CN111422976A - Process for treating high ammonia nitrogen wastewater by using moving bed biofilm reactor - Google Patents
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Abstract
A process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor comprises the following steps: 1) a film formation preparation stage: 1-1) preparing a nutrient solution with the same components as the high ammonia nitrogen wastewater to be treated; 1-2) using MBBR suspended filler K1 and polyethylene glycol particle balls as fillers; 1-3) adding nutrient solution and microbial inoculum to form bacterial solution; 2) and (3) viable bacteria adsorption stage: operating the wastewater treatment system, controlling the flow and the concentration of dissolved oxygen, and forming a biological membrane; 3) and (3) viable bacteria enrichment stage: continuously adding nutrient solution into the moving bed biofilm reactor to complete the enrichment of live bacteria in the bacterial solution; 4) and (3) film formation finishing stage: stopping adding the nutrient solution when protozoa are observed on the surface of the biological membrane; 5) optimizing process parameters: 5-1) obtaining the optimal range of the ammonia nitrogen concentration of the bacterial liquid; 5-2) obtaining the optimal range of the carbon-nitrogen ratio of the bacterial liquid; 5-3) obtaining the optimal range of the hydraulic retention time of the bacterial liquid; 6) and (3) a high ammonia nitrogen wastewater treatment stage: and (4) discharging bacteria liquid, and introducing high ammonia nitrogen wastewater to be treated for treatment.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor.
Background
The high ammonia nitrogen wastewater mainly comes from garbage percolate, coking wastewater, coal gas wastewater, printing and dyeing wastewater, sludge digestion liquid and breeding wastewater, and the high ammonia nitrogen wastewater with wide sources directly enters a water body, so that water eutrophication can be caused, biotoxicity is generated, fish and shrimp die, and drinking water safety is harmed.
The existing high ammonia nitrogen wastewater treatment method comprises the following steps: chemical precipitation, breakpoint chlorination, stripping, adsorption, ion exchange, and biological methods. The chemical precipitation method needs to add a chemical reagent to react with ammonia nitrogen in the water body, so that secondary pollution can be caused; the breakpoint chlorination method has high ammonia nitrogen removal rate, but the cost for the subsequent disinfection process is high; the blowing-off method has higher energy consumption; the ion exchange process is inefficient and requires a large amount of ion exchange resin.
In the biological method, an activated sludge process is generally adopted to carry out Biofilm formation on suspended fillers by utilizing a Moving-Bed Biofilm Reactor (MBBR) for wastewater treatment, although the microorganisms can adsorb and degrade pollutants in wastewater, the microorganisms in the Moving-Bed Biofilm Reactor of a wastewater treatment system grow slowly, the starting time is long, and under high ammonia-nitrogen concentration, the tolerance of the microorganisms is poor, the pollutant removal rate is low, the treatment effect on the high ammonia-nitrogen wastewater is not good, and how to make the wastewater treatment system utilizing the Moving-Bed Biofilm Reactor to carry out safe and efficient treatment on the high ammonia-nitrogen wastewater is a problem to be solved.
Disclosure of Invention
The invention aims to provide a process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor, which utilizes a heterotrophic nitrification-aerobic denitrification composite microbial agent to strengthen the moving bed biofilm reactor, effectively shortens the starting period of equipment, creates conditions for the enrichment of heterotrophic nitrification-aerobic denitrification composite bacteria, fully exerts various excellent performances of the heterotrophic nitrification-aerobic denitrification composite bacteria, combines the moving bed biofilm reactor technology, an adsorption fixed microorganism technology and the heterotrophic nitrification-aerobic denitrification technology, stably and efficiently removes main pollutants in the high ammonia nitrogen wastewater by an aerobic denitrification mode, occupies a small area and greatly reduces the economic cost.
The purpose of the invention is realized by adopting the following scheme: a process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor comprises the following steps:
1) a film formation preparation stage:
1-1) preparing a nutrient solution with the same components as the high ammonia nitrogen wastewater to be treated;
1-2) adding an MBBR suspended filler K1 and polyethylene glycol pellets as fillers into a moving bed biofilm reactor of a wastewater treatment system, wherein the filling rate of the fillers in the moving bed biofilm reactor is 15-67%;
1-3) adding the nutrient solution prepared in the step 1-1) into a moving bed biofilm reactor of a wastewater treatment system to serve as a culture medium, and adding a heterotrophic nitrification-aerobic denitrification composite microbial inoculum with the inoculum size of 5-10% according to the volume of the nutrient solution to form a bacterial solution;
2) and (3) viable bacteria adsorption stage:
operating a wastewater treatment system, controlling the flow of bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 24-72 h, and maintaining the dissolved oxygen concentration in the bacterial liquid within the range of 2-4 mg/L through an aeration device and a flowmeter of the wastewater treatment system, so that the viable bacteria of the heterotrophic nitrification-aerobic denitrification composite microbial inoculum are adsorbed on the surface of the filler, and a light yellow biofilm is quickly formed;
3) and (3) viable bacteria enrichment stage:
OD for detecting bacteria liquid in moving bed biofilm reactor600Numerical value of (1) and NH4 +Concentration of-N, COD, TN, if OD600Is less than 1, and NH4 +Respectively controlling the concentration of-N, COD and TN to be lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, and continuously adding nutrient solution into the moving bed biofilm reactor to make the OD of the bacterial solution600The value of (2) reaches 1-1.5, and the content of viable bacteria in the bacterial liquid reaches 180-200 hundred million/g, so that the enrichment of the viable bacteria in the bacterial liquid is completed;
4) and (3) film formation finishing stage:
after finishing the enrichment of live bacteria in the bacteria liquid, detecting NH of the bacteria liquid in the moving bed biofilm reactor4 +Concentration of N, COD, TN, once NH4 +Respectively controlling the concentration of-N, COD and TN to be lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, continuously adding nutrient solution into the moving bed biofilm reactor until a layer of tawny biofilm is formed on the filler in the moving bed biofilm reactor, observing protozoa on the surface of the biofilm through a microscope, and detecting the OD of the bacterial solution in the moving bed biofilm reactor600Numerical value of (1) and NH4 +Concentration of-N, COD, TN, OD of the bacterial liquid600Is less than 0.2, NH4 +The concentrations of-N, COD and TN are respectively lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, namely the biofilm formation in the moving bed biofilm reactor is finished, and the nutrient solution is stopped to be added;
5) optimizing process parameters:
5-1) determining the optimal range of the ammonia nitrogen concentration of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor to be within 72h, adding a carbon source and a nitrogen source to enable the carbon-nitrogen ratio of the bacterial liquid to be 8, changing the ammonia nitrogen concentration of the bacterial liquid within the range of 400-1000 mg/L, and when NH (NH) of the bacterial liquid4 +When the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 73%, the ammonia nitrogen concentration is 500-700 mg/L, and the optimal range of the ammonia nitrogen concentration of the bacterial liquid is obtained;
5-2) determining the optimal range of the carbon-nitrogen ratio of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 72h, adding a carbon source and a nitrogen source to ensure that the carbon-nitrogen ratio of the bacterial liquid is changed within the range of 1-15 when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, and when NH of the bacterial liquid4 +The carbon-nitrogen ratio is 8-10 when the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 82%, and the optimal range of the carbon-nitrogen ratio of the bacterial liquid is obtained;
5-3) confirming the optimal range of the hydraulic retention time of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the carbon-nitrogen ratio of the bacterial liquid to be 8-10 by adding a carbon source and a nitrogen source, controlling the flow of the bacterial liquid when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, changing the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 6-72 h, and when NH of the bacterial liquid4 +The hydraulic retention time is 24-36 h when the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 85%, and the optimal range of the hydraulic retention time of the bacterial liquid is obtained;
6) and (3) a high ammonia nitrogen wastewater treatment stage: and (4) discharging bacteria liquid in the moving bed biofilm reactor, introducing the high ammonia nitrogen wastewater to be treated, and controlling the running wastewater treatment system to treat the high ammonia nitrogen wastewater to be treated by adopting the optimized optimal process parameters.
The nutrient solution in the step 1-1) comprises 2.9-3.2 g/L of anhydrous sodium acetate, 2.1-2.3 g/L of ammonium sulfate, 0.6-0.8 g/L of dipotassium hydrogen phosphate, 1.9-2.1 g/L of magnesium sulfate heptahydrate, 0.1-0.2 g/L of magnesium sulfate monohydrate, 1.4-1.6 g/L of calcium chloride and 0.1-0.2 g/L of ferrous sulfate heptahydrate.
The preparation steps of the nutrient solution are as follows:
a) preparing solution of trace elements
The trace element solution comprises 1.9-2.0 g/L of mixed magnesium sulfate heptahydrate, 0.1-0.2 g/L of magnesium sulfate monohydrate, 1.4-1.5 g/L of calcium chloride and 0.1-0.2 g/L of ferrous sulfate heptahydrate;
b) preparing simulated high ammonia nitrogen wastewater
Calculating the adding amount of a carbon source, a nitrogen source and a phosphorus source by using the effective volume of the moving bed biofilm reactor, wherein the adding proportion is that anhydrous sodium acetate is 4.73 g/L, ammonium sulfate is 2.03 g/L, and dipotassium phosphate is 0.14 g/L, and the obtained NH simulating the high ammonia nitrogen wastewater4 +The concentrations of N, COD and TN are 480-520 mg/L, 40000-40100 mg/L and 520-540 mg/L respectively;
c) preparing nutrient solution
The prepared simulated high ammonia nitrogen wastewater is mixed with trace element solution = 1L: 5m L.
The heterotrophic nitrification-aerobic denitrification composite microbial inoculum comprises cuppridinium bulimia SWA1, alcaligenes faecalis, acinetobacter and ochrobactrum TAC-2.
The content ratio of the cuppridinium bulimia SWA1, the alcaligenes faecalis, the acinetobacter and the ochrobactrum anthropi TAC-2 in the heterotrophic nitrification-aerobic denitrification composite microbial agent is 10-20%: 5-20%: 10-30%: 20 to 50 percent.
The temperature of the bacteria liquid in the moving bed biofilm reactor is kept within the range of 30 +/-2 ℃ through a temperature control system in the wastewater treatment system.
The invention has the following beneficial effects:
1. high ammonia nitrogen resistance: the patent CN109082387A provides a heterotrophic nitrification-aerobic denitrification composite microbial inoculum capable of removing high ammonia nitrogen at low temperature and application thereof, the heterotrophic nitrification-aerobic denitrification composite microbial inoculum is derived from high ammonia nitrogen wastewater, has the capability of removing waste organic matters, ammonia nitrogen and nitrate nitrogen, and has strong adaptability to the diversity of high ammonia nitrogen wastewater pollutants.
2. The selected filler has the advantages that: the polyethylene glycol can be used for thickening a liquid containing suspended particulate matters, so when the polyethylene glycol particle balls are used as the filler, not only can microorganisms adsorbed on the surfaces of the ball-shaped filler be uniformly contacted with wastewater due to the fact that the balls have larger surface areas, the wastewater treatment efficiency is higher, but also a better space is provided for the growth and the propagation of heterotrophic nitrification-aerobic denitrification composite bacteria due to the thickening of the bacterial liquid, the adsorption of the heterotrophic nitrification-aerobic denitrification composite bacteria is facilitated, the heterotrophic nitrification-aerobic denitrification composite bacteria are easier to fix on the filler, the retention time of the heterotrophic nitrification-aerobic denitrification composite bacteria in the moving bed biofilm reactor is prolonged, and the problems that part of microorganisms are slow in growth and easy to run off are effectively solved.
3. Optimizing process parameters: effectively improving the effect of the biomembrane in the moving bed biomembrane reactor on removing pollutants and realizing safe and efficient removal of COD and ammonia nitrogen.
4. The starting running time is short: the method is started by adopting a microbial inoculum sequencing batch biofilm formation mode, and the adopted denitrifying bacteria are heterotrophic bacteria and have a high growth rate, so that the starting time of the process is only 12-15 days, which is obviously lower than that of the traditional biological membrane process of activated sludge biofilm formation.
5. The operation management is convenient: the biomembrane method of the invention is different from the activated sludge method, can not produce a large amount of excess sludge, does not need the sludge to flow back, can not produce the problems such as the sludge bulking, etc., and on the basis of the aerobic denitrification technology, can realize the simultaneous removal of COD, ammonia nitrogen and nitrate nitrogen under a single condition in a structure, the process flow is more succinct compared with the traditional denitrification process, the operation management is more convenient.
6. The occupied area is small, and the cost is low: the selected filler fully utilizes the inner space of the reactor, and can realize the removal of pollutants in a single reactor, thereby effectively reducing the operation cost.
7. The application range is wide: the invention can be applied to the treatment of various high ammonia nitrogen wastewater, different types of fillers and operation parameters are selected according to different types of high ammonia nitrogen wastewater, the application is more flexible, the application range is wider, the requirement on the temperature is not strict, and the temperature can be regulated at normal temperature.
Drawings
FIG. 1 is a flow chart of the present invention;
FIG. 2 is a schematic diagram showing the change of the removal rate of each water quality index at the process parameter optimization stage in the example;
FIG. 3 is a schematic view showing the construction of a wastewater treatment system used in the present invention.
In fig. 3, 1 is a moving bed biofilm reactor, 2 is an aeration device, 3 is a water inlet tank, 4 is a water outlet tank, 5 is a temperature control system, 6 is a thermometer, and 7 is a filler.
Detailed Description
As shown in fig. 1 to 3, a process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor comprises the following steps:
1) a film formation preparation stage:
1-1) preparing a nutrient solution with the same components as the high ammonia nitrogen wastewater to be treated;
the nutrient solution in the step 1-1) comprises 2.9-3.2 g/L of anhydrous sodium acetate, 2.1-2.3 g/L of ammonium sulfate, 0.6-0.8 g/L of dipotassium hydrogen phosphate, 1.9-2.1 g/L of magnesium sulfate heptahydrate, 0.1-0.2 g/L of magnesium sulfate monohydrate, 1.4-1.6 g/L of calcium chloride and 0.1-0.2 g/L of ferrous sulfate heptahydrate.
The preparation steps of the nutrient solution are as follows:
a) preparing solution of trace elements
The trace element solution comprises 1.9-2.0 g/L of mixed magnesium sulfate heptahydrate, 0.1-0.2 g/L of magnesium sulfate monohydrate, 1.4-1.5 g/L of calcium chloride and 0.1-0.2 g/L of ferrous sulfate heptahydrate;
b) preparing simulated high ammonia nitrogen wastewater
Calculating carbon source by using effective volume of moving bed biofilm reactorThe adding amount of the nitrogen source and the phosphorus source is that anhydrous sodium acetate is 4.73 g/L, ammonium sulfate is 2.03 g/L, dipotassium hydrogen phosphate is 0.14 g/L, and the obtained NH simulating the high ammonia nitrogen wastewater4 +The concentrations of N, COD and TN are 480-520 mg/L, 40000-40100 mg/L and 520-540 mg/L respectively;
c) preparing nutrient solution
The prepared simulated high ammonia nitrogen wastewater is mixed with trace element solution = 1L: 5m L.
1-2) adding an MBBR suspended filler K1 and polyethylene glycol pellets as fillers into a moving bed biofilm reactor of a wastewater treatment system, wherein the filling rate of the fillers in the moving bed biofilm reactor is 15-67%;
1-3) adding the nutrient solution prepared in the step 1-1) into a moving bed biofilm reactor of a wastewater treatment system to serve as a culture medium, and adding a heterotrophic nitrification-aerobic denitrification composite microbial inoculum with the inoculum size of 5-10% according to the volume of the nutrient solution to form a bacterial solution; the heterotrophic nitrification-aerobic denitrification composite microbial inoculum comprises cuppridinium bulimia SWA1, alcaligenes faecalis, acinetobacter and ochrobactrum TAC-2. The content ratio of the cuppridinium bulimia SWA1, the alcaligenes faecalis, the acinetobacter and the ochrobactrum anthropi TAC-2 in the heterotrophic nitrification-aerobic denitrification composite microbial agent is 10-20%: 5-20%: 10-30%: 20 to 50 percent.
2) And (3) viable bacteria adsorption stage:
the temperature of the bacterial liquid in the moving bed biofilm reactor is kept within the range of 30 +/-2 ℃ through a temperature control system in the wastewater treatment system, the wastewater treatment system is operated, the flow of the bacterial liquid is controlled, the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor is controlled within the range of 24-72 h, the dissolved oxygen concentration in the bacterial liquid is maintained within the range of 2-4 mg/L through an aeration device and a flowmeter of the wastewater treatment system, and the viable bacteria of the heterotrophic nitrification-aerobic denitrification composite microbial inoculum are adsorbed on the surface of a filler to quickly form a light yellow biofilm;
3) and (3) viable bacteria enrichment stage:
OD for detecting bacteria liquid in moving bed biofilm reactor600Numerical value of (1) and NH4 +-N、COD、TNConcentration of (1), if OD600Is less than 1, and NH4 +Respectively controlling the concentration of-N, COD and TN to be lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, and continuously adding nutrient solution into the moving bed biofilm reactor to make the OD of the bacterial solution600The value of (2) reaches 1-1.5, and the content of viable bacteria in the bacterial liquid reaches 180-200 hundred million/g, so that the enrichment of the viable bacteria in the bacterial liquid is completed;
4) and (3) film formation finishing stage:
after finishing the enrichment of live bacteria in the bacteria liquid, detecting NH of the bacteria liquid in the moving bed biofilm reactor4 +Concentration of N, COD, TN, once NH4 +Respectively controlling the concentration of-N, COD and TN to be lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, continuously adding nutrient solution into the moving bed biofilm reactor until a layer of tawny biofilm is formed on the filler in the moving bed biofilm reactor, observing protozoa on the surface of the biofilm through a microscope, and detecting the OD of the bacterial solution in the moving bed biofilm reactor600Numerical value of (1) and NH4 +Concentration of-N, COD, TN, OD of the bacterial liquid600Is less than 0.2, NH4 +The concentrations of-N, COD and TN are respectively lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, namely the biofilm formation in the moving bed biofilm reactor is finished, and the nutrient solution is stopped to be added;
5) optimizing process parameters:
5-1) determining the optimal range of the ammonia nitrogen concentration of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor to be within 72h, adding a carbon source and a nitrogen source to enable the carbon-nitrogen ratio of the bacterial liquid to be 8, changing the ammonia nitrogen concentration of the bacterial liquid within the range of 400-1000 mg/L, and when NH (NH) of the bacterial liquid4 +When the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 73%, the ammonia nitrogen concentration is 500-700 mg/L, and the optimal range of the ammonia nitrogen concentration of the bacterial liquid is obtained;
5-2) confirming the optimal range of the carbon-nitrogen ratio of the bacterial liquid: respectively adopting sequencing batch mode and continuous flow mode to operate moving bed reactorControlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within 72h, adding a carbon source and a nitrogen source to change the carbon-nitrogen ratio of the bacterial liquid within 1-15 when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, and when NH of the bacterial liquid4 +The carbon-nitrogen ratio is 8-10 when the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 82%, and the optimal range of the carbon-nitrogen ratio of the bacterial liquid is obtained;
5-3) confirming the optimal range of the hydraulic retention time of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the carbon-nitrogen ratio of the bacterial liquid to be 8-10 by adding a carbon source and a nitrogen source, controlling the flow of the bacterial liquid when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, changing the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 6-72 h, and when NH of the bacterial liquid4 +The hydraulic retention time is 24-36 h when the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 85%, and the optimal range of the hydraulic retention time of the bacterial liquid is obtained;
6) and (3) a high ammonia nitrogen wastewater treatment stage: and (4) discharging bacteria liquid in the moving bed biofilm reactor, introducing the high ammonia nitrogen wastewater to be treated, and controlling the running wastewater treatment system to treat the high ammonia nitrogen wastewater to be treated by adopting the optimized optimal process parameters.
The invention will now be further illustrated by reference to the following examples:
preparing nutrient solution by using the waste water of a livestock and poultry farm in the Banan region of Chongqing as raw water, and adding filler with the density of 1g/cm into a moving bed biomembrane reactor of a waste water treatment system3The MBBR suspended filler K1 and the polyethylene glycol particle pellets have the filling rate of 40 percent, then the nutrient solution is added into a moving bed biofilm reactor, the temperature of the solution in the moving bed biofilm reactor is kept at 30 +/-2 ℃, 5 to 10 percent of heterotrophic nitrification-aerobic denitrification composite microbial inoculum formed by compounding 10 to 20 percent of cupronickel bacteria SWA1, 5 to 20 percent of alcaligenes faecalis, 10 to 30 percent of acinetobacter and 20 to 50 percent of ochrobactrum SiCOC-2 is added into a biological reaction tank according to the volume of the nutrient solution to form a bacterial solution, a wastewater treatment system is operated, the HRT is 24hDO is 2-4 mg/L, so that the living bacteria of the heterotrophic nitrification-aerobic denitrification composite bacteria agent are adsorbed on the filler in the moving bed biofilm reactor, and the OD of the bacteria liquid at the 3 rd day600Is sharply reduced, NH4+Average removal rates of-N, COD and TN are respectively 80.3%, 95% and 81.4%, and a light yellow biological film is rapidly formed on a filler in the moving bed biological film reactor;
NH of bacterial liquid after 3d4 +The concentrations of-N, COD and TN are respectively reduced to 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, the removal rates can respectively reach 90.2%, 95% and 81.4%, and the OD of the bacteria liquid600The value of the biological membrane is increased to 1.3, thus finishing the enrichment of live bacteria in the bacterial liquid and gradually increasing the thickness of the biological membrane on the filler in the moving bed biological membrane reactor.
After finishing the enrichment of live bacteria in the bacteria liquid, detecting NH of the bacteria liquid in the moving bed biomembrane reactor once every 3d4 +Concentration of N, COD, TN, once NH4 +The concentration of-N, COD and TN is lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, nutrient solution is continuously added into the moving bed biofilm reactor until a layer of tawny biofilm is formed on the filler in the moving bed biofilm reactor, and when protozoa exist on the surface of the biofilm through microscope observation, the OD of the bacterial solution in the biological reaction tank is detected600Numerical value of (1) and NH4 +Removal of N, COD, TN, NH4 +Average removal rates of-N, COD and TN are 90%, 95% and 85% and are kept stable, the removal rate of each pollutant is high, namely, the biofilm formation in the moving bed biofilm reactor is finished, and the addition of nutrient solution is stopped for 12-15 days.
After the biofilm formation in the moving bed biofilm reactor is finished, entering an optimal process parameter optimization stage to obtain the optimal ammonia nitrogen concentration, the optimal carbon-nitrogen ratio and the optimal hydraulic retention time of bacteria liquid, and comprising the following steps of:
a) confirming the optimal range of the ammonia nitrogen concentration of the bacterial liquid: respectively adopting sequencing batch mode and continuous flow mode to operate the moving bed biofilm reactor, controlling the flow of bacteria liquid, controlling the hydraulic retention time of the bacteria liquid in the moving bed biofilm reactor within 72h, andammonium sulfate and anhydrous sodium acetate are added to ensure that the ammonia nitrogen concentration of the bacterial liquid is changed within the range of 400-1000 mg/L when the carbon-nitrogen ratio of the bacterial liquid is 8, and when NH of the bacterial liquid is generated4 +When the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 73%, the ammonia nitrogen concentration is 500-700 mg/L, and the optimal range of the ammonia nitrogen concentration of the obtained bacterial liquid is 500-700 mg/L;
b) determining the optimal range of the carbon-nitrogen ratio of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor to be within the range of 72h, adding ammonium sulfate and anhydrous sodium acetate to ensure that the carbon-nitrogen ratio of the bacterial liquid is changed within the range of 1-15 when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, and when NH of the bacterial liquid4 +The carbon-nitrogen ratio is 8-10 when the average removal rate of N, COD and TN is stabilized at 90%, 95% and 82%, namely the optimal range of the carbon-nitrogen ratio of the bacterial liquid is 8-10;
c) determining the optimal range of the hydraulic retention time of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the carbon-nitrogen ratio of the bacterial liquid to be 8-10 by adding ammonium sulfate and anhydrous sodium acetate, controlling the flow of the bacterial liquid when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, changing the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 6-72 h, and when NH (NH) of the bacterial liquid4 +The hydraulic retention time is 24 hours when the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 85%, and the optimal range of the hydraulic retention time of the obtained bacterial liquid is 24-32 hours;
the change condition of each water quality index of bacteria liquid in the moving bed biofilm reactor is shown in figure 2.
When the wastewater of a certain livestock and poultry farm in the Banan area of Chongqing city is treated, the bacteria liquid in the moving bed biofilm reactor is discharged firstly, the wastewater to be treated is introduced, the optimized optimal process parameters are adopted to control the operation of the wastewater treatment system for treatment, and NH of the treated wastewater4 +The removal rates of-N, COD and TN are respectively 90%, 95% and 80%, and all indexes meet the livestock and poultry breeding wastewater discharge standard (GB 18596-2001).
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and modifications of the present invention by those skilled in the art are within the scope of the present invention without departing from the spirit of the present invention.
Claims (6)
1. A process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor is characterized by comprising the following steps:
1) a film formation preparation stage:
1-1) preparing a nutrient solution with the same components as the high ammonia nitrogen wastewater to be treated;
1-2) adding an MBBR suspended filler K1 and polyethylene glycol pellets as fillers into a moving bed biofilm reactor of a wastewater treatment system, wherein the filling rate of the fillers in the moving bed biofilm reactor is 15-67%;
1-3) adding the nutrient solution prepared in the step 1-1) into a moving bed biofilm reactor of a wastewater treatment system to serve as a culture medium, and adding a heterotrophic nitrification-aerobic denitrification composite microbial inoculum with the inoculum size of 5-10% according to the volume of the nutrient solution to form a bacterial solution;
2) and (3) viable bacteria adsorption stage:
operating a wastewater treatment system, controlling the flow of bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 24-72 h, and maintaining the dissolved oxygen concentration in the bacterial liquid within the range of 2-4 mg/L through an aeration device and a flowmeter of the wastewater treatment system, so that the viable bacteria of the heterotrophic nitrification-aerobic denitrification composite microbial inoculum are adsorbed on the surface of the filler, and a light yellow biofilm is quickly formed;
3) and (3) viable bacteria enrichment stage:
OD for detecting bacteria liquid in moving bed biofilm reactor600Numerical value of (1) and NH4 +Concentration of-N, COD, TN, if OD600Is less than 1, and NH4 +Respectively controlling the concentration of-N, COD and TN to be lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, and continuously adding nutrient solution into the moving bed biofilm reactor to make the OD of the bacterial solution600The number of the bacteria reaches 1 to 1.5, and the viable bacteria in the bacteria liquidThe content reaches 180-200 hundred million/g, thus finishing the enrichment of live bacteria in the bacterial liquid;
4) and (3) film formation finishing stage:
after finishing the enrichment of live bacteria in the bacteria liquid, detecting NH of the bacteria liquid in the moving bed biofilm reactor4 +Concentration of N, COD, TN, once NH4 +Respectively controlling the concentration of-N, COD and TN to be lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, continuously adding nutrient solution into the moving bed biofilm reactor until a layer of tawny biofilm is formed on the filler in the moving bed biofilm reactor, observing protozoa on the surface of the biofilm through a microscope, and detecting the OD of the bacterial solution in the moving bed biofilm reactor600Numerical value of (1) and NH4 +Concentration of-N, COD, TN, OD of the bacterial liquid600Is less than 0.2, NH4 +The concentrations of-N, COD and TN are respectively lower than 80-100 mg/L, 150-200 mg/L and 80-108 mg/L, namely the biofilm formation in the moving bed biofilm reactor is finished, and the nutrient solution is stopped to be added;
5) optimizing process parameters:
5-1) determining the optimal range of the ammonia nitrogen concentration of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor to be within 72h, adding a carbon source and a nitrogen source to enable the carbon-nitrogen ratio of the bacterial liquid to be 8, changing the ammonia nitrogen concentration of the bacterial liquid within the range of 400-1000 mg/L, and when NH (NH) of the bacterial liquid4 +When the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 73%, the ammonia nitrogen concentration is 500-700 mg/L, and the optimal range of the ammonia nitrogen concentration of the bacterial liquid is obtained;
5-2) determining the optimal range of the carbon-nitrogen ratio of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the flow of the bacterial liquid, controlling the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 72h, adding a carbon source and a nitrogen source to ensure that the carbon-nitrogen ratio of the bacterial liquid is changed within the range of 1-15 when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, and when NH of the bacterial liquid4 +of-N, COD, TNWhen the average removal rate is stabilized at 90%, 95% and 82%, the carbon-nitrogen ratio is 8-10, and the optimal range of the carbon-nitrogen ratio of the bacterial liquid is obtained;
5-3) confirming the optimal range of the hydraulic retention time of the bacterial liquid, namely operating the moving bed biofilm reactor in a sequencing batch mode and a continuous flow mode respectively, controlling the carbon-nitrogen ratio of the bacterial liquid to be 8-10 by adding a carbon source and a nitrogen source, controlling the flow of the bacterial liquid when the ammonia nitrogen concentration of the bacterial liquid is 500-700 mg/L, changing the hydraulic retention time of the bacterial liquid in the moving bed biofilm reactor within the range of 6-72 h, and when NH of the bacterial liquid4 +The hydraulic retention time is 24-36 h when the average removal rate of-N, COD and TN is stabilized at 90%, 95% and 85%, and the optimal range of the hydraulic retention time of the bacterial liquid is obtained;
6) and (3) a high ammonia nitrogen wastewater treatment stage: and (4) discharging bacteria liquid in the moving bed biofilm reactor, introducing the high ammonia nitrogen wastewater to be treated, and controlling the running wastewater treatment system to treat the high ammonia nitrogen wastewater to be treated by adopting the optimized optimal process parameters.
2. The process for treating high ammonia nitrogen wastewater by using the moving bed biofilm reactor of claim 1, wherein the nutrient solution in the step 1-1) comprises 2.9-3.2 g/L of anhydrous sodium acetate, 2.1-2.3 g/L of ammonium sulfate, 0.6-0.8 g/L of dipotassium hydrogen phosphate, 1.9-2.1 g/L of magnesium sulfate heptahydrate, 0.1-0.2 g/L of magnesium sulfate monohydrate, 1.4-1.6 g/L of calcium chloride and 0.1-0.2 g/L of ferrous sulfate heptahydrate.
3. The process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor according to claim 2, which is characterized in that: the preparation steps of the nutrient solution are as follows:
a) preparing solution of trace elements
The trace element solution comprises 1.9-2.0 g/L of mixed magnesium sulfate heptahydrate, 0.1-0.2 g/L of magnesium sulfate monohydrate, 1.4-1.5 g/L of calcium chloride and 0.1-0.2 g/L of ferrous sulfate heptahydrate;
b) preparing simulated high ammonia nitrogen wastewater
Calculating the adding amount of a carbon source, a nitrogen source and a phosphorus source by using the effective volume of the moving bed biofilm reactor, wherein the adding proportion is that anhydrous sodium acetate is 4.73 g/L, ammonium sulfate is 2.03 g/L, and dipotassium phosphate is 0.14 g/L, and the obtained NH simulating the high ammonia nitrogen wastewater4 +The concentrations of N, COD and TN are 480-520 mg/L, 40000-40100 mg/L and 520-540 mg/L respectively;
c) preparing nutrient solution
The prepared simulated high ammonia nitrogen wastewater is mixed with trace element solution = 1L: 5m L.
4. The process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor according to claim 1, which is characterized in that: the heterotrophic nitrification-aerobic denitrification composite microbial inoculum comprises cuppridinium bulimia SWA1, alcaligenes faecalis, acinetobacter and ochrobactrum TAC-2.
5. The process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor according to claim 4, which is characterized in that: the content ratio of the cuppridinium bulimia SWA1, the alcaligenes faecalis, the acinetobacter and the ochrobactrum anthropi TAC-2 in the heterotrophic nitrification-aerobic denitrification composite microbial agent is 10-20%: 5-20%: 10-30%: 20 to 50 percent.
6. The process for treating high ammonia nitrogen wastewater by using a moving bed biofilm reactor according to claim 1, which is characterized in that: the temperature of the bacteria liquid in the moving bed biofilm reactor is kept within the range of 30 +/-2 ℃ through a temperature control system in the wastewater treatment system.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109337832A (en) * | 2018-03-14 | 2019-02-15 | 重庆理工大学 | A kind of anthropi of resistance to high ammonia nitrogen heterotrophic nitrification-aerobic denitrification and its application |
| CN113213644A (en) * | 2021-04-20 | 2021-08-06 | 复旦大学 | Method for treating high-concentration ammonia nitrogen wastewater by culturing nitrification combined flora |
| CN115353191A (en) * | 2022-08-23 | 2022-11-18 | 北京工业大学 | Method for treating high-C/N wastewater to realize efficient denitrification by using aerobic biofilm reactor |
| CN115974298A (en) * | 2022-11-15 | 2023-04-18 | 上海交通大学重庆研究院 | Nitrogen-carbon salt matter full-flow treatment system for landfill leachate emergency concentrated solution |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102786140A (en) * | 2011-05-20 | 2012-11-21 | 北京师范大学 | Surface modification method of polypropylene biological filling material |
| CN102976553A (en) * | 2012-11-19 | 2013-03-20 | 四川大学 | Method for biological denitrogenation of nitrogen-containing organic industrial wastewater |
| CN108585195A (en) * | 2018-03-14 | 2018-09-28 | 重庆理工大学 | Low temperature low-carbon ammonia nitrogen wastewater treatment device and method based on solid phase denitrification and heterotrophic nitrification-aerobic denitrification |
| CN109082387A (en) * | 2018-03-14 | 2018-12-25 | 重庆理工大学 | It is a kind of can low temperature remove heterotrophic nitrification-aerobic denitrification composite bacteria agent and its application of high ammonia nitrogen |
-
2020
- 2020-03-09 CN CN202010156444.XA patent/CN111422976A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102786140A (en) * | 2011-05-20 | 2012-11-21 | 北京师范大学 | Surface modification method of polypropylene biological filling material |
| CN102976553A (en) * | 2012-11-19 | 2013-03-20 | 四川大学 | Method for biological denitrogenation of nitrogen-containing organic industrial wastewater |
| CN108585195A (en) * | 2018-03-14 | 2018-09-28 | 重庆理工大学 | Low temperature low-carbon ammonia nitrogen wastewater treatment device and method based on solid phase denitrification and heterotrophic nitrification-aerobic denitrification |
| CN109082387A (en) * | 2018-03-14 | 2018-12-25 | 重庆理工大学 | It is a kind of can low temperature remove heterotrophic nitrification-aerobic denitrification composite bacteria agent and its application of high ammonia nitrogen |
Non-Patent Citations (2)
| Title |
|---|
| 刘向阳 等: "《HN-AD菌强化3D-RBC处理养猪废水及微生物特性研究》", 《中国环境科学》 * |
| 王荣昌 等: "《流动床生物膜反应器在污水处理中的应用研究现状》", 《环境污染治理技术与设备》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109337832A (en) * | 2018-03-14 | 2019-02-15 | 重庆理工大学 | A kind of anthropi of resistance to high ammonia nitrogen heterotrophic nitrification-aerobic denitrification and its application |
| CN113213644A (en) * | 2021-04-20 | 2021-08-06 | 复旦大学 | Method for treating high-concentration ammonia nitrogen wastewater by culturing nitrification combined flora |
| CN115353191A (en) * | 2022-08-23 | 2022-11-18 | 北京工业大学 | Method for treating high-C/N wastewater to realize efficient denitrification by using aerobic biofilm reactor |
| CN115974298A (en) * | 2022-11-15 | 2023-04-18 | 上海交通大学重庆研究院 | Nitrogen-carbon salt matter full-flow treatment system for landfill leachate emergency concentrated solution |
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