JP4690265B2 - Wastewater treatment method - Google Patents

Description

  The present invention relates to a wastewater treatment method for removing organic matter, nitrogen, phosphorus, and the like from sewage, domestic wastewater, organic industrial wastewater, and the like.

In recent years, eutrophication has become a major problem in closed waters such as lakes and sea bays, and removal of nitrogen and phosphorus that cause this has become important. Therefore, a treatment method capable of removing nitrogen and phosphorus in addition to organic substances has been developed as an improved method of the activated sludge method. As a representative method, A ₂ O method (anaerobic-anoxic-aerobic method), batch The activated sludge method, the intermittent aeration activated sludge method (hereinafter, abbreviated as the intermittent aeration method), and the like are known. In these treatment methods, organic substances, nitrogen, and phosphorus are removed by a biological reaction by microorganisms.

  Here, the principle of the wastewater treatment mainly aimed at removing nitrogen and phosphorus will be briefly explained. The organic matter in the wastewater is decomposed and removed as food of microorganisms constituting the activated sludge. Ammonia nitrogen generated by the decomposition of organic matter is oxidized to nitrate nitrogen by the action of nitrifying bacteria under aerobic conditions (nitrification step). The nitrate nitrogen is reduced to nitrogen gas by the action of denitrifying bacteria under anaerobic conditions and released to the outside air (denitrification step). Therefore, by repeating intermittent aeration, the nitrification step and the denitrification step are alternately performed, and nitrogen in the organic matter is removed.

  Further, dephosphorylated bacteria have the property of absorbing phosphorus under aerobic conditions and releasing phosphorus under anaerobic conditions. Therefore, by alternately changing the operating conditions of the aeration tank between aeration (aerobic conditions) and non-aeration (anaerobic conditions), absorption and release of phosphorus by dephosphorization bacteria are repeated. Phosphorus can be removed by causing the dephosphorizing bacteria to absorb phosphorus and removing the activated sludge containing the dephosphorizing bacteria in which phosphorus has been absorbed as excess sludge from the treatment system.

  Therefore, two aeration tanks that alternately repeat aeration and non-aeration are provided. In the first aeration tank, nitrogen is removed and phosphorus is released. Similarly, in the second aeration tank, nitrogen removal and activated sludge are performed. There is a two-tank intermittent aeration method in which phosphorus is removed by absorbing phosphorus to the activated sludge in the second aeration tank and absorbing phosphorus in a high concentration, and drawing this activated sludge. Proposed.

  Thus, in removing nitrogen and phosphorus, it is indispensable to repeat aerobic conditions and anaerobic conditions. Strictly speaking, anaerobic conditions for denitrification and anaerobic conditions for dephosphorization Is different. That is, under the anaerobic condition caused by the non-aerated state of the intermittent aeration method, the denitrification is completed, the dissolved oxygen in the tank disappears, and after the oxygen molecules due to nitrate nitrogen and nitrite nitrogen disappear, Release of phosphorus from sludge begins. This leads to the absorption of phosphorus in the next aeration process.

  Therefore, in the first aeration tank, phosphorus is effectively released, and in the second aeration tank, phosphorus is effectively absorbed into the activated sludge. It is necessary to set the aeration time and the non-aeration time, and various studies have been made on the setting conditions for the aeration time and the non-aeration time.

  As such a wastewater treatment method, the following Patent Document 1 discloses that wastewater is introduced into a first aeration tank equipped with a first ORP meter and mixed with activated sludge, and aeration and non-aeration are alternately repeated. Then, when the aeration tank is transferred to a second aeration tank equipped with a second ORP meter and aeration and non-aeration are alternately repeated in the second aeration tank, the aeration time for performing aeration in the first aeration tank is Ta. The non-aeration denitrification time is Tb, the end of Tc (= Ta + Tb) is the time when the ORP inflection point is detected by the first ORP meter, and then the non-aeration is further aerated by the second aeration tank. Until the start, phosphorus is released from the activated sludge. In the second aeration tank, the aeration time for aeration is Td, the non-aeration denitrification time is Te, and the end of Tf (= Td + Te) is the second. When the ORP inflection point is detected by the ORP meter Immediately after that, the aeration in the first aeration tank and the second aeration tank are resumed at the same time to absorb phosphorus into the activated sludge, and the membrane separation device installed in the second aeration tank treats the membrane surface only during aeration. Processed water is obtained by separating into water and activated sludge, and part of the activated sludge absorbed and concentrated by phosphorus is removed as excess sludge, and the other part is returned to the first aeration tank. A wastewater treatment method is disclosed.

Further, in Patent Document 2 below, wastewater is allowed to flow into an aeration tank, and after performing treatment by alternately repeating an aerobic state in which aeration is performed and an anaerobic state in which aeration is stopped and agitation is performed, the treated water is supplied. The first aeration tank into which the wastewater flows in the control method of the intermittent aeration activated sludge method that discharges from the final sedimentation basin, returns the sludge to the aeration tank, extracts the excess sludge, and removes nitrogen and phosphorus in the wastewater. And a second aeration tank connected in series to the first aeration tank, an ORP meter is installed in the second aeration tank, and the first aeration tank is aerated for a predetermined time (T _a ). Then, this is stopped and stirring is started. In the second aeration tank, the sum of the aeration time and the stirring time is set to a predetermined time (T _ds ) based on the appearance time of the ORP inflection point of the ORP meter in the previous processing step. Controlled by the first aeration tank set in advance Between de窒時as _{T k} in the agitation _step, to set the respective time _{T a + T k <T ds} , first the transition from the stirring process to the aeration process on the basis of the detection of the ORP bending point of ORP meter, the A control method of an intermittent aeration activated sludge method characterized by performing two aeration tanks simultaneously is disclosed.

Furthermore, the following Patent Document 3 includes a first aeration tank and a second aeration tank connected in series to the first aeration tank, an aerobic state in which aeration of waste water is performed in these two aeration tanks, and aeration is stopped. In the intermittent aeration activated sludge process for removing nitrogen and phosphorus in the waste water by repeating the anaerobic state where stirring is performed, the volume of the first aeration tank is V ₁ , and the second aeration tank V ₂ , anaerobic / aerobic cycle time consisting of aeration and agitation, T _s , T _{a1 for} the aeration time of the first aeration tank within one cycle T _s , and T a for the aeration time of the second aeration tank _a2 , sludge residence time of this process is n days, specific growth rate of nitrifying bacteria is μ, and aeration time ratio r is r = (V ₁ · T _a1 + V ₂ · T _a2 ) / [(V ₁ + V ₂ ) · _{T s]} calculated as, r is greater than 1 / (n · μ), and _{T a1} hours of _{T s} times 1/2 Set T _a1, T _a2 so that the bottom, in the first aeration tank performed after stirring T _a1 hours aeration, in the second aeration tank performed after stirring T _a2 hours aeration, both aeration, the total time of agitation Has disclosed an operation control method for an intermittent aeration activated sludge process characterized in that, when Ts reaches T _s , both the first aeration tank and the second aeration tank are simultaneously shifted from the stirring process to the aeration process.

In Patent Document 4 below, a separation membrane distributes water to be treated into a first treatment tank and performs intermittent aeration treatment to perform nitrification and denitrification, and water in the first treatment tank. The process is led to the second treatment tank installed, nitrified by continuous aeration treatment, suction filtered through the separation membrane, and the membrane permeated water is discharged out of the system, and the water in the second treatment tank And a step of returning a part of the wastewater to the first treatment tank.
Japanese Patent No. 3738377 Patent No. 2803941 Japanese Patent No. 2960273 Japanese Patent No. 3150506

  In the two-tank intermittent aeration method as described above, the treated water treated in the second aerated tank is separated into treated water and activated sludge by a membrane separator (Patent Document 1) or stored in a sedimentation basin. Thus, it is separated into treated water and activated sludge (Patent Documents 2 and 3). The method using the membrane separation apparatus has the advantages that the installation area is small and the amount of excess sludge generated is small compared to the method using the sedimentation basin. However, in the method of Patent Document 1, the aeration of the second aeration tank is performed. Since the discharge from the membrane separator is performed only in time, it is difficult to increase the processing capacity.

  In the method of Patent Document 4, the water in the first treatment tank is guided to the second treatment tank in which the separation membrane is disposed, and nitrification is performed by continuous aeration treatment, and suction is performed through the separation membrane. Filtering and draining the membrane permeate out of the system will not limit the time to collect the membrane permeate, but it is not a two-tank intermittent aeration method, so it is difficult to remove phosphorus There was a problem.

  Furthermore, in order to decompose organic substances and remove nitrogen and phosphorus in the aeration tank, it is necessary to have a certain amount of activated sludge holding microorganisms, but when extracting treated water from the aeration tank Since the activated sludge is also pulled out together, the amount of activated sludge in the aeration tank may be insufficient. For this reason, Patent Documents 2 and 3 disclose that the activated sludge extracted from the second aeration tank and separated in the sedimentation basin is returned to the first aeration tank.

  However, in the two-tank intermittent aeration method, in particular in the wastewater treatment method using the membrane separation device, how to return the activated sludge separated by the membrane separation device has not been studied so far. . Further, in the case of the 2-tank intermittent aeration method, particularly when the activated sludge is returned to the first aeration tank as shown in Patent Documents 2 and 3 in the wastewater treatment method using the membrane separation device, Depending on the case, there is a possibility that the release of phosphorus in the first aeration tank may be hindered.

  Accordingly, an object of the present invention is a two-tank intermittent aeration method, and in the wastewater treatment method using a membrane separator, while maintaining the amount of activated sludge in each aeration tank appropriately, the phosphorus in the first aeration tank It is an object of the present invention to provide a wastewater treatment method in which organic matter, nitrogen and phosphorus in wastewater can be efficiently removed by effectively performing release of phosphorus and absorption of phosphorus in a second aeration tank.

In order to achieve the above object, the waste water treatment method of the present invention uses a first aeration tank and a second aeration tank connected in series to the first aeration tank, and performs aeration of waste water in these two aeration tanks. A wastewater treatment method for removing nitrogen and phosphorus in wastewater by performing intermittent aeration treatment that repeats a state and a state in which aeration is stopped and stirring is performed, and an ORP meter is installed in the first aeration tank, The waste water in the second aeration tank after the intermittent aeration treatment is introduced into a membrane separation device and separated into treated water and concentrated sludge, and the concentrated sludge is returned to the first aeration tank and the second aeration tank, The amount of return to the first aeration tank is made smaller than the amount returned to the second aeration tank, and the concentrated sludge is removed until the ORP value in the first aeration tank shows a bending point at the end of denitrification. Returning to the first aeration tank and the second aeration tank, the ORP value in the first aeration tank is Until turn to increase after showing the points, characterized by returning the concentrated sludge only in the second aeration tank.

According to the wastewater treatment method of the present invention, the sludge concentration in each aeration tank can be increased by returning the concentrated sludge obtained by separation with a membrane separator to the first aeration tank and the second aeration tank. Therefore, the processing efficiency by the intermittent aeration method can be improved. In addition, since the concentrated sludge is often returned to the second aeration tank, the sludge concentration in the second aeration tank is less likely to decrease even if the filtration flux in the membrane separation device is improved. The amount of activated sludge in each of the first aeration tank and the second aeration tank is appropriately maintained, and the treatment efficiency of the entire wastewater treatment can be improved. Furthermore, since the amount of return of the concentrated sludge to the first aeration tank is reduced, the influence on the phosphorus release in the first aeration tank is reduced, and the release of phosphorus in the first aeration tank and the second aeration tank It is possible to effectively absorb phosphorus. In addition, when the ORP value in the first aeration tank indicates the bending point at the end of denitrification, dissolved oxygen, nitrite nitrogen, and nitrate nitrogen are not present in the first aeration tank. Furthermore, phosphorus release is achieved by maintaining. Therefore, after the ORP value in the first aeration tank shows the bending point at the end of denitrification, the concentrated sludge is not returned to the first aeration tank, but only to the second aeration tank. The phosphorus release in the first aeration tank can be effectively performed.

  In the wastewater treatment method of the present invention, it is preferable that the concentrated sludge is introduced into a retention tank to reduce dissolved oxygen in the concentrated sludge and then returned to the first aeration tank and the second aeration tank. Even under anaerobic conditions, dephosphorylated bacteria absorb phosphorus when dissolved oxygen, nitrite nitrogen, or nitrate nitrogen is present, and dissolved oxygen, nitrate nitrogen, and nitrate nitrogen Release phosphorus only if not present. For this reason, when dephosphorization bacteria are releasing phosphorus in the first aeration tank, returning concentrated sludge containing dissolved oxygen or the like will inhibit phosphorus release by the dephosphorization bacteria, and the first aeration tank. In some cases, phosphorus does not move effectively from the first to the second aeration tank. According to the above aspect, by removing the dissolved oxygen in the concentrated sludge to be returned to the aeration tank, the release of phosphorus in the first aeration tank becomes difficult to be inhibited, and the phosphorus in the first aeration tank Release can be effected effectively.

  Further, in the wastewater treatment method of the present invention, the first aeration tank is in a state where aeration is stopped, and dissolved oxygen, nitrite nitrogen and nitrate nitrogen are not present in the first aeration tank. The concentrated sludge is preferably returned only to the second aeration tank. As described above, the release of phosphorus in the first aeration tank is performed only in the anaerobic state when dissolved oxygen, nitrite nitrogen, and nitrate nitrogen are not present. When concentrated sludge containing oxygen or the like is returned to the first aeration tank, phosphorus release by dephosphorizing bacteria is inhibited. Therefore, when the first aeration tank is in a state where aeration is stopped and dissolved oxygen, nitrite nitrogen and nitrate nitrogen are not present in the first aeration tank, the concentrated sludge is used only in the second aeration tank. By returning to the first aeration tank and not returning it to the first aeration tank, it is possible to effectively release phosphorus in the first aeration tank. In addition, by returning more concentrated sludge containing dissolved oxygen to the second aeration tank, the nitrification process and the denitrification process are promoted, and the absorption of phosphorus into the activated sludge is promoted. , Phosphorus can be removed more effectively.

  Further, in the wastewater treatment method of the present invention, an ORP meter is installed in the first aeration tank, and the concentrated sludge is added until the ORP value in the first aeration tank shows a bending point at the end of denitrification. Return to the first aeration tank and the second aeration tank, and return the concentrated sludge only to the second aeration tank until the ORP value in the first aeration tank shows an inflection point and then starts to increase. It is preferable. If the ORP value in the first aeration tank shows the inflection point at the end of denitrification, the dissolved oxygen, nitrite nitrogen, and nitrate nitrogen are not present in the first aeration tank, so the anaerobic state is further maintained. By doing so, phosphorus is released. Therefore, after the ORP value in the first aeration tank shows the inflection point at the end of denitrification, the concentrated sludge is not returned to the first aeration tank, but is returned only to the second aeration tank. It is possible to effectively release phosphorus in the aeration tank.

  According to the wastewater treatment method of the present invention, the concentrated sludge obtained by separation with the membrane separation device is returned to the first aeration tank and the second aeration tank, and is often returned to the second aeration tank. Even if the filtration flux in the membrane separation device is improved, the sludge concentration in the second aeration tank becomes difficult to decrease, and the amount of activated sludge in each of the first aeration tank and the second aeration tank is appropriately maintained, and the wastewater treatment. Overall processing efficiency can be improved. Furthermore, since the amount of return of the concentrated sludge to the first aeration tank is reduced, the influence on the phosphorus release in the first aeration tank is reduced, and the release of phosphorus in the first aeration tank and the second aeration tank Phosphorus can be effectively removed by removing excess sludge from the second aeration tank.

  In the present invention, wastewater to be treated is not particularly limited as long as it contains nitrogen and phosphorus. For example, household wastewater, cereal starch manufacturing industry, dairy manufacturing industry, meat center, sugar manufacturing industry, livestock food Wastewater from food manufacturing industry, livestock farming, meat product manufacturing industry, meat ham / sausage manufacturing industry, fish paste product manufacturing industry, fishery food product manufacturing industry, organic chemical industry manufacturing industry, inorganic chemical industry manufacturing industry, etc.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings. FIG. 1 shows an example of a wastewater treatment apparatus for carrying out a wastewater treatment method according to an embodiment of the present invention. In FIG. 1, the paths of drainage, air, and concentrated sludge (activated sludge) are represented by solid arrows.

  The waste water treatment apparatus used in the waste water treatment method of the present invention mainly includes a first aeration tank 10, a second aeration tank 20 connected in series to the first aeration tank 10, and activated sludge taken out from the second aeration tank 20 to concentrate permeate water. It is comprised with the membrane separation apparatus 30 isolate | separated into sludge (activated sludge).

  A drainage supply pipe L1 connected to a drainage supply device (not shown) is connected to the first aeration tank 10. An air diffuser 11a is disposed at the bottom of the first aeration tank 10, and a pipe L7 connected to the blower 13 is connected to the air diffuser 11a via a valve 12a. The blower 13, the pipe L <b> 7, the valve 12 a, and the aeration device 11 a constitute an aeration device for the first aeration tank 10. A stirring motor 15a is installed above the first aeration tank 10, and a stirring blade 14a is provided at the lower end of the stirring shaft 17a that extends downward from the stirring motor 15a and is inserted into the first aeration tank 10. It is installed. The stirring motor 15a, the stirring shaft 17a, and the stirring blade 14a constitute a stirrer of the first aeration tank 10. Further, in the first aeration tank 10, a first ORP meter 16a for measuring an oxidation-reduction potential (ORP) of waste water stored in the tank is installed. The first aeration tank 10 is connected to the second aeration tank 20 via a pipe L8.

  The second aeration tank 20 basically has the same structure as the first aeration tank 10. That is, an air diffuser 11b is disposed at the bottom of the second aeration tank 20, and a pipe L7 connected to the blower 13 is connected to the air diffuser 11b via a valve 12b. The blower 13, the pipe L <b> 7, the valve 12 b, and the aeration device 11 b constitute an aeration device for the second aeration tank 20. A stirring motor 15b is installed above the second aeration tank 20, and a stirring blade 14b is provided at the lower end of the stirring shaft 17b extending downward from the stirring motor 15b and inserted into the second aeration tank 20. It is installed. The stirring motor 15b, the stirring shaft 17b, and the stirring blade 14b constitute a stirrer of the second aeration tank 20. Further, in the second aeration tank 20, a second ORP meter 16b that measures the oxidation-reduction potential (ORP) of the wastewater stored in the tank is installed.

  On the other hand, the membrane separation device 30 includes an activated sludge inlet 31, an activated sludge outlet 32, and a treated water outlet 33.

  The activated sludge inlet 31 is connected to the lower side of the second aeration tank 20 via a pipe L2 in which the extraction pump P1 is arranged. A pipe L9 connected to the blower 13 is connected in the middle of the pipe L2.

  A pipe L3 is connected to the activated sludge discharge port 32. This pipe L3 is connected to the first aeration tank 10 via a valve 34 and is connected to the second aeration tank 20 via a valve 35. ing. The pipe L3 and the valves 34 and 35 form a return path for the concentrated sludge to the first aeration tank 10 and the second aeration tank 20.

  A pipe L5 in which a suction device 36 is disposed is connected to the treated water discharge port 33.

  The membrane used for the membrane separation device 30 can be appropriately selected from general filtration membranes. For example, microfiltration membranes (MF membranes), ultrafiltration membranes (UF membranes), nanofiltration membranes (NF membranes) Etc. Moreover, there is no limitation in particular as a form of the membrane separation apparatus 30, A hollow fiber membrane module, a flat membrane type module, a spiral type module, a tube type module etc. can be used.

  As the suction device 36, a pump is used in this embodiment, but siphon suction or the like can also be used.

  Next, the waste water treatment method of the present invention using this waste water treatment apparatus will be described.

  The waste water to be treated is introduced into the first aeration tank 10 from the waste water supply device (not shown) via the waste water supply pipe L1, mixed with the activated sludge in the tank, and intermittent aeration processing is performed in which aeration and non-aeration are repeated alternately. . A part of the wastewater treated in the first aeration tank 10 is sent to the second aeration apparatus 20 through the pipe L8, and intermittent aeration processing is performed in the second aeration tank 20 to alternately repeat aeration and non-aeration again. The aeration process in each of the aeration tanks 10 and 20 is performed by opening the valves 12a and 12b and supplying a gas containing oxygen (usually air) from the blower 13 from the air diffusers 11a and 11b. Further, when not aerated, the blower 13 is stopped, the valves 12a and 12b are closed, the stirring motors 15a and 15b are operated, and the stirring blades 14a and 14b are rotated to stir the inside of the tank. Make sure that the sludge in the tank does not settle. However, when the activated sludge concentration in the aeration tanks 10 and 20 is high, the activated sludge is difficult to settle, and therefore stirring by the stirring blades 14a and 14b may not be particularly required.

  During the aeration treatment in each of the aeration tanks 10 and 20, the inside of the tank is in an aerobic state, decomposition of organic matter by microorganisms proceeds, and ammonia nitrogen generated by the decomposition of organic matter is sublimated by nitrite bacteria and nitrate bacteria. It is converted into nitric acid and nitric acid (nitrification process). Further, phosphorus is absorbed by the dephosphorizing bacteria in the activated sludge. On the other hand, in the non-aerated state in which aeration in each of the aeration tanks 10 and 20 is stopped, the inside of the tank becomes anaerobic, decomposition of organic substances by microorganisms proceeds, and nitrous acid and nitric acid formed in the aerobic state are removed. It is reduced to nitrogen by the action of nitrogen bacteria and released to the outside air (denitrification process). And in the anaerobic state, when the said denitrification process is complete | finished and it will be in the state which does not have dissolved oxygen, nitrite nitrogen, and nitrate nitrogen in a tank, release | release of phosphorus by a dephosphorization bacterium will be performed.

  Therefore, in the present invention, in the first aeration tank 10, the nitrification process and the denitrification process are completed, and the non-aerated state is maintained until the phosphorus absorbed by the dephosphorizing bacteria is released, so that the second aeration is performed. In the tank 20, the aeration time and the non-aeration time in each tank are controlled so that the aeration process is started again before the nitrification process and the denitrification process are completed and phosphorus absorbed by the dephosphorizing bacteria is released. To do. As a method for controlling such aeration time and non-aeration time, Patent Document 1 (Patent No. 3738377), Patent Document 2 (Patent No. 2803394), and Patent Document 3 (Patent No. 2960273) described above. The described method can be employed.

  For example, when the method described in Japanese Patent No. 3738377 is adopted, in the first aeration tank 10, the aeration time for aeration is Ta, the non-aeration denitrification time is Tb, and Tc (= Ta + Tb) The end time is defined as the time point when the ORP inflection point is detected by the first ORP meter, and then the non-aeration is continued until the second aeration tank 20 starts aeration to release phosphorus from the activated sludge. 2 In the aeration tank 20, when the aeration time for aeration is Td, the denitrification time for non-aeration is Te, and when the end of Tf (= Td + Te) is detected by the second ORP meter, the ORP inflection point is detected Then, the process of restarting the aeration of the first aeration tank 10 and the second aeration tank 20 at the same time may be repeated immediately thereafter.

  As a result, in the first aeration tank 10, the nitrification process is performed at the aeration time Ta, the denitrification process is performed at the non-aeration time Tb, and the dephosphorization bacteria are used until the aeration is started again after the Tc time has elapsed. The absorbed phosphorus will be released. Further, in the second aeration tank 20, a nitrification process is performed at the aeration time Tb, and a denitrification process is performed at the non-aeration time Te, and the dephosphorizing bacteria are in a state of absorbing and holding phosphorus during these processes. Then, the phosphorus released in the first aeration tank 10 is absorbed into the activated sludge of the second aeration tank 20 by simultaneously restarting the aeration of the first aeration tank 10 and the second aeration tank 20 after the time Tf has elapsed. The phosphorus can be removed by extracting the activated sludge from the second aeration tank 20.

  Under general conditions, when one cycle is 2 hours, the aeration time (aerobic) in the first aeration tank 10 is about 30 minutes, and then the oxygen-free time (denitrification of nitrous acid and nitrate nitrogen) Time) is about 30 minutes, and finally the anaerobic time (phosphorus release) is about 60 minutes. Although it depends on the water quality and temperature, the aeration time and the non-aeration time can be determined based on this by further adjusting while driving to obtain appropriate conditions.

  Moreover, if the method described in Patent Document 3 (Japanese Patent No. 2960273) is adopted, the first ORP meter 16a provided in the first aeration tank 10 and the second ORP meter provided in the second aeration tank 20 are used. It is also possible to control the aeration time and the non-aeration time by timer control without performing control by 16b or the like.

  After the waste water is intermittently aerated in each aeration tank as described above, the treated waste water containing activated sludge in the second aeration tank 20 (hereinafter referred to as treated waste water) is drawn from the pipe L2 by the pump P1, and the membrane Supply to separation device 30. Then, the air from the blower 13 is introduced into the membrane separation device 30 through the pipes L9 and L2 as air lift air, and the supplied treated waste water is passed through the membrane separation device 30. The membrane-filtered treated water is sucked by the suction device 36, separated into concentrated sludge (activated sludge) and treated water, and the treated water is drawn out of the system from the pipe L5.

The filtration conditions in the membrane separation device 30 are not particularly limited because they vary depending on the type of membrane, the sludge concentration in the treated wastewater, etc. For example, a tubular made of polyvinylidene fluoride (PVDF) having an inner diameter of 5-10 mm When the membrane is used as a module, the filtration flux of the treated wastewater is preferably about 1 m ³ / m ² days. When a vertical membrane module installed outside the tank is used as the membrane separator 30, the height is preferably about 3 to 4 m. In this case, it is preferable that the flow rate of the treated waste water drawn out from the pump P1 is about 0.5 m / second, and the flow rate ratio between the treated waste water and the air lift air is about 1: 1. According to this, the air lift effect can be used effectively.

  In addition, as the filtration treatment is performed in the membrane separation device 30 for a long period of time, the filtration treatment efficiency may be reduced. Therefore, the backwash water is supplied to the secondary side of the membrane at a frequency of about once every 10 minutes. It is preferable to perform backwashing that flows from the (treated water discharge side) to the primary side (active sludge flow path side). For long-term membrane fouling and clogging, fill the secondary side of the membrane with chemicals such as sodium hypochlorite and citric acid, and hold the membrane for 1-2 hours while immersed in these chemicals. It is preferable to perform the chemical cleaning to be performed about once a month.

  The concentrated sludge (activated sludge) discharged from the membrane separation device 30 is returned to the first aeration tank 10 and the second aeration tank 20 through the pipe L3 and the valves 34 and 35. At this time, the return amount of the concentrated sludge (activated sludge) to the first aeration tank 10 is made smaller than the return amount to the second aeration tank 20.

  Specifically, concentrated sludge (activated sludge) of 1 to 5 times the amount of inflow of wastewater into the first aeration tank 10 is returned to the first aeration tank 10, and the second aeration tank 20 is supplied with the first aeration tank 10. It is preferable to return concentrated sludge (activated sludge) in an amount 10 to 20 times the amount of inflow of wastewater into one aeration tank 10. As described above, in the membrane separator 30, treated water is obtained by filtering the treated wastewater in the second aeration tank 20, but in order to improve wastewater treatment efficiency, It is necessary to increase the filtration flux. Since the treated wastewater contains a large amount of activated sludge in the tank, if the filtration flux is increased, the sludge concentration in the second aeration tank 20 tends to decrease. For this reason, in order not to reduce the sludge concentration in the second aeration tank 20, it is necessary to circulate the concentrated sludge (activated sludge) between the second aeration tank 20 and the membrane separation device 30. 2 The amount of return of concentrated sludge (activated sludge) to the aeration tank 20 is made larger than the amount of return to the first aeration tank 10. On the other hand, in the 1st aeration tank 10, since the activated sludge in a tank does not flow out so much, the return amount of the grade which maintains the sludge density | concentration in a tank may be sufficient, and 1 to 2 times the inflow amount of waste_water | drain is more. preferable.

  By adjusting the return amount in this way, the sludge concentration in each aeration tank can be maintained at 8000 to 20000 mg / L. Moreover, if the difference between the activated sludge concentration in the first aeration tank 10 and the activated sludge concentration in the second aeration tank 20 is too large, it is not preferable from the viewpoint of operation management and processing performance, and the difference is 5000 mg / L or less. It is preferable to adjust so that it becomes.

  Thus, the amount of return of the concentrated sludge (activated sludge) discharged from the membrane separation device 30 is reduced to the first aeration tank 10 and increased to the second aeration tank 20, so that the inside of each aeration tank 10, 20 The amount of activated sludge can be maintained at an appropriate amount, and the wastewater can be treated efficiently by promoting the decomposition, denitrification and dephosphorization of organic substances by microorganisms. In addition, by reducing the return amount of the concentrated sludge to the first aeration tank 10, it is possible to suppress adverse effects on the phosphorus release in the first aeration tank 10, so that phosphorus release in the first aeration tank 10, The phosphorus absorption in the 2nd aeration tank 20 can be performed effectively, and the phosphorus in waste_water | drain can be removed efficiently.

  In the present invention, when the first aeration tank 10 is in a state where aeration is stopped and dissolved oxygen, nitrite nitrogen, and nitrate nitrogen are not present in the first aeration tank 10, the valve It is preferable to close 34 and open only the valve 35 and return the concentrated sludge (activated sludge) only to the second aeration tank 20. When the first aeration tank 10 is in a state where aeration is stopped and dissolved oxygen, nitrite nitrogen and nitrate nitrogen are not present in the first aeration tank 10, the first aeration tank 10 contains phosphorus. Since it is in a released state, if the concentrated sludge containing dissolved oxygen or the like is returned to the first aeration tank 10 at this time, the release of phosphorus in the first aeration tank 10 is hindered, and the second aeration tank 20 The transfer of phosphorus to is not done effectively. Accordingly, when the first aeration tank 10 is in a state where aeration is stopped and dissolved oxygen, nitrite nitrogen and nitrate nitrogen are not present in the first aeration tank 10, concentrated sludge (activated sludge). Is returned only to the second aeration tank 20 and is not returned to the first aeration tank 10, thereby promoting the release of phosphorus in the first aeration tank 10, and the phosphorus to the second aeration tank 20. Transition can be done effectively.

  In addition, when the 1st aeration tank 10 is in the state which stopped aeration, and dissolved oxygen, nitrite nitrogen, and nitrate nitrogen do not exist in the 1st aeration tank 10, concentrated sludge (activated sludge) Various methods can be adopted as a method of returning the air to the second aeration tank 20 only and not returning it to the first aeration tank 10, for example, the method described in Japanese Patent No. 3738377 When the aeration time and the non-aeration time are controlled by, for example, until the ORP value by the first ORP meter 16a installed in the first aeration tank 10 indicates the bending point of the denitrification end, After returning to the 1 aeration tank 10 and the 2nd aeration tank 20, and the ORP value in the 1st aeration tank 10 shows the bending point, by the aeration simultaneous restart in the 1st aeration tank 10 and the 2nd aeration tank 20 Until it starts to increase, concentrate the sludge only in the second aeration tank 20 It is sufficient to return.

  And if wastewater is processed by such an activated sludge method, since the amount of activated sludge accumulated in the system gradually increases, a part of the activated sludge in the second aeration tank 20 or the membrane separation device 30 separates it. A portion of the concentrated sludge is extracted as excess sludge. The sludge extracted in this manner contains a high concentration of phosphorus absorbed by the dephosphorization bacteria. As a result, phosphorus is removed from the waste water, so that organic matter is decomposed in the treated water flowing out through the pipe L5. Nitrogen and phosphorus are removed to form purified water. Further, the concentrated sludge extracted as excess sludge can be composted by a known means and used as a fertilizer rich in nitrogen and phosphorus.

  FIG. 2 shows an example of a wastewater treatment apparatus for carrying out a wastewater treatment method according to another embodiment of the present invention. In addition, the same code | symbol is attached | subjected to the same part as the waste water treatment apparatus of the said embodiment, and the description is abbreviate | omitted.

  In the wastewater treatment apparatus of this embodiment, the pipe L6 arranged at the activated sludge discharge port 32 of the membrane separation apparatus 30 is connected to the staying tank 40, and the concentrated sludge (activated sludge) treated in the staying tank 40 is piped. The point which is comprised so that it may return to the 1st aeration tank 10 and the 2nd aeration tank 20 through L3 and the valves 34 and 35 is different from the waste water treatment apparatus of the said embodiment. Other configurations are the same as those of the above embodiment.

  As the retention tank 40, for example, a round or square tank structure provided with a short-circuit prevention structure (baffle plate, height difference, etc.) so that the flow does not short-circuit between the inflow portion and the outflow portion of the concentrated sludge. A thing having can be adopted.

  The residence time of the concentrated sludge (activated sludge) in the residence tank 40 depends on temperature, dissolved oxygen concentration, etc., but 1 to 5 minutes is preferable. According to this, since the dissolved oxygen concentration can be made almost zero, organic substances, phosphorus and nitrogen in the waste water can be efficiently removed.

  In this embodiment, the concentrated sludge (activated sludge) obtained by filtering the treated wastewater with the membrane separator 30 is stored in the retention tank 40 for a predetermined time, and dissolved oxygen is generated by the respiration action of microorganisms in the retention tank. After the reduction or removal, it is returned to the first aeration tank 10 and the second aeration tank 20.

  Thus, by returning the concentrated sludge (activated sludge) from which dissolved oxygen has been reduced or removed, adverse effects on phosphorus release in the first aeration tank 10 are reduced. For this reason, for example, the return timing and return destination of the concentrated sludge (activated sludge) obtained by filtering the treated wastewater with the membrane separator 30 are not particularly controlled, and the first aeration tank 10 and the second aeration tank 20 are controlled. Even when it is always returned at a predetermined rate, the release of phosphorus in the first aeration tank 10 is not so hindered, and the movement of phosphorus to the second aeration tank 20 and the absorption and removal of phosphorus in the second aeration tank 20 Can be done effectively.

  However, also in this embodiment, as described above, the first aeration tank 10 is in a state in which aeration is stopped, and dissolved oxygen, nitrite nitrogen, and nitrate nitrogen are contained in the first aeration tank 10. Of course, it is more preferable to return the concentrated sludge (activated sludge) only to the second aeration tank 20 and not to return it to the first aeration tank 10 in the case where there is not.

It is a schematic block diagram which shows an example of the waste water treatment apparatus for enforcing the waste water treatment method by one Embodiment of this invention. It is a schematic block diagram which shows an example of the waste water treatment apparatus for enforcing the waste water treatment method by other embodiment of this invention.

Explanation of symbols

10: 1st aeration tank 11a, 11b: Air diffuser 12a, 12b, 34, 35: Valve 13: Blower 14a, 14b: Agitation blade 15a, 15b: Agitation motor 16a: 1st ORP meter 16b: 2nd ORP Total 17a, 17b: Stirrer shaft 20: Second aeration tank 30: Membrane separation device 31: Activated sludge inlet 32: Activated sludge outlet 33: Treated water outlet 36: Suction device 40: Residence tank

Claims (3)

Using the first aeration tank and the second aeration tank connected in series to the first aeration tank, in these two aeration tanks, the state in which the aeration of the waste water is aerated and the state in which the aeration is stopped and the agitation is performed are repeated. A wastewater treatment method for removing nitrogen and phosphorus in wastewater by performing intermittent aeration treatment,
An ORP meter is installed in the first aeration tank,
The waste water in the second aeration tank after the intermittent aeration treatment is introduced into a membrane separation device and separated into treated water and concentrated sludge, and the concentrated sludge is returned to the first aeration tank and the second aeration tank, The return amount to the first aeration tank is less than the return amount to the second aeration tank ,
The concentrated sludge is returned to the first aeration tank and the second aeration tank until the ORP value in the first aeration tank indicates the bending point at the end of denitrification, and the ORP value in the first aeration tank is The wastewater treatment method is characterized in that the concentrated sludge is returned only to the second aeration tank until it starts to increase after showing the bending point .   The wastewater treatment method according to claim 1, wherein the concentrated sludge is introduced into a retention tank to reduce dissolved oxygen in the concentrated sludge and then returned to the first aeration tank and the second aeration tank.   When the first aeration tank is in a state where aeration is stopped and dissolved oxygen, nitrite nitrogen and nitrate nitrogen are not present in the first aeration tank, the concentrated sludge is used only in the second aeration tank. The wastewater treatment method according to claim 1 or 2, wherein the wastewater treatment method is returned to the factory.