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    • 专利摘要:
    The invention belongs to the field of sewage treatment. Specifically; it relates to antibiotic wastewater treatment process and the system used in the wastewater 5 treatment process. The process of the invention comprises the following steps: (1) The antibiotic wastewater is pumped with the peristaltic pump from the water feeding tank into the reactor of upflow anaerobic composite bed for anaerobic treatment; (2) As defined in (l); the water after anaerobic treatment is delivered to the electrochemical reactor for further treatment and then discharged via the 10 second outlet. Beneficial effects of the invention: the use of the invented method and system to treat antibiotic wastewater reduces the cycle of antibiotic wastewater treatment; less power consumption reduces the cost; stable system operation maintains the rates of removing CODcr and ammonia nitrogen within certain range; CODcr and ammonia nitrogen removal rate over 90% demonstrates 15 the excellent treatment effect.
    公开号:NL2024125A
    申请号:NL2024125
    申请日:2019-10-30
    公开日:2021-02-01
    发明作者:Wang Hao；Bo Guozhu；Lu Huan；Zhong Huiyuan；Yang Yong；Luo Litao；Li Fuping
    申请人:Univ North China Science & Technology；
    IPC主号:
    专利说明:

    ANTIBIOTIC WASTEWATER TREATMENT PROCESS ANDSYSTEM
    FIELD OF INVENTION The invention belongs to the field of sewage treatment. Specifically, it relates to antibiotic wastewater treatment process and the system used in the wastewater treatment process.
    BACKGROUND OF THE PRESENT INVENTION Antibiotics are organic substances produced (or obtained through other means) by living organisms, including microorganisms, plants, and animals, in the course of their life activities, that selectively inhibit or affect other biological functions at low concentrations. China is not only a big country of antibiotic consumption, but also a big country of antibiotic production. Antibiotic wastewater 1s characterized with complex composition, poor biodegradability, deep color, high toxicity and high CODer, SS and ammonia nitrogen, as well as difficult degradation. Anaerobic biological treatment technology provides advantages of high load, less sludge production and higher economic benefits. It can be used to treat refractory, high concentration organic wastewater. However, the anaerobic biological treatment technology 1s disadvantaged due to long start- up time and the difficulty in meeting the emission requirements: when single UBF reactor 1s used to treat antibiotic wastewater, with COD being 9000--10000mg/L, the COD removal rate is up to 91.7%. But COD effluent after treatment 1s still up to 700--800mg/L. So further treatments are required. Electrocatalytic oxidation technology is characterized with high treatment efficiency and that no other pollutants are produced in the process of treatment. By introducing catalyst, electrochemical oxidation technology can improve degradation rate and efficiency. When electrocatalytic oxidation is used to treat antibiotic wastewater,
    for three-hour degradation, COD could be degraded from 450mg/L to 40mg/L, and the removal rate can reach over 91%. The lower COD in inlet water, the shorter the degradation time and the less power consumption, which can effectively save the cost. As for the treatment process of antibiotic wastewater, the following patents/patent application documents disclose: CN108558003A A method and an installation using two-stage MBR to remove various pollutants from antibiotic wastewater, 1.e. using a two-stage anaerobic MBR unit to treat the antibiotic wastewater. The disadvantage is also the issue of long processing time, in addition to the following issues: the water treated by anaerobic biological treatment technology is often unable to meet the requirement for direct emission and needs further treatment.
    CN106745532A A method of treating antibiotic wastewater, wherein it comprises the following specific steps: (1) Take certain amount of filler particle electrode, which can be Fe30., titanium foam, activated carbon, ceramic, zeolite, kaolin, carbon nanofiber, graphene or carbon aerogel, etc. Put it in the electrocatalytic oxidation unit after sequential treatment. Adjust pH, and control air flow. Take samples for analysis after certain reaction time.
    (2) The electrocatalytic oxidation installation is provided with evenly distributed fine tubes on its tank bottom. An opening is provided in the bottom so as to ensure uniform water distribution and air intake. The anode is Ti/SnO,, and the cathode is stainless steel plate electrode, which 1s fixed on both sides of the tank body.
    The above patents use an electrocatalytic oxidation tank to treat antibiotic wastewater. The disadvantage is that solely using the electrocatalytic oxidation tank to treat the wastewater leads to higher treatment cost due to increase of power consumption.
    Therefore, it is necessary to eliminate the above defects by inventing a wastewater treatment method that can effectively treat antibiotic wastewater with less cost in power consumption.
    SUMMARY OF THE INVENTION To solve the above technical issues, the invention provides a wastewater treatment process that can effectively treat antibiotic wastewater with less cost in power consumption.
    The invention also provides a system used for the process.
    The antibiotic wastewater treatment process comprises the following primary steps: (1) Inoculate granular sludge under aerobic conditions until filamentous bacteria multiply. Then transfer the inoculated granular sludge to the upflow anaerobic composite bed reactor to form a granular sludge layer, on which a sludge layer is paved, followed up by a layer of packing of polyurethane foam; oxygen 1s injected into the upflow anaerobic composite bed reactor through its first circulation port and second circulation port, while the dissolved oxygen in upflow anaerobic composite bed reactor is controlled at 1-3mg/L; when the amount of biofilm formation reaches 3-5g:9°t and becomes stable, inject nitrogen to convert the former aerobic environment into anaerobic environment; (2) Transfer the nutrient solution to upflow anaerobic composite bed reactor and control COD=800-1200mg/L, pH=6.5-7.5; the nutrient solution successively passes through the granular sludge layer , suspended sludge layer and polyurethane foam packing layer in the upflow anaerobic composite bed reactor. The retention time of nutrient solution in upflow anaerobic composite bed reactor 1s 22 to 26 hours; Then use the peristaltic pump to pump the antibiotic wastewater from the water feeding tank to the upflow anaerobic composite bed reactor for anaerobic treatment, during which the supply quality of antibiotic wastewater should be CODcr=6400-6600mg/L, with ammonia nitrogen being 120-130 mg/L and pH=6.5-7.5, inflow controlled at 0.3-0.5L/h, organic loading being 1- 3kgCOD/m -d and continuous feeding for 3 to 5 hours; Regularly check the sludge concentration and the amount of biofilm formation on the packing layer via the sampling port. When the sludge concentration and the amount of biofilm formation become stable, supply the antibiotic wastewater diluted to different multiples to the upflow anaerobic composite bed reactor. By controlling the COD concentration at water inlet, maintain the organic loading gradient at 1-2kgCOD/m -d until the CODcr and ammonia nitrogen removal rate is stable; (3) Deliver the anaerobic treated wastewater in (1) to the electrochemical reactor through the first outlet for treatment with hydrogen peroxide as the catalyst, and then discharge it through the second outlet.
    Preferably, in (1), the height ratio of granular sludge layer to the suspended sludge layer and the polyurethane foam packing layer is 3: 3: 4.
    The height ratio of granular sludge layer to upflow anaerobic composite bed reactor is 1:6.
    In (1), when the amount of biofilm formation reaches 4g-g' and becomes stable, inject nitrogen to convert the former aerobic environment into anaerobic environment; (2) Transfer the nutrient solution to upflow anaerobic composite bed reactor and control COD=1000mg/L, pH=7; the nutrient solution successively passes through the granular sludge layer, the suspended sludge layer and the polyurethane foam packing layer in the reactor. The retention time of nutrient solution in upflow anaerobic composite bed reactor is 24 hours; Then use the peristaltic pump to pump the antibiotic wastewater from the water feeding tank to the upflow anaerobic composite bed reactor for anaerobic treatment, during which the supply quality of antibiotic wastewater should be CODcr=6500mg/L, with ammonia nitrogen being 125 mg/L and pH=7, inflow controlled at 0.4L/h, organic loading being 1.5kgCOD/m’:d and continuous feeding for 4 hours.
    Oxygen is injected into the upflow anaerobic composite bed reactor through its first circulation port and second circulation port, while the dissolved oxygen in upflow anaerobic composite bed reactor is controlled at 2mg/L;
    5 Regularly check the sludge concentration and the amount of biofilm formation on the packing layer via the sampling port.
    When the sludge concentration and the amount of biofilm formation become stable, supply the antibiotic wastewater diluted to different multiples to the upflow anaerobic composite bed reactor.
    By controlling the COD concentration at water inlet,
    maintain the organic loading gradient at 1.5kgCOD/m -d until the CODer and ammonia nitrogen removal rate is stable; In (3), the mass concentration of hydrogen peroxide is 26 -30%, and the dosage is 0.1 -0.3% of the volume of wastewater.
    Preferably, in (3), the mass concentration of hydrogen peroxide is 28%, and the dosage 1s 0.2% of the volume of wastewater.
    The system used for the antibiotic wastewater treatment process comprises the following components: The system comprises a water feeding tank, which is connected to the water inlet of the upflow anaerobic composite bed reactor through a pipeline.
    Inside the upflow anaerobic composite bed reactor there are, from bottom to top, a granular sludge layer, a suspended sludge layer and a packing layer.
    The upflow anaerobic composite bed reactor 1s provided with a sampling port on the left and a vent on the top.
    A corresponding sealing cover is provided on the vent.
    The upflow anaerobic composite bed reactor is provided with the first circulation port in the bottom close to the right end and the second circulation port in the lower middle part to the right end.
    The first water outlet on the upper part of the upflow anaerobic composite bed reactor is connected to the electrochemical reactor through a pipeline.
    The electrochemical reactor contains an electrode, which 1s connected with the power supply device. The second water outlet 1s provided on the right side of the electrochemical reactor.
    The upflow anaerobic composite bed reactor is a cylindrical plexiglass vessel with a ratio of 1:6 in diameter to height and 1:20 m wall thickness to diameter.
    The sampling port is designed at a height of 2/3 from top to bottom at the left end of the up-flow anaerobic composite bed reactor. The first water outlet is arranged at a height of 1/12 from top to bottom on the right side of the upflow anaerobic composite bed reactor. A circular vent is provided at the center of the upper cover of the up-flow anaerobic composite bed reactor. The diameter of the vent is of a ratio 1:5 compared with that of the cross-section of the up-flow anaerobic composite bed reactor.
    The electrochemical reactor is a cuboid vessel with a length-width-height ratio of 16:15:16. The second water outlet is provided at a height of 1/8 from bottom to top of the electrochemical reactor. The diameter of the outlet pipe connected to the second water outlet 1s 1/50 of the width of the electrochemical reactor and its length 1s 2/15 of the width of the electrochemical reactor.
    The electrode materials include anode and cathode, wherein the anode is SnO,-Sb/Ti and the cathode 1s made of stainless steel.
    Benefits of the invention: (1) The invention uses UBF reactor and electrocatalytic oxidation unit to Jointly act on antibiotic wastewater, which reduces the treatment cycle of antibiotic wastewater.
    (2) The antibiotic wastewater treated by the mstallation of the invention meets the requirement for emission.
    (3) In consideration of energy consumption and cost reduction, the invention employs the UBF reactor for pretreatment, and then uses the electrocatalytic oxidation unit for joint treatment, which greatly reduces power consumption, as compared with solely using the electrocatalytic oxidation method for treatment of antibiotic wastewater. The invention considerably reduces the power consumption of the effluent of the electrocatalytic oxidation treatment reactor and saves the cost. (4) The system of the invention runs stably and the removal rate of CODecr and ammonia nitrogen is kept within a certain range. Antibiotic wastewater treated by the installation and process of the invention enjoys the removal rates of CODcr and ammonia nitrogen up to 54% and 65% in effluent of the UBF reactor during stable operation. The rates of removing CODcr and ammonia nitrogen from the effluent after electrocatalytic oxidation are more than 90%, indicating an excellent treatment.
    BRIEF DESCRIPTION OF THE DRAWINGS Figure 1A is a diagram of system components defined in embodiment 1 of the invention. Wherein, 1- water feeding tank, 2- peristaltic pump, 3- water inlet, 31- sampling port, 21- packing layer, 33- suspended sludge, 34- granular sludge, 4- UBF reactor, 5- vent, 6- the first outlet, 7- the second circulation port, 8- the first circulation port, 9- circulation pump, 10- electrode, 12- electrochemical reactor, 13- the second outlet
    DETAILED DESCRIPTION In order to enable the technicians in this field to better understand the invention, further explanation of the invention is given in combination with the specific embodiments. Embodiment 1A As shown in Figure 1, the components of the installation of the invention are as the following: The system of the invention comprises a water feeding tank (1), which is connected to the water inlet (3) of the upflow anaerobic composite bed reactor (4) through a pipeline. Inside the upflow anaerobic composite bed reactor (4) there are, from bottom to top, a granular sludge layer (34), a suspended sludge layer (33) and a packing layer (32).
    The upflow anaerobic composite bed reactor (4) is provided with the first circulation port (8) in the bottom close to the right end and the second circulation port (7) in the lower middle part to the right side.
    The upflow anaerobic composite bed reactor (4) is a cylindrical plexiglass vessel with a ratio of 1:6 in diameter to height and 1:20 in wall thickness to diameter. The sampling port (31) 1s designed at a height of 2/3 from top to bottom at the left end of the up-flow anaerobic composite bed reactor (4). The first water outlet (6) is arranged at a height of 1/12 from top to bottom on the right side of the upflow anaerobic composite bed reactor (4). A circular vent (5) is provided at the center of the upper cover of the up-flow anaerobic composite bed reactor (4).
    The diameter of the vent (5) is of a ratio 1:5 compared with that of the cross- section of the up-flow anaerobic composite bed reactor (4).
    The first water outlet (6) on the upper part of the upflow anaerobic composite bed reactor (4) 1s connected to the electrochemical reactor (12) through a pipeline. The electrochemical reactor (12) contains an electrode (11), which is connected with the power supply device (10). The second water outlet (13) is provided on the right side of the electrochemical reactor (12).
    The electrochemical reactor (12) 1s a cuboid vessel with a length-width-height ratio of 16:15:16. The second water outlet (13) is provided at a height of 1/8 from bottom to top of the electrochemical reactor (12). The diameter of the outlet pipe connected to the second water outlet (13) is 1/50 of the width of the electrochemical reactor (12) and its length 1s 2/15 of the width of the electrochemical reactor (12). For electrode materials the anode 1s SnO,-Sb/Ti and the cathode is made of stainless steel.
    Embodiment 1B Compared with embodiment 1, embodiment 1B is a pilot trial case in specific industrial production, as follows: The UBF reactor (4) is a cylindrical plexiglass reactor with 100mm in diameter, 600mm in height and 5mm in wall thickness. The UBF reactor (4) 1s provided with a water inlet (3) on the bottom, which is connected to the water feeding tank (1) through a pipeline. A sampling port (31) is designed 1n the left end of the UBF reactor (4), 200mm from the bottom. A circulation port (2) is provided on the right end, 200mm from the bottom. The first water outlet (6) is provided at 50mm to the top end of the UBF reactor (4). On top the UBF reactor (4) there is a cover, on which a round vent (5) is provided in the middle. Diameter of the top cover 1s 100mm. On the bottom of the UBF reactor (4) is the mature granular sludge layer (34) in the UASB rector, (the granular sludge layer treated in step (1) according to the embodiment 1), in a height of 120mm. The granular sludge layer (34) is covered with a backflow sludge layer (33) (i.e. the suspended sludge layer) taken from the secondary sedimentation tank of the sewage plant, in a height of 120mm. Above the granular sludge, a polyurethane foam packing layer (32) is provided in a height of 160mm. The electrochemical reactor (12) is a cuboid vessel with a length, width and height being respectively: 160mm, 150mm and 160mm. The second water outlet (13) 1s provided at a height of 20mm from bottom to top of the electrochemical reactor (12). The outlet pipe connected to the second water outlet (13) is 3mm in diameter and 20mm 1n length.
    Embodiment IC The practical operation of the system defined in embodiment 1 follows a principle as below:
    The speed and amount of biofilm formation determine how fast the UBF reactor (4) will start.
    To improve the starting efficiency of the reactor, the invention adopts aerobic moculation of sludge to make filamentary bacteria multiply rapidly.
    The moculated sludge is transferred to the UBF reactor (4). When the biofilm formation becomes stable, nitrogen 1s injected to convert the former aerobic environment into anaerobic environment.
    The aerobic inoculated strains are common strains.
    The carrier of strain is common activated sludge.
    That is to say, the strain in activated sludge is used whose inoculated volume of sludge is 25%. The antibiotic wastewater is subject to anaerobic treatment in the UBF reactor (4). But the wastewater after anaerobic treatment cannot meet the requirement for direct emission.
    Further treatments are necessary.
    The invention uses electrocatalytic oxidation to further treat the effluent from the UBF reactor (4) by utilizing hydrogen peroxide as the catalyst and performing electrocatalytic oxidation treatment of wastewater with electrode plates, so as to have the wastewater effectively treated to the emission standard, in addition to reduction of high energy consumption and high cost brought by solely application of the electrocatalytic oxidation treatment.
    Embodiment 2 Use the system defined in embodiment 1 to treat antibiotic wastewater (the following embodiments and comparison cases shall be referred to as treatment with the system defined in embodiment 1 if not noted otherwise), and the antibiotic wastewater treatment process comprises the following primary steps: (1) Inoculate granular sludge under aerobic conditions until filamentous bacteria multiply.
    Then transfer the inoculated granular sludge to the upflow anaerobic composite bed reactor (4) to form a granular sludge layer (34), on which a suspended sludge layer (33) is paved.
    The suspended sludge layer (33) is the backflow sludge from the secondary sedimentation tank of the sewage plant.
    Then a packing layer of polyurethane foam (32) is applied.
    When the amount of biofilm formation reaches 4g:g! and becomes stable, inject nitrogen to convert the former aerobic environment into anaerobic environment; (2) Transfer the nutrient solution to upflow anaerobic composite bed reactor (4) and control COD=1000mg/L, pH=7; the nutrient solution successively passes through the granular sludge layer (34), the suspended sludge layer (33) and the polyurethane foam packing layer (32) in the reactor. The retention time of nutrient solution 1n upflow anaerobic composite bed reactor (4) is 24 hours; Then use the peristaltic pump to pump the antibiotic wastewater from the water feeding tank (1) to the upflow anaerobic composite bed reactor (4) for anaerobic treatment, during which the supply quality of antibiotic wastewater should be CODcr=6500mg/L, with ammonia nitrogen being 125 mg/L and pH=7, inflow controlled at 0.4L/h, organic loading being 2kgCOD/m :d and continuous feeding for 4 hours. Oxygen is injected into the upflow anaerobic composite bed reactor (4) through its first circulation port (8) and second circulation port (7), while the dissolved oxygen in upflow anaerobic composite bed reactor (4) is controlled at 2mg/L; Regularly check the sludge concentration and the amount of biofilm formation on the packing layer via the sampling port (31). When the sludge concentration and the amount of biofilm formation become stable, replace the feeding water with the antibiotic wastewater diluted to different multiples. By controlling the COD concentration at water inlet, maintain the organic loading gradient at 2kgCOD/m’-d until the CODcr and ammonia nitrogen removal rate 1s stable; (3) Deliver the anaerobic treated wastewater in (1) to the electrochemical reactor for treatment with hydrogen peroxide as the catalyst, and then discharge it through the second outlet (13). The hydrogen oxide is provided with a mass concentration of 28% and its dosage takes up 0.2% of the volume of wastewater.
    Embodiment 3
    The antibiotic wastewater treatment process comprises the following primary steps:
    (1) Inoculate granular sludge under aerobic conditions until filamentous bacteria multiply.
    Then transfer the inoculated granular sludge to the upflow anaerobic composite bed reactor (4) to form a granular sludge layer (34), on which a suspended sludge layer (33) is paved.
    The suspended sludge layer (33) is the backflow sludge from the secondary sedimentation tank of the sewage plant.
    Then a packing layer of polyurethane foam (32) is applied.
    When the amount of biofilm formation reaches 3.5g:g7 and becomes stable, inject nitrogen to convert the former aerobic environment into anaerobic environment;
    (2) Transfer the nutrient solution to upflow anaerobic composite bed reactor (4) and control COD=900mg/L, pH=6.8; the nutrient solution successively passes through the granular sludge layer (34), the suspended sludge layer (33) and the polyurethane foam packing layer (32) in the reactor.
    The retention time of nutrient solution In upflow anaerobic composite bed reactor (4) is 24 hours;
    Then use the peristaltic pump to pump the antibiotic wastewater from the water feeding tank (1) to the upflow anaerobic composite bed reactor (4) for anaerobic treatment, during which the supply quality of antibiotic wastewater should be CODcr=6400mg/L, with ammonia nitrogen being 120 mg/L and pH=7.2, inflow controlled at 0.35L/h, organic loading being 2kgCOD/m -d and continuous feeding for 4 hours.
    Oxygen is injected into the upflow anaerobic composite bed reactor (4) through its first circulation port (8) and second circulation port (7), while the dissolved oxygen in upflow anaerobic composite bed reactor (4) is controlled at 1.8mg/L;
    Regularly check the sludge concentration and the amount of biofilm formation on the packing layer via the sampling port (31). When the sludge concentration and the amount of biofilm formation become stable, replace the feeding water with the antibiotic wastewater diluted to different multiples.
    By controlling the COD concentration at water inlet, maintain the organic loading gradient at 1.8kgCOD/m :d until the CODcr and ammonia nitrogen removal rate 1s stable; (3) Deliver the anaerobic treated wastewater in (1) to the electrochemical reactor for treatment with hydrogen peroxide as the catalyst, and then discharge it through the second outlet (13). The hydrogen oxide 1s provided with a mass concentration of about 27% and its dosage takes up about 0.25% of the volume of wastewater.
    Embodiment 4 The antibiotic wastewater treatment process comprises the following primary steps: (1) Inoculate granular sludge under aerobic conditions until filamentous bacteria multiply. Then transfer the inoculated granular sludge to the upflow anaerobic composite bed reactor (4) to form a granular sludge layer (34), on which a suspended sludge layer (33) is paved. The suspended sludge layer (33) is the backflow sludge from the secondary sedimentation tank of the sewage plant. Then a packing layer of polyurethane foam (32) is applied. When the amount of biofilm formation reaches 4g:g! and becomes stable, inject nitrogen to convert the former aerobic environment into anaerobic environment; (2) Transfer the nutrient solution to upflow anaerobic composite bed reactor (4) and control COD=1100mg/L, pH=7.2; the nutrient solution successively passes through the granular sludge layer (34), the suspended sludge layer (33) and the polyurethane foam packing layer (32) in the reactor. The retention time of nutrient solution in upflow anaerobic composite bed reactor (4) is 24 hours; Then use the peristaltic pump to pump the antibiotic wastewater from the water feeding tank (1) to the upflow anaerobic composite bed reactor (4) for anaerobic treatment, during which the supply quality of antibiotic wastewater should be CODcr=6600mg/L, with ammonia nitrogen bemg 125mg/L and pH=7.2, inflow controlled at 0.4L/h, organic loading being 2.4kgCOD/m -d and continuous feeding for 4 hours.
    Oxygen is injected into the upflow anaerobic composite bed reactor (4) through its first circulation port (8) and second circulation port (7), while the dissolved oxygen in upflow anaerobic composite bed reactor (4) is controlled at 2mg/L;
    Regularly check the sludge concentration and the amount of biofilm formation on the packing layer via the sampling port (31). When the sludge concentration and the amount of biofilm formation become stable, replace the feeding water with the antibiotic wastewater diluted to different multiples.
    By controlling the COD concentration at water inlet, maintain the organic loading gradient at 2.1kgCOD/m -d until the CODcr and ammonia nitrogen removal rate 1s stable;
    (3) Deliver the anaerobic treated wastewater in (1) to the electrochemical reactor for treatment with hydrogen peroxide as the catalyst, and then discharge it through the second outlet (13). The hydrogen oxide is provided with a mass concentration of about 28% and its dosage takes up around 0.2% of the volume of wastewater.
    Example of Comparison 1 The difference from embodiment 2 lies in that, in (1) of the comparison case 1, only the inoculated granular sludge was transferred to the upflow anaerobic composite bed reactor (4) to form granular sludge layer (34), followed by the paving of a packing layer of polyurethane foam (32). Others are similar to embodiment 2. The details are as follows:
    (1) Inoculate granular sludge under aerobic conditions until filamentous bacteria multiply.
    Then transfer the inoculated granular sludge to the upflow anaerobic composite bed reactor (4) to form a granular sludge layer (34). When the amount of biofilm formation reaches 4gg-1 and becomes stable, inject nitrogen to convert the former aerobic environment into anaerobic environment.
    Example of comparison 2 The difference from embodiment 2 lies in that, instead of undergoing treatment in the UBF reactor for the first step, the antibiotic wastewater 1s directly treated in the electrochemical reactor (12) by using hydrogen peroxide as the catalyst, and then discharged via the second outlet. Example of comparison 3 The difference from embodiment 2 lies in that the incoming water quality CODer of the antibiotic wastewater is higher than that in embodiment 2. Others are similar to embodiment 2. The details are as follows: The antibiotic wastewater incoming quality should be CODcr=14000mg/L, with ammonia nitrogen being 125 mg/L and pH=7, inflow controlled at 0.4L/h, organic loading being 2kgCOD/m -d and continuous feeding for 4 hours. Oxygen 1s injected into the upflow anaerobic composite bed reactor through its first circulation port and second circulation port, while the dissolved oxygen in upflow anaerobic composite bed reactor is controlled at 2mg/L.
    Table 1 Treatment effect comparison between the embodiments and comparison cases The first outlet | The first outlet Th second | Th second outlet outlet fee rate % AiR CORor removal | Ammonia removal rate% rate %o nitrogen o removal rate% comparison | comparison 2
    As can be seen from the figures provided in the table above, the wastewater treated with the processes presented in embodiments 2 to 4 of the invention has a removal rate of CODcr up to 54% and a removal rate of ammonia nitrogen up to 65% in the effluent from the first outlet; and their removal rates reach 98% and 96% respectively at the second outlet.
    In the example of comparison 1, the UBF reactor contains just one granular layer. As a result, the CODcr removal rate of water discharged from the first outlet 1s about 42%, and the ammonia nitrogen removal rate 1s about 43.4%; the CODer removal rate of water discharged from the second outlet is about 87.9%, and the ammonia nitrogen removal rate is about 88.1%. The removal effect of both 1s not as good as the method presented in embodiment 2.
    In the example of comparison 2, the sole one-stage treatment in the electrochemical reactor (12) provides an effect that is far less than that in embodiment 1. By checking the water discharged from the second outlet, both the CODecr and ammonia nitrogen removal rates are around 60%, which fails to meet the direct emission requirement, in addition to high cost in energy consumption. In the example of comparison 3, the measurement of water discharged from the first outlet shows that the CODcr and ammonia nitrogen removal rates are
    50.5% and 58.7% respectively, which indicates a less effective treatment than that in embodiment 2. In addition, the CODcr and ammonia nitrogen removal rates are
    91.6% and 92.5% respectively at the second outlet, which are inferior to the effect provided by embodiment 2. Table 2 is a comparison of treatment effects and economic benefits provided with sole UBF reactor, sole catalytic oxidation and combined process.
    According to the contents and data listed 1n the table, the treatment effect of the invention is sufficient to meet the emission standard and its economic benefit is acceptable.
    Table 2 - Comparison of treatment effects between sole process and combined processes == . Emission | Economic Process Incoming Outgoing Total Emission | Incoming Outgoing Total standard | benefit COD COD ( COD standard | ammonia ammonia | ammonia met mg/L) removal met nitrogen | nitrogen { | nitrogen mg/L) rate (%) (mg/L) mg/L) removal rate% - i No Acceptable UBF reactor | 6400-6600 | 2912-30294 | 541-545 | No 120-130 | 41.04-45.11 | 65.3-658 No Low Electrocatalytic | 6500 2255.5 65.3 No 125 16.63 62.7 oxidation } Yes Acceptable Process of the | 6400-6600 | 96-1188 | 982-985 | Yes 120-130 | 42-494 | 96.2965 invention It shows from the characteristics of the antibiotic wastewater and the effect of the current antibiotic wastewater treatment process, using of only a single method is difficult to achieve a win-win result on treatment effect and economic benefit.
    Therefore, the invention adopts a method of combining the UBF reactor with the electrocatalytic oxidation to jointly treat the antibiotic wastewater, which provides a new idea for antibiotic wastewater treatment.
    Combined with the advantages and disadvantages of anaerobic biological treatment and electrocatalytic oxidation as well as the characteristics of antibiotic wastewater, a two-stage combined treatment process is proposed.
    In other words, the invention aims to discover a process for efficient treatment of antibiotic wastewater, while the single UBF anaerobic biological treatment and the single electrocatalytic oxidation cannot achieve the high efficiency and economic benefits like the two- stage combined treatment process does.
    At present, such a combined process has not been put forward yet.
    Therefore, the two-stage combined treatment process is an innovative process.
    权利要求:
    Claims (10)
    [1]
    1. An antibiotic wastewater treatment process, mainly comprising the following steps: (1) Inoculate granular sludge under aerobic conditions until the filamentous fungus is propagated and then transfer the inoculated granular sludge to an upstream anaerobic composite bed reactor (4) to form a granular sludge layer (34 ) to shape; The granular sludge layer (34) is covered with a suspended sludge layer (32) and then a filler layer of polyurethane foam is placed thereon, feed oxygen into the upstream anaerobic composite bed reactor (4) through the first circulation port (8) and the second circulation port (7) on the upstream anaerobic composite bed reactor (4) so that the dissolved oxygen in the upstream anaerobic composite bed reactor (4) is controlled at 1-3 mg / L; when the membrane volume is 3-5 g: g ° and stabilized, enter nitrogen to convert the previous aerobic environment to an anaerobic environment; (2) transport the feed solution to the upstream anaerobic composite bed reactor (4), controlling its COD = 800-1200 mg / L, pH = 6.5-7.5; The feed solution successively passes through the granular sludge layer (34), the suspended sludge layer (33) and the polyurethane foam filler layer (32) in the upstream anaerobic composite bed reactor (4) and the residence time of the feed solution in the upstream anaerobic composite bed reactor (4) is 22- 26 hours; Then, the antibiotic wastewater is pumped from the water inlet tank (1) to the upstream anaerobic composite bed reactor (4) for anaerobic treatment. The influent water quality of the antibiotic wastewater is CODer = 6400-6600mg / L, and the ammonia nitrogen is 120-130mg / L and pH = 6.5-7.5, and check that the influent flow rate is 0.3-0.5L / h, the organic load is 1-3kgCOD / m'-d, keep water intake for 3-5 hours; The sludge concentration and the membrane volume on the filler layer are periodically checked from the sampling port (31). After the sludge concentration and membrane volume have stabilized, the antibiotic wastewater diluted to various concentrations is transported to the upstream anaerobic composite bed reactor (4). By controlling the COD concentration of the influent water, the gradient of the organic load is increased by 1-2 kgCOD / m2d until the CODcr and ammonia nitrogen removal rate is stable; (3) The anaerobically treated wastewater in (1) is fed to the electrochemical reactor through the first water outlet (6), treated with hydrogen peroxide as a catalyst, and then discharged through the second water outlet (13).
    [2]
    The process for treating antibiotic wastewater according to claim 1, characterized in that: In (1) 1s the height ratio of the granular sludge layer (34) to the suspended sludge layer (33) to the polyurethane foam filler layer (32) 3: 3: 4.
    [3]
    The process for treating antibiotic wastewater according to claim 1, characterized in that: In (1) the height ratio of the granular sludge layer (34) to the upstream anaerobic composite bed reactor (4) is 1: 6.
    [4]
    The process for treating antibiotic wastewater according to claim 1, characterized in that: In (1), feed oxygen into the upstream anaerobic composite bed reactor (4) through the first circulation port (8) and the second circulation port (7) on the upstream anaerobic composite bed reactor (4) so that the dissolved oxygen in the upstream anaerobic composite bed reactor (4) is controlled at 2mg / L; when the membrane volume is 4 µg! and stabilized, introduce nitrogen to convert the previous aerobic environment into an anaerobic environment;
    [5]
    The process for treating antibiotic wastewater according to claim 1, characterized in that: (2) transport the nutrient solution to the upstream anaerobic composite bed reactor (4), controlling its COD = 1000 mg / L, pH = 7. feed solution successively passes through the granular sludge layer (34), the suspended sludge layer (33) and the polyurethane foam filler layer (32) and the residence time of the feed solution in the upstream anaerobic composite bed reactor (4) is 24 hours; Then, the antibiotic wastewater is pumped from the water inlet tank (1) to the upstream anaerobic composite bed reactor (4) for anaerobic treatment. The influent water quality of the antibiotic wastewater is CODcr = 6500 mg / L, and the ammonia nitrogen is 125 mg / L and pH = 7, and control that the influent flow rate is 0.4L / h, the organic load is 1.5kgCOD / m'-d , keep the water intake for 4 hours; The sludge concentration and the membrane volume on the filler layer are periodically checked from the sampling port (31). After the sludge concentration and membrane volume have stabilized, the antibiotic wastewater diluted to various concentrations is transported to the upstream anaerobic composite bed reactor (4). By controlling the COD concentration of the influent water, the gradient of the organic load is increased by 1.5 kgCOD / m3 until the CODer and ammonia nitrogen removal rate is stable.
    [6]
    The process for treating antibiotic wastewater according to claim 1, characterized in that: In (3), the mass concentration of hydrogen peroxide is 26% -30% and the amount thereof is 0.1-0.3% of the volume of the waste water body ,; Preferably in (3), the mass concentration of hydrogen peroxide is 28% and the amount thereof is 0.2% of the volume of the waste water body.
    [7]
    The system for the antibiotic wastewater treatment process according to claim 1, characterized in that: The system comprises a water inlet tank (1), the water inlet tank (1) is connected to the water inlet port (3) of the upstream anaerobic composite bed reactor ( 4) through a pipeline and in the interior of the upstream anaerobic composite bed reactor (4) is a granular sludge layer (34), a suspended sludge layer (33), a filler layer (32) in sequence from bottom to top; There is a sampling port (31) on the left side of the upstream anaerobic composite bed reactor (4), and an outlet port (5) on the top of the upstream anaerobic composite bed reactor (4), and there is a corresponding sealing cover at the outlet port (5) ; On the right side of the lower bottom part of the upstream anaerobic composite bed reactor (4) is the first circulation port (8), and on the right side of the lower middle part of the upstream anaerobic composite bed reactor (4) is the second circulation port (7); The first water outlet (6) in the upper part of the upstream anaerobic composite bed reactor (4) is connected to the electrochemical reactor (12) by a pipeline, and the electrode (11) is located in the electrochemical reactor (12) and the electrode ( 11) is connected to the power supply (10) and on the right side of the electrochemical reactor (12) a second water outlet (13) is provided.
    [8]
    The system for the antibiotic wastewater treatment process according to claim 7, characterized in that: The upstream anaerobic composite bed reactor (4) is a cylindrical plexiglass container with a diameter to height ratio of 1: 6 and a wall to thickness to diameter ratio of 1: 20; The sampling port (31) is located at a height of 2/3 from the top to the bottom of the top end of the upstream anaerobic composite bed reactor (4); The first water outlet (6) is located at a height of 1/12 from the top to the bottom of the right side of the upstream anaerobic composite bed reactor (4); In the center of the top cover of the upstream anaerobic composite bed reactor (4) there is a circular outlet port (5), and the ratio of the diameter of the outlet port (5) to the diameter of the cross section of the upstream anaerobic composite bed reactor (4) is 1: 5.
    [9]
    The system for the antibiotic wastewater treatment process according to claim 7, characterized in that: The electrochemical reactor (12) is a square container having a length, width and height ratio of 16:15:16, and a second water outlet (13) is provided at a height of 1/8 of the electrochemical reactor (12) from bottom to top; The diameter of the outlet pipe connected to the second water outlet (13) is 1/50 of the width of the electrochemical reactor (12) and the length is 2/15 of the width of the electrochemical reactor (12).
    [10]
    The system for the antibiotic wastewater treatment process according to claim 7, characterized in that: The electrode material comprises an anode and a cathode, the anode material being SnO; - Sb / Ti and the cathode being made of a stainless steel material. .
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    同族专利:
    公开号 | 公开日
    CN110255827A|2019-09-20|
    CN110255827B|2021-11-30|
    NL2024125B1|2021-10-12|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    CN201910612343.6A|CN110255827B|2019-07-08|2019-07-08|Antibiotic wastewater treatment process and system|
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