetic leather wastewater comprising dimethylformamide | |
| CN104129853B (en) | A kind of starting method of quick short distance nitration | |
| CN104310580B (en) | Part denitrification series connection autotrophic denitrification realizes the apparatus and method of nitrate wastewater and city sewage deep denitrogenation | |
| CN113415910A (en) | Device and method for denitrification coupling anaerobic ammonium oxidation biological nitrogen and phosphorus removal in iron ammonium oxidation enhanced AAO process | |
| CN204417293U (en) | A kind of denitrification dephosphorization apparatus | |
| CN105110572A (en) | Device and method for treating municipal wastewater with low C/N ratio through silicon source adsorption/nitrification/partial denitrification/anaerobic ammonia oxidation coupling process | |
| CN105016470A (en) | Method for realizing advanced nitrogen and phosphorus removal of low C/N and C/P municipal sewage through excess sludge anaerobic fermentation mixture | |
| CN111410310A (en) | Method for realizing efficient denitrification by utilizing synchronous shortcut nitrification-denitrification-anaerobic ammonia oxidation coupling drive | |
| CN110723812B (en) | Method for improving pH impact resistance of anaerobic ammonium oxidation particles | |
| CN107473370B (en) | Sewage treatment system and method combining membrane bioreactor and phosphorus recovery process | |
| CN113233592A (en) | Treatment device and method for realizing synchronous deep denitrification and carbon removal of advanced landfill leachate and domestic sewage | |
| CN101186387A (en) | Method for increasing organism synchronous dephosphorization denitrogenation effect of sewage under anaerobic-hypoxia condition | |
| CN107540095B (en) | Method for rapidly recovering sulfur cycle coupling denitrification dephosphorization system | |
| KR20150093810A (en) | Biological wastewater treatment processes that enhances the capacity for polyhydroxyalkanoate accumulation in a mixed culture biomass | |
| Deng et al. | Low-carbon nitrogen removal from power plants circulating cooling water and municipal wastewater by partial denitrification-anammox | |
| CN113003718B (en) | Starting method and application of short-range denitrification system | |
| JP5869208B2 (en) | Waste water treatment method and waste water treatment apparatus | |
| CN107253761B (en) | Anaerobic ammonia oxidation rapid enhanced starting method based on inactivated sludge | |
| CN113023871A (en) | Device and method for synchronously treating domestic sewage and late-stage landfill leachate by virtue of shortcut nitrification-anaerobic ammonia oxidation coupling denitrification process | |
| CN104829044A (en) | Method used for realizing whole-course autotrophic nitrogen removing via anaerobic ammonium oxidation immobilization | |
| CN110255812B (en) | Biochemical and advanced oxidation combined method for retaining ammonia nitrogen and removing antibiotics in livestock and poultry breeding sewage treatment process | |
| Frison et al. | Enhanced retention of deammonification microorganisms for the treatment of psycrophilic anaerobic digestate | |
| Li et al. | Mainstream wastewater treatment by polyaluminium ferric chloride (PAFC) flocculation and nitritation-denitritation membrane aerated biofilm reactor (MABR) |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |