JP4508694B2 - Water treatment method and apparatus - Google Patents

Description

  The present invention relates to a water treatment method and apparatus, and relates to a water treatment technique for removing contaminants from sewage, industrial wastewater, domestic wastewater, and the like.

  Conventionally, there is a batch activated sludge method as a method of performing denitrification treatment in water treatment. This is to store sewage (sewage) such as sewage, industrial wastewater, domestic wastewater in an aeration tank, purify the sewage by aeration in the aeration tank for a certain period of time, then stop the aeration and precipitate activated sludge. The low-concentration liquid (treated water) is taken out, and the sewage is newly introduced into the tank with the precipitate (concentrated sludge) remaining in the tank. The aeration tank and the precipitation tank are combined into one tank. .

  Further, there is a membrane separation activated sludge method as a continuous activated sludge method. For example, as shown in FIG. 11, liquids to be treated such as sewage, industrial wastewater, and domestic wastewater are introduced into a reaction tank 31 that forms a first tank, thereby forming a second tank that also serves as a separate reaction tank. The mixed liquid in the tank is circulated between the membrane separation tank 32 and the reaction tank 31.

  When the reaction tank 31 is an oxygen-free tank, the organic nitrogen or ammonia in the liquid to be treated is oxidized to nitrate nitrogen and nitrite nitrogen by nitrification reaction in the membrane separation tank 32, and denitrified in the reaction tank 31. Nitrate nitrogen and nitrite nitrogen are reduced to nitrogen by the reaction to remove nitrogen from the water environment. When the reaction tank 31 is an anaerobic tank, phosphorus is released from the activated sludge in the reaction tank 31, and the activated sludge ingesting phosphorus is taken out in the membrane separation tank 32 to remove phosphorus from the water environment.

Further, in the membrane separation tank 32, the aeration air diffused from the air diffuser 33 generates an upward flow of the solid-gas / liquid mixed phase, and the mixed liquid in the tank is supplied to the membrane separation apparatus 34 by the cross flow by the upward flow. The mixed liquid in the tank is solid-liquid separated while performing surface cleaning, the membrane filtrate is taken out of the tank, and the activated sludge is kept at a high concentration by retaining the separated activated sludge in the tank.
JP 2002-346585 A Japanese Patent Laid-Open No. 7-241596

  In the batch activated sludge method, generally, the sludge concentration in the tank is about 5 g / L and the reaction rate is low, so the tank volume becomes large. If the sludge concentration in the tank is kept at a high concentration, the reaction rate increases. However, if the sludge concentration increases, precipitation concentration becomes difficult, and the efficiency of dissolving oxygen dissolved in the tank mixture by aeration decreases.

  Further, in the batch activated sludge method, it is difficult to remove the soluble substance (colloidal substance) from the water environment by using a flocculant, not by decomposition, and it is necessary to use a large amount of the flocculant. .

  In the membrane separation activated sludge method, there are many pollutants in the liquid to be treated (the load is high), and the sludge concentration in the tank mixture is high and contains a lot of membrane pollutants (such as adhesive substances discharged by microorganisms). In addition, increasing the sludge concentration has the advantage of increasing the reaction rate due to microorganisms, but membrane contaminants can clog the pores of the membrane, causing clogging, increasing the number of backwash operations and lowering the operating rate. There is a dilemma to do.

  In the membrane-separated activated sludge method, biological treatment is carried out in an almost completely mixed state, so that a short-circuit flow is likely to occur, and there are problems such as a large tank or multiple stages to ensure a sufficient reaction time.

  Patent Document 1 sets each cycle of waste water input-aeration-precipitation-processed water discharge sequentially as one cycle, and sets the operation time of one cycle of a batch type reaction tank that repeats this cycle to 5 hours or less. A pair of reaction tanks are operated with a time difference, and the treated water discharged from these reaction tanks is directly guided to a common membrane separation tank for filtration, but the sludge concentration in each reaction tank is small, The capacity is large.

  Patent Document 2 discloses that the water to be treated in the submerged membrane module biological treatment tank is stirred to form an anaerobic state, and denitrification is performed by denitrifying bacteria in the anaerobic state, and the submerged membrane module Water to be treated in a biological treatment tank is aerated to form an aerobic atmosphere, and nitrification is performed by a short cycle batch activated sludge method with nitrifying bacteria in the aerobic atmosphere. According to this configuration, the sludge concentration in the tank can be maintained at a high concentration, but the problem of membrane surface contamination accompanying the increase in concentration has not been solved.

  The present invention solves the above-mentioned problems, and maintains a high concentration of microorganisms (activated sludge), shortens the reaction time, and can easily follow the flow rate fluctuation of the inflow amount. It is an object of the present invention to provide a water treatment method and apparatus that efficiently removes pollutants in waste water.

  In order to solve the above-mentioned problem, the water treatment method of the present invention described in claim 1 is a batch-type activated sludge treatment of a liquid to be treated in a batch-type reaction tank, and a low-concentration liquid in the batch-type reaction tank is subjected to a second reaction. Supplying to the tank, treating the membrane separation activated sludge while circulating the mixed liquid in the second reaction tank with the membrane separation tank, and returning the mixed liquid in the second reaction tank to the batch reaction tank It is.

  With the configuration described above, the batch type reaction tank removes pollutant components that are likely to settle in the liquid to be treated by batch activated sludge treatment, and returns the mixed liquid in the tank having a high sludge concentration from the second reaction tank to return the sludge concentration. To increase the biological response.

  For this reason, the low-concentration liquid in the batch-type reaction tank flowing into the second reaction tank and the membrane separation tank has a low pollution load and a low sludge concentration, and the membrane filtrate is taken out by membrane separation. Even if it is concentrated, the membrane contaminants in the mixed liquid in the tank circulating between the second reaction tank and the membrane separation tank are reduced, and the sludge concentration is not too high.

This makes it possible to increase the oxygen dissolution efficiency while suppressing membrane surface clogging due to membrane contaminants and sludge and to treat membrane-separated activated sludge that is difficult to separate by precipitation flowing from the batch reaction tank.
The water treatment method of the present invention described in claim 2 forms a sludge concentration gradient in the water depth direction in the second reaction tank, and sends the mixed liquid in the tank having a low sludge concentration at a low depth to the membrane separation tank. The mixture in the tank having a high sludge concentration under deep water is returned to the batch reaction tank.

With the above configuration, a sludge concentration difference is formed in the second reaction tank and the membrane separation tank in which the mixed liquid in the tank circulates, and the sludge concentration in the mixed liquid in the tank returned from the second reaction tank to the batch reaction tank is increased. As a result, the sludge concentration in the batch reactor is further increased, and the sludge concentration in the membrane separation tank is optimized by reducing the sludge concentration in the tank mixture sent from the second reaction tank to the membrane separation tank. The efficiency is further increased, and further suppression of membrane surface blockage can be realized.
In the water treatment method of the present invention described in claim 3, the liquid to be treated is treated in a batch-type activated sludge in a batch-type reaction tank, and the low-concentration liquid in the batch-type reaction tank is supplied to the membrane separation tank. The mixed liquid in the tank that has been treated and concentrated in the membrane separation tank is returned to the batch reaction tank.

  The water treatment method of the present invention described in claim 4 is a batch-type reaction tank, an anaerobic stirring process performed while supplying the liquid to be treated, an aerobic reaction process performed while aeration of the mixed liquid in the tank, and agglomeration An agitation and precipitation process in which an agent is added and allowed to stand after agitation, and a transfer process in which the precipitated and separated low-concentration liquid is fed to the next tank are sequentially performed.

  The water treatment device of the present invention described in claim 5 is a batch type reaction tank for treating a liquid to be treated in a batch activated sludge, a second reaction tank for storing a low concentration liquid in the batch type reaction tank, and an immersion type membrane. A membrane separation tank having a separation device for treating the mixed liquid in the tank of the second reaction tank with membrane separation activated sludge; a first liquid feeding system for feeding a low concentration liquid of the batch reaction tank to the second reaction tank; A first return system for returning the liquid mixture in the tank of the second reaction tank to the batch reaction tank, a second liquid supply system for supplying the liquid mixture in the tank of the second reaction tank to the membrane separation tank, and membrane separation And a second return system that returns the mixed liquid in the tank to the second reaction tank.

  The water treatment apparatus of the present invention described in claim 6 has a batch type reaction tank for treating the liquid to be treated in a batch type activated sludge, and a submerged type membrane separation apparatus for membrane separation of a low concentration liquid in the batch type reaction tank. A membrane separation tank for activated sludge treatment, a liquid feed system for feeding a low concentration liquid in a batch reaction tank to the membrane separation tank, and a return system for returning the mixed liquid in the tank of the membrane separation tank to the batch reaction tank. It is what you have.

  As described above, according to the present invention, the batch activated sludge treatment step and the membrane separation activated sludge treatment step are sequentially performed, and the mixed liquid in the tank concentrated in the membrane separation activated sludge treatment step is returned to the batch activated sludge treatment step. By doing so, it is possible to realize a biological reaction under a high sludge concentration in the batch reaction tank and a reduction in the tank volume, and to improve the oxygen dissolution efficiency in the membrane separation tank and to suppress the membrane surface clogging.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings. This embodiment is an example of treatment of organic wastewater containing BOD and nitrogen. 1 to 4, the batch-type reaction tank 1 has a flow rate adjusting tank 2 as a front tank, and the flow rate adjusting tank 2 communicates with a liquid supply system 3 to be processed into which the liquid to be processed flows. A liquid feed system 4 to be treated having a pump for supplying the treatment liquid to the batch reaction tank 1 is provided.

  The batch reaction tank 1 is connected with a chemical supply system 5 for supplying a coagulant such as an organic polymer and coagulant, and an aeration tube 7 connected to a blower 6 and a stirrer 8 are arranged. Is provided with a pump for supplying the second reaction tank 9 to the second reaction tank 9, and a sludge extraction system 11 is provided at the bottom of the tank.

  The second reaction tank 9 that stores the low-concentration liquid in the batch reaction tank 1 is provided with a first return system 12 that returns the mixed liquid in the tank to the batch reaction tank 1, and an air diffuser 14 connected to the blower 13. And a stirrer 15 are provided, and a second liquid feeding system 17 having a pump for supplying the mixed liquid in the tank to the membrane separation tank 16 of the next tank is provided.

  The membrane separation tank 16 for treating the mixed liquid in the second reaction tank 9 with membrane separation activated sludge is provided with a second return system 18 for returning the mixed liquid in the tank to the second reaction tank 9 under natural flow, and is immersed A mold membrane separator 19 is disposed, and a sludge extraction system 20 is provided at the bottom of the tank.

  The submerged membrane separation device 19 has a membrane filling unit 21, a suction pump 22 that applies driving pressure (transmembrane differential pressure) is connected to the membrane filling unit 21, and an air diffuser 23 is disposed below the membrane filling unit 21. The blower 24 is connected to the air diffuser 23. The membrane filling unit 21 is composed of membrane cartridges arranged in parallel with a predetermined gap. Each membrane cartridge has organic flat membranes arranged on both sides of the filter plate, and the membrane surfaces are arranged along the vertical direction. . A ceramic membrane, a hollow fiber membrane, or a tubular membrane can be used for the membrane filling portion 21.

  In the configuration described above, each tank body does not have to be an independent separate body, and can be configured by partitioning one tank body with a wall body. It is also possible to use these means.

  Hereinafter, the operation of the above-described configuration will be described. First, the batch activated sludge treatment in the batch reaction tank 1 will be described. As shown in FIG. 5, in the batch reaction tank 1, the oxygen-free stirring step (a), the aerobic reaction step (b), the stirring precipitation step (c), and the transfer step (d) are sequentially performed in a batch manner.

  In the oxygen-free stirring step (a), the blower 6 is stopped, the stirrer 8 is driven to supply the liquid to be treated while stirring, and nitrate nitrogen and nitrite generated in the aerobic reaction step (b) described later Biological denitrification treatment is performed using organic substances in the liquid to be treated as a hydrogen donor under an oxygen-free state.

  In the aerobic reaction step (b), the blower 6 is driven to aerate the aerated air from the diffuser tube 7, and the mixed liquid in the tank having a high sludge concentration in the second reaction tank 9 and the membrane separation tank 16 described later is returned. However, the pollutants are oxidized and decomposed by biological treatment under oxygen-rich conditions, and the pollutants (active sludge) grow by assimilating the pollutants into living organisms.

  In the stirring / precipitation step (c), the blower 6 is stopped, the stirrer 8 is driven, the aggregating agent and the agglomerating aid are supplied from the drug supply system 5 while agitating, and then the mixture is left to settle and separate. This precipitation separation does not require the formation of a complete solid-liquid separation layer because membrane separation is performed in a later step. In general precipitation separation, the concentrated activated sludge concentration of the sediment layer is 5 to 8 g / L by stopping the sludge concentration of the mixed liquid in the tank at the time of reaction to 3 to 5 g / L. In the present embodiment, a flocculant is used in combination, and the sludge concentration of the sludge concentration in the tank at the time of reaction can be achieved by returning the mixed liquid in the tank having a high concentration of sludge separated by membrane.

In the transfer step (d), a low-concentration liquid (sludge concentration of less than 4 g / L) having a low sludge concentration in the low-concentration liquid layer formed in the tank in the stirring and precipitation step (c) is supplied to the second reaction tank 9.
As shown in FIG. 1, during the oxygen-free stirring step (a) in the batch reaction tank 1, the transfer of the liquid mixture in the tank by the first liquid feeding system 10 and the first return system 12 is stopped. Then, the liquid to be processed flowing into the flow rate adjustment tank 2 from the liquid supply system 3 to be processed is supplied to the batch reaction tank 1 through the liquid supply system 4 to be biologically denitrified.

  Regardless of the state of the batch activated sludge treatment in the batch reaction tank 1, in the membrane separation activated sludge treatment in the second reaction tank 9 and the membrane separation tank 16, the mixed liquid in the second reaction tank 9 is used as the first mixture. A two-liquid feed system 17 sends a fixed amount of liquid to the membrane separation tank 16, and a mixed liquid in the tank of the membrane separation tank 16 is returned to the second reaction tank 9 by the second return system 18 under a natural flow. The mixed liquid in the tank 9 is circulated between the membrane separation tank 16 and subjected to the membrane separation activated sludge treatment with almost complete mixing.

  In the second reaction tank 9, the aerated air supplied from the blower 13 is diffused from the diffuser tube 14 and stirred by the stirrer 15. Either aeration or agitation can be performed. In the membrane separation tank 16, aeration air supplied from the blower 24 is diffused from the diffusion tube 23, and the mixed liquid in the tank is supplied to the membrane filling unit 21 of the submerged membrane separation device 19 by the upward flow of the solid-gas / liquid mixed phase generated by the aeration air. Membrane separation is carried out while supplying the membrane by cross flow, and the membrane filtrate is taken out of the tank through the suction pump 22.

  As shown in FIG. 2, during the aerobic reaction step (b) in the batch reaction tank 1, the transfer by the liquid feed system 4 to be treated and the first liquid feed system 10 is stopped, and the second reaction tank 9 is sent to the batch reaction tank 1 by the first return system 12.

  In this way, the membrane separation activated sludge treatment is performed in the second reaction tank 9 and the membrane separation tank 16 while almost completely mixing the tank mixture, and the tank mixture having a high sludge concentration is returned to the batch reaction tank 1. By increasing the sludge concentration in the batch-type reaction tank 1 to promote the biological reaction, the batch-type activated sludge treatment can remove the pollutant components that easily settle in the liquid to be treated, adsorb the pollutants (microorganisms), It is possible to effectively act on the liquid to be treated which is supplied at the time of the next batch treatment by keeping the coagulation aid in the batch type reaction tank 1 for coagulation (flocculating agent) and precipitation.

  As shown in FIG. 3, during the stirring and precipitation step (c) in the batch reaction tank 1, the transfer by the liquid feed system 4 to be processed, the first liquid feed system 10, and the first return system 12 is stopped. A low concentration liquid layer is formed by precipitation separation.

  As shown in FIG. 4, during the transfer step (d) in the batch reaction tank 1, the transfer by the liquid supply system 4 to be processed and the first return system 12 are stopped, and the first liquid supply system 10 The low concentration liquid of the batch reaction tank 1 is supplied to the second reaction tank 9.

  This low-concentration liquid has a low pollution load and a low sludge concentration, and the sludge concentration in the mixed liquid in the second reaction tank 9 and the membrane separation tank 16 in the membrane separation activated sludge treatment decreases. By reducing the sludge concentration, the membrane separation tank 16 increases the oxygen dissolution efficiency while suppressing membrane surface clogging due to membrane contaminants and sludge, and precipitates flowing from the batch reaction tank 1 are difficult to separate and difficult to separate. Biodegradation products can be treated with membrane activated activated sludge.

  The excess sludge can be taken out from the membrane separation tank 16 by the sludge extraction system 20 or in the sludge extraction system 11 of the batch reaction tank 1. If the excess sludge is drawn from the membrane separation tank 16, the concentration of the sludge in the batch reaction tank 1 can be maintained high, and if the excess sludge is drawn from the batch reaction tank 1, the load on the membrane separation tank 16 can be reduced.

  In the above-described operation, the suction port of the first return system 12 in the second reaction tank 9 is disposed at a position lower than the suction port of the second liquid supply system 17, and the stirring strength of the stirrer 15 is adjusted by standing for a fixed time. By forming a sludge concentration gradient in the depth direction, the mixed liquid in the tank with low sludge concentration under the low depth is sent to the membrane separation tank 16, and the mixed liquid in the tank with high sludge concentration under the deep water depth is sent to the membrane separation tank 16. It is also possible to return to the batch reaction tank 1.

  In this case, a sludge concentration difference is formed between the second reaction tank 9 and the membrane separation tank 16 in which the mixed liquid in the tank is circulated, and the sludge concentration in the second reaction tank 9 is increased, and the sludge concentration in the membrane separation tank 16 is increased. Is reduced, the sludge concentration of the mixed liquid in the tank returned from the second reaction tank 9 to the batch reaction tank 1 is increased, and the sludge concentration in the batch reaction tank 1 is further increased. By reducing the sludge concentration of the mixed liquid in the tank that is fed to the membrane separation tank 16, the oxygen dissolution efficiency in the membrane separation tank 16 is further increased, and further suppression of the membrane surface blockage can be realized.

  By the way, in the batch-type reaction tank 1, the operating water level can be freely changed to cope with the flow rate fluctuation, but the membrane separation tank 16 can also be operated by changing the water level according to the water quantity fluctuation. For this reason, as shown in FIGS. 7-10, the structure which eliminates the 2nd reaction tank 9 is also realizable.

  7 to 10, the same reference numerals are given to the same components as those in the previous embodiment, and the description thereof is omitted. 8 corresponds to the state in which the aerobic reaction step (b) is performed in the batch reaction tank 1, FIG. 7 corresponds to the state in which the oxygen-free stirring step (a) is performed in the batch reaction tank 1, and FIG. 10 corresponds to the state in which the stirring and precipitation step (c) is performed in the batch reaction tank 1, and FIG. 10 corresponds to the state in which the transfer step (d) is performed in the batch reaction tank 1.

  As shown in FIG. 10, in the membrane separation tank 16, the water level rises when the low-concentration liquid is transferred from the batch reaction tank 1, and the inflow of the low-concentration liquid stops as shown in FIGS. In the meantime, the water level gradually decreases as the membrane filtrate is taken out by the submerged membrane separator 19.

The fluctuation range of the water level in the membrane separation tank 16 is 5 to 50%, and the amount of low-concentration liquid transferred from the batch reaction tank 1 is an amount corresponding to the fluctuation range of the water level in the membrane separation tank 16.
As shown in FIG. 6, daily inflow Q of the liquid to be treated, return ratio r (return pump flow rate / inflow), membrane tank (all membrane separation activated sludge tanks) capacity V, number of batch cycles per day In the case where the flow rate fluctuation of the water to be treated is absorbed in the batch tank and all flows into the batch tank, if the water level fluctuation width of the membrane separation tank is 50%, the transfer amount of one cycle must be within that fluctuation range. .

Therefore, [(r + 1) / b] Q <0.5V.
The greater the number of cycles, the lower the efficiency because the precipitation time is shortened. The number of cycles is at most about 20 times / day. The return ratio is usually 0.1-5.

Therefore, for example, when b = 10 and r = 1, V> 0.4Q is designed.
However, when the total capacity is relatively small, for example, when it is not much larger than 0.4Q, it is not a good idea to increase the capacity of the tank.

The schematic diagram which shows the anoxic stirring process of the water treatment apparatus in embodiment of this invention The schematic diagram which shows the aerobic reaction process of the water treatment apparatus in the embodiment The schematic diagram which shows the stirring precipitation process of the water treatment apparatus in the embodiment The schematic diagram which shows the transfer process of the water treatment apparatus in the embodiment The schematic diagram which shows the batch processing procedure of the batch type reaction tank in the same embodiment The figure for demonstrating the relationship between the inflow amount Q, the return ratio r, the membrane tank capacity V, and the number b of batches per day The schematic diagram which shows the oxygen-free stirring process of the water treatment apparatus in other embodiment of this invention. The schematic diagram which shows the aerobic reaction process of the water treatment apparatus in the embodiment The schematic diagram which shows the stirring precipitation process of the water treatment apparatus in the embodiment The schematic diagram which shows the transfer process of the water treatment apparatus in the embodiment Schematic diagram showing a conventional water treatment device

Explanation of symbols

Single batch reactor (first reactor)
DESCRIPTION OF SYMBOLS 2 Flow control tank 3 To-be-processed liquid supply system 4 To-be-processed liquid supply system 5 Chemical supply system 6 Blower 7 Aeration pipe 8 Stirrer 9 2nd reaction tank 10 1st liquid supply system 11 Sludge extraction system 12 1st return system 13 Blower 14 Aeration tube 15 Stirrer 16 Membrane separation tank (third reaction tank)
17 Second liquid supply system 18 Second return system 19 Submerged membrane separator 20 Sludge extraction system 21 Membrane filling part 22 Suction pump 23 Aeration pipe 24 Blower

Claims (6)

In the batch-type reaction tank, the liquid to be treated is treated in a batch-type activated sludge, the low-concentration liquid in the batch-type reaction tank is supplied to the second reaction tank, and the mixed liquid in the tank in the second reaction tank is between the membrane separation tank. A water treatment method characterized in that the membrane-separated activated sludge is treated while circulating and the mixed liquid in the second reaction tank is returned to the batch reaction tank. A sludge concentration gradient in the depth direction is formed in the second reaction tank, and the mixed liquid in the tank having a low sludge concentration at a low depth is sent to the membrane separation tank, and the mixed liquid in the tank having a high sludge concentration at a deep depth is obtained. The water treatment method according to claim 1, wherein the water is returned to the batch reaction tank. In the batch reaction tank, the liquid to be treated is treated in batch activated sludge, and the low concentration liquid in the batch reaction tank is supplied to the membrane separation tank to perform membrane separation activated sludge treatment. A water treatment method characterized by returning to a batch reaction tank. In a batch reaction tank, an oxygen-free stirring process performed while supplying the liquid to be treated, an aerobic reaction process performed while aeration of the mixed liquid in the tank, and an agitation-precipitation process for adding a flocculant and allowing to stand after stirring. The water treatment method according to any one of claims 1 to 3, wherein the low concentration liquid separated by precipitation is sequentially transferred to the next tank. A batch reaction tank for treating the liquid to be treated with a batch activated sludge, a second reaction tank for storing a low-concentration liquid in the batch reaction tank, and an in-vessel mixing of the second reaction tank with a submerged membrane separator A membrane separation tank that treats the liquid with membrane separation activated sludge, a first liquid feed system that feeds a low-concentration liquid in a batch reaction tank to the second reaction tank, and a batch reaction of the liquid mixture in the tank of the second reaction tank A first return system that returns to the tank, a second liquid supply system that sends the mixed liquid in the tank of the second reaction tank to the membrane separation tank, and a mixed liquid in the tank of the membrane separation tank is returned to the second reaction tank. A water treatment device comprising a second return system. A batch type reaction tank for treating a liquid to be treated with a batch activated sludge, a membrane separation tank for treating a low concentration liquid of a batch type reaction tank having a submerged membrane separation apparatus, and a batch type reaction tank A water treatment apparatus comprising: a liquid feeding system for feeding a low concentration liquid to a membrane separation tank; and a return system for returning the liquid mixture in the tank of the membrane separation tank to a batch reaction tank.

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