CN115611415A - Method and apparatus for treating organic wastewater - Google Patents
Method and apparatus for treating organic wastewater Download PDFInfo
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- CN115611415A CN115611415A CN202210796592.7A CN202210796592A CN115611415A CN 115611415 A CN115611415 A CN 115611415A CN 202210796592 A CN202210796592 A CN 202210796592A CN 115611415 A CN115611415 A CN 115611415A
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1278—Provisions for mixing or aeration of the mixed liquor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Abstract
Provided are a method for treating organic wastewater and an apparatus for treating organic wastewater, which can perform stable solid-liquid separation by a membrane while maintaining high treatment efficiency in a treatment in which membrane separation is performed after a biological treatment of organic wastewater. In a method for treating organic wastewater, wherein the organic wastewater is biologically treated under aerobic conditions in a reaction tank (12) provided with a carrier (44), and SS component in the obtained biologically treated water is subjected to membrane separation, the BOD of the organic wastewater flowing into the reaction tank (12): the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank (12) at 5mg/L or less, and adding a nitrogen source to the reaction tank (12) so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing biological treatment.
Description
Technical Field
The present invention relates to a method and an apparatus for treating organic wastewater.
Background
The biological treatment by the activated sludge method is generally adopted for the treatment of organic wastewater, but the BOD volume load is 0.5 to 1.0kg/m 3 Around a day, and therefore requires a wider footprint. On the other hand, the biological treatment method using the carrier can perform BOD volume load of 1.5kg/m 3 The load per day or more is increased, and the floor area can be reduced.
As shown in patent document 1, a membrane separation method is proposed as a solid-liquid separation method for treated water in a fluidized bed biological treatment method using a carrier. By performing solid-liquid separation of sludge by a microfiltration membrane (MF membrane) or an ultrafiltration membrane (UF membrane), good treated water can be obtained, while in a high-load treatment in which the BOD volume load is set to be high, sludge is likely to adhere to the membrane, and stable operation becomes a problem.
Documents of the prior art
Patent document
Patent document 1: JP-A2013-208560
Disclosure of Invention
(problems to be solved by the invention)
An object of the present invention is to provide a method and an apparatus for treating organic wastewater, which can perform stable solid-liquid separation by a membrane while maintaining high treatment efficiency in a treatment in which membrane separation is performed after biological treatment of organic wastewater.
(means for solving the problems)
The present invention provides a method for treating organic wastewater, which comprises biologically treating organic wastewater under aerobic conditions in a reaction tank equipped with a carrier and separating SS components in the obtained biologically treated water by a membrane, wherein the BOD: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
In addition to the method for treating organic wastewater, it is preferable that the biological treatment is performed while maintaining the concentration of soluble phosphorus in the reaction tank at 0.1mg/L or more.
In the method for treating organic wastewater, it is preferable that the reaction tank is composed of 2 or more stages of reaction tanks connected in series, and in at least 1 reaction tank among the 2 or more stages of reaction tanks connected in series, the BOD: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
In the method for treating organic wastewater, the reaction tank is preferably a fluidized bed type reaction tank, and the BOD volume load of the reaction tank is preferably 1.5kg/m 3 More than one day.
The present invention provides an apparatus for treating organic wastewater, which biologically treats organic wastewater under aerobic conditions in a reaction tank equipped with a carrier, and performs membrane separation of SS component in the obtained biologically treated water, wherein the BOD of the organic wastewater flowing into the reaction tank: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
In the apparatus for treating organic wastewater, the biological treatment is preferably performed while maintaining a concentration of soluble phosphorus in the reaction tank at 0.1mg/L or more.
In the organic wastewater treatment apparatus, it is preferable that the reaction tank is composed of 2 or more stages of reaction tanks connected in series, and in at least 1 reaction tank out of the 2 or more stages of reaction tanks connected in series, the ratio of BOD: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
In the organic wastewater treatment apparatus, the reaction tank is preferably a fluidized bed reaction tank, and the BOD volumetric load of the reaction tank is preferably 1.5kg/m 3 More than one day.
(effect of the invention)
The present invention can provide a method and an apparatus for treating organic wastewater, which can perform stable solid-liquid separation by a membrane while maintaining high treatment efficiency in a treatment in which membrane separation is performed after biological treatment of organic wastewater.
Drawings
Fig. 1 is a schematic diagram showing an example of the configuration of an organic wastewater treatment apparatus according to the present embodiment.
Fig. 2 is a schematic diagram showing another example of the configuration of the organic wastewater treatment apparatus according to the present embodiment.
Detailed Description
Hereinafter, embodiments of the present invention will be described. This embodiment is an example of the present invention, and the present invention is not limited to this embodiment.
Fig. 1 shows an outline of an example of an organic wastewater treatment apparatus according to an embodiment of the present invention, and a configuration thereof will be described.
The organic wastewater treatment apparatus 1 shown in fig. 1 is an organic wastewater treatment apparatus for biologically treating organic wastewater under aerobic conditions in a reaction tank 12 provided with a carrier 44 and performing membrane separation of SS components in the obtained biologically treated water. The processing apparatus 1 includes, for example: a reaction tank 12 having a carrier 44 for biologically treating organic wastewater under aerobic conditions; a membrane separation device 48 for performing membrane separation of the SS component in the biologically treated water obtained by the biological treatment; a detector 20 as a dissolved nitrogen concentration detection means for detecting the dissolved nitrogen concentration in the reaction tank 12; a nitrogen source addition unit that adds a nitrogen source to the reaction tank 12; and a control device 16 as control means for controlling the flow rate of BOD: the weight ratio of nitrogen is less than 100:3, the addition of the nitrogen source to the reaction tank 12 is controlled so that the BOD of the organic wastewater is controlled to be equal to or less than 5mg/L while the concentration of the soluble nitrogen in the reaction tank 12 is maintained at 5mg/L or less: the weight ratio of nitrogen is 100:1 to 3. The processing apparatus 1 may include a phosphorus source adding unit that adds a phosphorus source to the reaction tank 12.
The treatment apparatus 1 may include a raw water tank 10 for storing organic wastewater as raw water, a biological treatment water tank 14 for storing biological treatment water, a nitrogen source tank 26 for storing a nitrogen source, and a phosphorus source tank 32 for storing a phosphorus source. The processing apparatus 1 may be provided with a detector 21 as a soluble phosphorus concentration detection means for detecting the concentration of soluble phosphorus in the reaction tank 12. The treatment apparatus 1 may include a BOD measuring unit that measures BOD of the organic wastewater flowing into the reaction tank 12.
In the treatment apparatus 1 shown in fig. 1, one end of the inflow line 22 is connected to the raw water outlet of the raw water tank 10, and the other end of the inflow line 22 is connected to the inlet of the reaction tank 12. The raw water pump 18 is provided in the inflow line 22. One end of a nitrogen source addition line 28 is connected to the inflow line 22 downstream of the raw water pump 18, and the other end of the nitrogen source addition line 28 is connected to the nitrogen source tank 26. One end of a phosphorus source addition line 34 is connected to the inflow line 22 downstream of the raw water pump 18, and the other end of the phosphorus source addition line 34 is connected to the phosphorus source tank 32. A nitrogen source addition pump 30 is provided in the nitrogen source addition line 28, and a phosphorus source addition pump 36 is provided in the phosphorus source addition line 34. One end of a biological treatment water line 24 is connected to the outlet of the reaction tank 12, and the other end of the biological treatment water line 24 is connected to the inlet of the biological treatment water tank 14. One end of a biological treatment water line 50 is connected to an outlet of the biological treatment tank 14, and the other end of the biological treatment water line 50 is connected to an inlet of the membrane separation device 48. To the outlet of the membrane separation device 48 is connected one end of a treated water line 52. The nitrogen source tank 26, the nitrogen source addition line 28, the nitrogen source addition pump 30, and the like function as nitrogen source addition means for adding a nitrogen source to the reaction tank 12, and the phosphorus source tank 32, the phosphorus source addition line 34, the phosphorus source addition pump 36, and the like function as phosphorus source addition means for adding a phosphorus source to the reaction tank 12.
The controller 16, the raw water pump 18, the nitrogen source addition pump 30, the phosphorus source addition pump 36, the detector 20, and the detector 21 are connected by wired or wireless electrical connections, respectively.
The reaction tank 12 is filled with a carrier 44 for holding microorganisms. The carrier 44 is not particularly limited, and examples thereof include a plastic carrier, a sponge carrier, and a gel carrier.
An aeration device 46 is provided as an oxygen-containing gas supply means for supplying an oxygen-containing gas such as air to the bottom of the reaction tank 12. An unillustrated blower is connected to the aeration device 46, and oxygen-containing gas such as air supplied from the blower is supplied from the aeration device 46 into the reaction tank 12.
The reaction tank 12 is provided with a detector 20 for detecting the concentration of soluble nitrogen in the reaction tank 12 and a detector 21 for detecting the concentration of soluble phosphorus in the reaction tank 12. The detectors 20, 21 may be disposed in the biological treatment tank 14 or the biological treatment water line 24. The soluble nitrogen concentration and the soluble phosphorus concentration of the biological treatment water detected by the detectors 20 and 21 in the biological treatment water tank 14 and the biological treatment water line 24 may be set to the soluble nitrogen concentration and the soluble phosphorus concentration in the reaction tank 12. The soluble nitrogen is, for example, nitrogen derived from a nitrogen source supplied from a nitrogen source addition unit, ammonia nitrogen, nitrate nitrogen, nitrite nitrogen, or the like originally contained in the organic wastewater. The soluble phosphorus is, for example, phosphorus derived from a phosphorus source supplied from the phosphorus source addition unit, a phosphorus compound originally contained in the organic wastewater, or the like.
The control device 16 is configured by, for example, a CPU that calculates a program, a microcomputer configured by a ROM and a RAM that store the program and a calculation result, an electronic circuit, and the like, and controls the operation of the processing device 1 by reading a predetermined program stored in the ROM or the like and executing the program. The control device 16 has the following functions: BOD of the organic wastewater flowing into the reaction tank 12: the weight ratio of nitrogen is less than 100:3, the concentration of dissolved nitrogen in the reaction tank 12 is maintained at 5mg/L or less, and the addition of the nitrogen source to the reaction tank 12 is controlled so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3. The controller 16 controls, for example, the operation and stop of the raw water pump 18. The controller 16 controls the operation and stop of the nitrogen source addition pump 30, the opening and closing of a valve provided in the nitrogen source addition line 28, and the like, based on, for example, BOD in the organic wastewater, the dissolved nitrogen concentration detected by the detector 20, and the like. The control device 16 controls, for example, the operation and stop of the phosphorus source addition pump 36, the opening and closing of a valve provided in the phosphorus source addition line 34, and the like based on the concentration of soluble phosphorus detected by the detector 21.
The method for treating organic wastewater and the operation of the treatment apparatus 1 according to the present embodiment will be described.
The organic wastewater treated by the treatment apparatus 1, that is, the organic wastewater fed into the raw water tank 10 is wastewater containing organic substances.
When the raw water pump 18 is operated by the controller 16, the organic wastewater in the raw water tank 10 is supplied to the reaction tank 12 through the inflow line 22. Then, oxygen-containing gas such as air is supplied from the aeration device 46 to the reaction tank 12, and the organic matter in the organic wastewater is biologically treated by microorganisms and the like adhering to the carriers 44 in the reaction tank 12 under aerobic conditions (biological treatment step). The biologically treated water treated in the reaction tank 12 is supplied to the biologically treated water tank 14 through the biologically treated water line 24. The biologically treated water stored in the biologically treated water tank 14 is supplied to the membrane separation device 48 through the biologically treated water line 50, and the SS component and the like are subjected to membrane separation in the membrane separation device 48 (membrane separation step). The treated water after the membrane separation treatment is discharged through a treated water line 52.
Through sharp discussion, the inventors of the present invention found the following results: in the membrane separation treatment performed after the biological treatment of the organic wastewater, the BOD of the organic wastewater flowing into the reaction tank 12: the weight ratio of nitrogen is less than 100:3, while maintaining the dissolved nitrogen concentration in the reaction tank 12 in a nitrogen-depleted state of 5mg/L or less, adding a nitrogen source to the reaction tank 12 so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, whereby the biological treatment is performed, and stable solid-liquid separation by a membrane can be performed in the membrane separation device 48 for performing membrane separation of the SS component in the biological treatment water while maintaining high treatment efficiency. In the biological treatment of organic wastewater, the filtration performance of solid-liquid separation using a membrane of the subsequent stage can be improved. In the present specification, BOD of organic wastewater: the weight ratio of nitrogen is less than 100:3 means that the nitrogen content is less than 3 parts by weight, and the BOD of the organic wastewater is: the weight ratio of nitrogen is 100:1 to 3 means 1 to 3 parts by weight of nitrogen per 100 parts by weight of BOD of the organic wastewater.
An example of controlling the concentration of dissolved nitrogen will be described below.
In the processing apparatus 1, the nitrogen source addition pump 30 is operated by the control unit 16, and the nitrogen source is introduced into the reaction tank 12. At this time, the controller 16 controls the flow rate of the organic wastewater based on the BOD: the weight ratio of nitrogen is less than 100:3, and the nitrogen source addition pump 30 is controlled so as to supply the nitrogen source in the calculated amount into the reaction vessel 12. For measuring BOD of organic wastewater, a BOD measuring device may be provided as a BOD measuring unit in the raw water tank 10 or the inflow line 22, and BOD may be measured at any time. The BOD of the organic wastewater is measured, for example, according to the method defined in JIS K0102. Since measurement of BOD by this method may take time, measurement of BOD may be performed before the operation of the processing apparatus 1. For example, a TOC measuring device may be provided as a BOD measuring means in the raw water tank 10 or the inflow line 22, the TOC of the organic wastewater may be detected, and BOD may be estimated from the detected TOC. Since TOC can be measured quickly, BOD of organic wastewater can be obtained at any time while operating the treatment apparatus 1 by a method of estimating BOD from TOC. The measured BOD is stored in the control device 16 for the purpose of calculating the supply amount of the nitrogen source. In addition, the nitrogen amount of the organic wastewater can be measured as needed. The measured nitrogen amount is stored in the control device 16 for the purpose of calculating the nitrogen source supply amount.
Then, when the concentration of dissolved nitrogen detected by the detector 20 is 5mg/L or less and the BOD of the organic wastewater is: the weight ratio of nitrogen is 100:1 to 3, the controller 16 controls the nitrogen source addition pump 30 to maintain the calculated amount of the nitrogen source. When the dissolved nitrogen concentration detected by the detector 20 exceeds 5mg/L, the controller 16 limits the output of the nitrogen source addition pump 30 to reduce the supply amount of the nitrogen source.
The concentration of the soluble phosphorus in the reaction vessel 12 is preferably maintained in a residual phosphorus state of 0.1mg/L or more, more preferably in the range of 0.5 to 1.0 mg/L. When the phosphorus concentration in the reaction tank 12 is low and the soluble phosphorus concentration detected by the detector 21 is less than 0.1mg/L, the control device 16 may operate the phosphorus source addition pump 36 to introduce the phosphorus source into the reaction tank 12. Further, even when the concentration of phosphorus in the organic wastewater is high and the concentration of soluble phosphorus detected by the detector 21 exceeds 0.1mg/L, the phosphorus source addition pump 36 may be operated to introduce the phosphorus source into the reaction tank 12. Among these, the upper limit of the concentration of the soluble phosphorus in the reaction tank 12 is preferably maintained at 8mg/L or less, more preferably at 4mg/L or less, considering the discharge standard and the like.
The detection of the concentration of soluble nitrogen and the concentration of soluble phosphorus in the reaction tank 12 is preferably performed on-line by a detector, but may be performed manually by an operator when the detector is not provided.
For example, the detector 20 may be provided in the raw water tank 10, and the soluble nitrogen concentration in the reaction tank 12 may be estimated from the soluble nitrogen concentration of the organic wastewater. In this case, for example, a map (or a relational expression, a table, or the like) showing the correlation between the soluble nitrogen concentration of the organic wastewater and the soluble nitrogen concentration in the reaction tank 12 is created in advance by an experiment or the like and stored in the control device 16. Then, the controller 16 compares the dissolved nitrogen concentration of the organic wastewater detected by the detector 20 with the BOD: the weight ratio of nitrogen is 100: the dissolved nitrogen concentration in the reaction tank 12 is estimated by applying the sum of the dissolved nitrogen concentrations obtained from the amounts of nitrogen source supplied in the ranges of 1 to 3 to the above-mentioned map or the like. The estimated concentration of dissolved nitrogen in the reaction tank 12 exceeds 5mg/L, and is equal to or higher than the BOD of the organic wastewater: the weight ratio of nitrogen is 100: when 3 is larger than nitrogen, the controller 16 limits the output of the nitrogen source addition pump 30 to reduce the amount of nitrogen to be supplied.
For example, the detector 21 may be provided in the raw water tank 10, and the soluble phosphorus concentration in the reaction tank 12 may be estimated from the soluble phosphorus concentration in the organic wastewater. In this case, for example, a map (or a relational expression, a table, or the like) showing the correlation between the soluble phosphorus concentration of the organic wastewater and the soluble phosphorus concentration in the reaction tank 12 is created in advance by an experiment or the like and stored in the control device 16. Then, the controller 16 estimates the concentration of soluble phosphorus in the reaction tank 12 by applying the concentration of soluble phosphorus in the organic wastewater detected by the detector 21 to the map or the like. In the case where the estimated concentration of soluble phosphorus in the reaction tank 12 is less than 0.1mg/L, the control device 16 may operate the phosphorus source addition pump 36 to introduce the phosphorus source into the reaction tank 12.
Fig. 2 is a schematic diagram showing another example of the configuration of the organic wastewater treatment apparatus according to the present embodiment. In the processing apparatus 2 of fig. 2, the same components as those of the processing apparatus 1 of fig. 1 are denoted by the same reference numerals, and descriptions thereof are omitted. The processing apparatus 2 shown in fig. 2 includes a reaction vessel group having a first reaction vessel 12a and a second reaction vessel 12b as reaction vessels. The reaction tank group is configured by arranging the first reaction tank 12a and the second reaction tank 12b in series with the first reaction tank 12a as a front stage and the second reaction tank 12b as a rear stage. The reaction vessel group may be configured by arranging reaction vessels of 3 or more stages in series.
In the treatment apparatus 2 shown in fig. 2, one end of an inflow line 22a is connected to the raw water outlet of the raw water tank 10, and the other end of the inflow line 22a is connected to the inlet of the first reaction tank 12a. The raw water pump 18 is provided in the inflow line 22 a. One end of a nitrogen source addition line 28a is connected to the raw water pump 18 downstream side of the inflow line 22a, and the other end of the nitrogen source addition line 28a is connected to the nitrogen source tank 26 a. One end of a phosphorus source addition line 34a is connected to the inflow line 22a on the downstream side of the raw water pump 18, and the other end of the phosphorus source addition line 34a is connected to the phosphorus source tank 32 a. A nitrogen source addition pump 30a is provided in the nitrogen source addition line 28a, and a phosphorus source addition pump 36a is provided in the phosphorus source addition line 34 a. One end of an inflow line 22b is connected to the outlet of the first reaction tank 12a, and the other end of the inflow line 22b is connected to the inlet of the second reaction tank 12b. One end of a nitrogen source addition line 28b is connected to the inflow line 22b, and the other end of the nitrogen source addition line 28b is connected to the nitrogen source tank 26 b. One end of a phosphorus source addition line 34b is connected to the inflow line 22b, and the other end of the phosphorus source addition line 34b is connected to the phosphorus source tank 32 b. A nitrogen source addition pump 30b is provided in the nitrogen source addition line 28b, and a phosphorus source addition pump 36b is provided in the phosphorus source addition line 34 b. One end of a biological treatment water line 24 is connected to the outlet of the second reaction tank 12b, and the other end of the biological treatment water line 24 is connected to the inlet of the biological treatment water tank 14. One end of a biological treatment water line 50 is connected to an outlet of the biological treatment tank 14, and the other end of the biological treatment water line 50 is connected to an inlet of the membrane separation device 48. To the outlet of the membrane separation device 48 is connected one end of a treated water line 52. The nitrogen source tank 26a, the nitrogen source addition line 28a, the nitrogen source addition pump 30a, and the like function as nitrogen source addition means for adding a nitrogen source to the first reaction tank 12a, and the nitrogen source tank 26b, the nitrogen source addition line 28b, the nitrogen source addition pump 30b, and the like function as nitrogen source addition means for adding a nitrogen source to the second reaction tank 12b. The phosphorus source tank 32a, the phosphorus source addition line 34a, the phosphorus source addition pump 36a, and the like function as phosphorus source addition means for adding a phosphorus source to the first reaction tank 12a, and the phosphorus source tank 32b, the phosphorus source addition line 34b, the phosphorus source addition pump 36b, and the like function as phosphorus source addition means for adding a phosphorus source to the second reaction tank 12b.
The control device 16 is connected to the raw water pump 18, the nitrogen source adding pumps 30a and 30b, the phosphorus source adding pumps 36a and 36b, the detectors 20a and 20b, and the detectors 21a and 21b by wired or wireless electrical connections, respectively.
The first reaction tank 12a and the second reaction tank 12b are filled with carriers 44 for holding microorganisms, respectively.
The first reaction tank 12a is provided with a detector 20a for detecting the concentration of soluble nitrogen in the first reaction tank 12a and a detector 21a for detecting the concentration of soluble phosphorus in the first reaction tank 12a. The second reaction tank 12b is provided with a detector 20b for detecting the concentration of soluble nitrogen in the second reaction tank 12b and a detector 21b for detecting the concentration of soluble phosphorus in the second reaction tank 12b. The detectors 20a and 21a of the first reaction tank 12a may be provided upstream of the connection point of the nitrogen source addition line 28b and the phosphorus source addition line 34b in the inflow line 22 b. The soluble nitrogen concentration and the soluble phosphorus concentration of the biological treatment water detected by the detectors 20a and 21a in the inflow line 22b may be set to the soluble nitrogen concentration and the soluble phosphorus concentration in the first reaction tank 12a. The detectors 20b and 21b of the second reaction tank 12b may be provided in the biological treatment water tank 14 or the biological treatment water line 24. The soluble nitrogen concentration and the soluble phosphorus concentration of the biological treatment water detected by the detectors 20b and 21b in the biological treatment water tank 14 or the biological treatment water line 24 may be the soluble nitrogen concentration and the soluble phosphorus concentration in the second reaction tank 12b.
The controller 16 controls, for example, the operation and stop of the raw water pump 18. The controller 16 controls the operation and stop of the nitrogen source addition pumps 30a and 30b, the opening and closing of the valves provided in the nitrogen source addition lines 28a and 28b, and the like, based on, for example, BOD in the organic wastewater, the dissolved nitrogen concentration detected by the detectors 20a and 20b, and the like. The controller 16 controls, for example, the operation and stop of the phosphorus source addition pumps 36a and 36b, and the opening and closing of valves provided in the phosphorus source addition lines 34a and 34b, based on the concentration of soluble phosphorus detected by the detectors 21a and 21b.
Next, the operation of the processing apparatus 2 shown in fig. 2 will be described.
When the raw water pump 18 is operated by the controller 16, the organic wastewater in the raw water tank 10 is supplied to the first reaction tank 12a through the inflow line 22 a. Then, oxygen-containing gas such as air is supplied from the aeration device 46a to the first reaction tank 12a, and the organic matter in the organic wastewater is biologically treated by microorganisms or the like adhering to the carriers 44 in the first reaction tank 12a under aerobic conditions (first biological treatment step). The first biologically treated water treated in the first reaction tank 12a is supplied to the second reaction tank 12b through the inflow line 22 b. Then, oxygen-containing gas such as air is supplied from the aeration apparatus 46b to the second reaction tank 12b, and the organic matter in the first biologically treated water is biologically treated by microorganisms or the like adhering to the carriers 44 in the second reaction tank 12b under aerobic conditions (second biologically treating step). The biologically treated water treated in the second reaction tank 12b is supplied to the biologically treated water tank 14 through the biologically treated water line 24. The biologically treated water stored in the biologically treated water tank 14 is supplied to the membrane separation device 48 through the biologically treated water line 50, and the SS component and the like are subjected to membrane separation in the membrane separation device 48 (membrane separation step). The treated water after the membrane separation treatment is discharged through a treated water line.
Here, in the case where the reaction tanks are configured to be 2 or more in order, the BOD of the organic wastewater flowing into the reaction tanks: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, and performing biological treatment. Thus, stable solid-liquid separation by a membrane can be performed in a membrane separation apparatus for performing membrane separation of an SS component in biologically treated water while maintaining high treatment efficiency. In the case where the reaction tank is composed of 2 or more stages, the BOD of the organic wastewater flowing into the reaction tank of the first stage is preferably: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank of the first stage at 5mg/L or less, and adding a nitrogen source to the reaction tank of the first stage so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing biological treatment. In this case, most of the organic matter is removed in the first-stage reaction tank, and the amount of organic matter removed in the second-stage reaction tank is small, so that BOD for maintaining the soluble nitrogen concentration at 5mg/L or less and draining the organic wastewater is not performed in the second-stage and subsequent reaction tanks: the weight ratio of nitrogen is 100:1 to 3, stable solid-liquid separation by a membrane can be performed in a membrane separation apparatus for performing membrane separation of an SS component in biologically treated water while maintaining high treatment efficiency of the entire system.
The following describes the operating conditions and the like of the treatment apparatus of the present embodiment.
From the viewpoint of culturing microorganisms, the pH in the reaction tank 12 is preferably adjusted to, for example, a weakly acidic to weakly alkaline pH, more preferably to a pH of 6 to 8. As the pH adjuster, an acid or an alkali may be used.
The dissolved oxygen concentration in the reaction tank 12 is, for example, preferably 0.5mg/L or more, and more preferably 1mg/L or more. The upper limit of the dissolved oxygen concentration in the reaction tank 12 is not particularly limited, but is, for example, 5.0mg/L or less.
The reaction tank 12 may be either a fixed bed type in which the carrier does not flow or a fluidized bed type in which the carrier flows. The fluidized bed reactor is preferred because it has advantages such as low short pass of raw water, excellent maintainability, and low introduction cost.
The BOD volume load of the reaction tank 12 (BOD volume load of all reaction tanks in the case of the reaction tank group) is preferably 1.5kg/m 3 More preferably 2.0kg/m 3 More than one day. The upper limit of the BOD volume load of the reaction tank 12 is not particularly limited, but is, for example, 8.0kg/m 3 The day is less.
The nitrogen source is not particularly limited, and examples thereof include ammonium chloride, ammonium sulfate, diammonium hydrogen phosphate, and urea. The remaining waste ammonium sulfate and the like generated in the plant can also be applied.
The phosphorus source includes phosphoric acid and a phosphorus compound, and is not particularly limited, but examples thereof include dipotassium phosphate, disodium phosphate, monopotassium phosphate, monosodium phosphate, and ammonium phosphate.
Nutrient salts and trace elements other than the nitrogen source and the phosphorus source may be added to the organic wastewater, and examples thereof include calcium, magnesium, iron, copper, zinc, and manganese.
The carrier 44 may be, for example, a plastic carrier, a sponge carrier, a gel carrier, or the like, but among them, a sponge carrier is preferable in terms of cost and durability.
From the viewpoint of improving the treatment speed of the biological treatment, the number of pores (number of pores) of the carrier 44 is preferably 30/25 mm or more, more preferably 30/25 mm or more and 100/25 mm or less, further preferably 40/25 mm or more and 100/25 mm or less, and particularly preferably 46/25 mm or more and 100/25 mm or less. The number of pores in the carrier is determined, for example, based on JIS K65400-1 (appendix 1).
The surface area of the carrier 44 is preferably 3000m in order to increase the treatment rate of the biological treatment 2 /m 3 Above, more preferably 3500m 2 /m 3 Above, more preferably 4000m 2 /m 3 Above, 4500m is particularly preferable 2 /m 3 The above. The upper limit of the surface area of the carrier is not particularly limited, and may be determined by considering the number of pores, the size of the carrier, and the like.
The amount of the carrier 44 to be attached with the living organisms is preferably 500mg/L or more, more preferably 1000mg/L or more, from the viewpoint of increasing the treatment speed of the biological treatment. The higher the amount of the carrier to be attached to the living body, the better, there is no particular upper limit, but the upper limit is, for example, 5000mg/L.
The shape of the carrier 44 is not particularly limited, and examples thereof include a tetragonal shape such as a cubic shape, a granular shape, a spherical shape, a granular shape, a cylindrical shape, a fibrous shape, and a film shape.
The size of the carrier 44 is not particularly limited, and may be appropriately set according to the size of the reaction vessel 12, the shape of the carrier, and the like, and for example, it is preferable that the length of one side is in the range of 3 to 20mm in the case of a cube shape, and the diameter is in the range of about 0.5 to 20mm in the case of a sphere shape. The size of the carrier 44 can be measured using a vernier caliper or a microscope or the like.
In order to form a fluidized state in the reaction tank 12, the specific gravity of the carrier 44 is preferably at least 1.0, for example, 1.1 or more as a true specific gravity, or 1.01 or more as an apparent specific gravity.
The amount of the carrier 44 to be charged into the reaction tank 12 is preferably in the range of 10 to 70% relative to the volume of the reaction tank 12. If the amount of the carrier 44 to be charged is less than 10% of the volume of the reaction tank 12, the reaction rate may be decreased, and if it exceeds 70%, the following may occur: the carrier 44 is difficult to flow, and the raw water passes through the carrier in a short distance due to clogging by sludge or the like during long-term operation, and the quality of the biological treatment water is deteriorated.
The membrane used in the membrane separation device 48 is not particularly limited as long as it is an organic membrane, for example, and can filter SS components (suspended substances) in the biologically treated water, and examples thereof include an ultrafiltration membrane (UF membrane) and a microfiltration membrane (MF membrane). The nominal pore diameter of the ultrafiltration membrane is 0.01 to less than 0.1 [ mu ] m, and the pore diameter of the microfiltration membrane is 0.1 to 0.3 [ mu ] m.
Examples of the material of the organic film include organic films such as Polyethersulfone (PES), polysulfone (PS), cellulose Acetate (CA), polyethylene (PE), polyvinylidene fluoride (PVDF), polytetrafluoroethylene (PTFE), polyvinyl alcohol (PVA), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), and Polycarbonate (PC).
The membrane separation device 48 is, for example, a module type membrane filtration device, and is a pressure type membrane filtration device having a filtration membrane sealed in a cylindrical container (casing) such as a cylindrical container. Examples of the form of the filtration membrane include a tubular membrane and a hollow fiber membrane. The filtration membrane may be passed through the membrane by either an internal pressure type or an external pressure type. As the membrane separation device 48, a flat membrane of a submerged type can be used.
In order to keep the SS concentration of the membrane separation device 48 low and set the filtration rate high, it is preferable that the sludge separated by solid-liquid separation by the membrane in the membrane separation device 48 does not flow into the reaction tank 12 provided with the carrier 44.
[ examples ] A method for producing a compound
The present invention will be described more specifically with reference to examples and comparative examples, but the present invention is not limited to the examples below.
[ test conditions ]
Volume of the reaction tank: 2L of
Carrier: sponge Carrier made of hydrophobic polyurethane (number of pores: 46/25 mm, shape: cube)
The carrier filling rate: the filling rate is 20 percent based on the bulk volume
Residence time in the reaction tank: 6 hours
BOD volume load of the reaction tank: about 3.2kg/m 3 Day/day
Water temperature in the reaction tank: about 20 c of the total weight of the composition,
dissolved oxygen concentration (DO) in the reaction tank: 2mg/L or more
pH in the reaction tank: 6.5 to 8.0
Organic drainage: drainage containing isopropanol (BOD about 800mg/L (BOD/TOC = 2.7), N2 mg/L or less, P0.1 mg/L or less)
The biologically treated water of the above-mentioned fluidized bed type biological treatment was subjected to suction filtration using an ultrafiltration membrane (UF membrane) (external pressure type, hollow fiber membrane, material: PVDF) with a flux of 3.0 m/day, and the inter-membrane pressure difference at this time was evaluated.
< comparative example 1 >
Ammonium chloride as a nitrogen source and phosphoric acid as a phosphorus source were added to organic wastewater as raw water so that BOD: n: p is calculated according to the ratio of 100:6.6:1.1 flows into the reaction tank. The biological treatment water had a soluble nitrogen concentration of 19mg/L and a residual nitrogen state, and a soluble phosphorus concentration of 4.4mg/L and a residual phosphorus state. The transmembrane pressure of the UF membrane was 36kPa, the BOD removal rate was 2.8kg/m 3 The day is one.
< comparative example 2 >
The amounts of ammonium chloride and phosphoric acid added were reduced from the operating conditions of comparative example 1 so that BOD: n: p is calculated by taking the ratio of 100:4.7:0.5 flows into the reaction tank. The biological treatment water had a soluble nitrogen concentration of 13mg/L and a soluble phosphorus concentration of 0.06mg/L and a phosphorus depleted state. The transmembrane pressure of the UF membrane was 33kPa, the BOD removal rate was 2.9kg/m 3 Day/day, same as in comparative example 1.
< example 1 >
The amounts of ammonium chloride and phosphoric acid added were reduced from the operating conditions of comparative example 1 so that BOD: n: p is calculated according to the ratio of 100:2.8:0.9 flows into the reaction tank. The concentration of dissolved nitrogen in the biologically treated water was 1.1mg/L (concentration of ammonium nitrogen was 0.3 mg)/L) was in a nitrogen-depleted state, the concentration of soluble phosphorus was 2.8mg/L, and phosphorus remained. The inter-membrane differential pressure of the UF membrane was greatly reduced to 12kPa. The BOD removal rate was 2.7kg/m 3 A high removal rate was maintained per day.
< example 2 >
The amounts of ammonium chloride and phosphoric acid added were reduced from the operating conditions of comparative example 1 so that BOD: n: p is calculated according to the ratio of 100:1.9:0.9 flows into the reaction tank. The biologically treated water had a soluble nitrogen concentration of 1.0mg/L (ammonia nitrogen concentration of 0.2 mg/L) and was in a nitrogen-depleted state, and a soluble phosphorus concentration of 3.6mg/L and was in a phosphorus-remaining state. The inter-membrane differential pressure of the UF membrane was greatly reduced to 14kPa. The BOD removal rate was 2.4kg/m 3 A high removal rate was maintained per day.
< example 3 >
The amounts of ammonium chloride and phosphoric acid added were reduced from the operating conditions of comparative example 1 so that BOD: n: p is calculated by taking the ratio of 100:1.0:0.8 flows into the reaction tank. The biologically treated water had a soluble nitrogen concentration of 2.6mg/L (ammonia nitrogen concentration of 0.4 mg/L) and was in a nitrogen-depleted state, and a soluble phosphorus concentration of 5.3mg/L and was in a phosphorus-remaining state. The inter-membrane differential pressure of the UF membrane was greatly reduced to 11kPa. The BOD removal rate was 2.1kg/m 3 A high removal rate was maintained per day.
< comparative example 3 >
The amounts of ammonium chloride and phosphoric acid added were reduced from the operating conditions of comparative example 1 so that BOD: n: p is calculated according to the ratio of 100:0.2:0.8 flows into the reaction tank. The biological treatment water had a soluble nitrogen concentration of 1.6mg/L and was in a nitrogen-depleted state, and a soluble phosphorus concentration of 6.5mg/L and was in a phosphorus-remaining state. The difference between the membrane pressures of the UF membranes was as low as 9kPa, but the BOD removal rate was 1.3kg/m 3 Day, a large drop in removal rate was exhibited.
From the above results, it was found that the dissolved nitrogen concentration in the reaction tank was maintained in a nitrogen-depleted state of 5mg/L or less, and the nitrogen source was added so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, and the concentration of the soluble phosphorus in the reaction vessel is set to a state of residual phosphorus, thereby enabling stable film treatment while maintaining high treatment efficiency. The pressure difference between the membranes of the UF membrane at the later stage of biological treatment can be below 20kPaThe BOD removal rate can be 2kg/m 3 More than one day.
As described above, according to the method of the embodiment, in the treatment of membrane separation performed after the biological treatment of organic wastewater, stable solid-liquid separation by a membrane can be performed while maintaining high treatment efficiency.
(description of reference numerals)
1. 2a treatment device, 10 a raw water tank, 12a reaction tank, 12a first reaction tank, 12b second reaction tank, 14 a biological treatment water tank, 16 a control device, 18 a raw water pump, 20a, 20b, 21a, 21b detector, 22a, 22b inflow pipeline, 24, 50 biological treatment water pipeline, 26a, 26b nitrogen source tank, 28, 28a, 28b nitrogen source addition lines, 30a, 30b nitrogen source addition pumps, 32a, 32b phosphorus source tanks, 34a, 34b phosphorus source addition lines, 36a, 36b phosphorus source addition pumps, 44 carriers, 46a, 46b aeration devices, 48 membrane separation devices, 52 process water lines.
Claims (8)
1. A method for treating organic wastewater, which comprises biologically treating the organic wastewater in a reaction tank equipped with a carrier under aerobic conditions and subjecting SS component in the obtained biologically treated water to membrane separation,
BOD of the organic wastewater flowing into the reaction tank: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
2. The method for treating organic wastewater according to claim 1,
the biological treatment is performed while maintaining the concentration of soluble phosphorus in the reaction tank at 0.1mg/L or more.
3. The method for treating organic wastewater according to claim 1 or 2,
the reaction tank is composed of 2 or more stages of reaction tanks connected in series, and the BOD: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
4. The method for treating organic wastewater according to any one of claims 1 to 3,
the reaction tank is a fluidized bed type reaction tank, and the BOD volume load of the reaction tank is 1.5kg/m 3 More than one day.
5. An apparatus for treating organic wastewater, which biologically treats organic wastewater under aerobic conditions in a reaction tank equipped with a carrier and performs membrane separation of SS component in the obtained biologically treated water,
BOD of the organic wastewater flowing into the reaction tank: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
6. The apparatus for treating organic wastewater according to claim 5,
the biological treatment is performed while maintaining the concentration of soluble phosphorus in the reaction tank at 0.1mg/L or more.
7. The apparatus for treating organic wastewater according to claim 5 or 6,
the reaction tank is composed of 2 or more stages of reaction tanks connected in series, and in at least 1 reaction tank among the 2 or more stages of reaction tanks connected in series, the BOD: the weight ratio of nitrogen is less than 100:3, maintaining the dissolved nitrogen concentration in the reaction tank at 5mg/L or less, and adding a nitrogen source to the reaction tank so that the BOD of the organic wastewater: the weight ratio of nitrogen is 100:1 to 3, thereby performing the biological treatment.
8. The apparatus for treating organic wastewater according to any one of claims 5 to 7,
the reaction tank is a fluidized bed type reaction tank, and the BOD volume load of the reaction tank is 1.5kg/m 3 More than one day.
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| JP3385306B2 (en) * | 1997-02-28 | 2003-03-10 | 株式会社クラレ | Wastewater treatment equipment |
| JP5789922B2 (en) * | 2010-07-02 | 2015-10-07 | 栗田工業株式会社 | Water treatment method and ultrapure water production method |
| JP6173205B2 (en) * | 2013-12-18 | 2017-08-02 | オルガノ株式会社 | Biological treatment apparatus and biological treatment method |
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- 2021-07-16 JP JP2021117974A patent/JP2023013640A/en active Pending
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- 2022-07-08 TW TW111125681A patent/TW202311175A/en unknown
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| CN1199712A (en) * | 1997-02-28 | 1998-11-25 | 可乐丽股份有限公司 | Waste water treatment apparatus |
| JP2001334285A (en) * | 2000-05-25 | 2001-12-04 | Japan Organo Co Ltd | Apparatus for biologically treating organic wastewater |
| CN1789169A (en) * | 2004-11-18 | 2006-06-21 | 栗田工业株式会社 | Organic sulfur compound containing water discharge apparatus |
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| JP2023013640A (en) | 2023-01-26 |
| TW202311175A (en) | 2023-03-16 |
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