JP5628955B2 - Organic waste water treatment apparatus and treatment method - Google Patents

Description

  The present invention relates to an organic wastewater treatment apparatus and an organic wastewater treatment method for treating an aerobic biological treatment of organic wastewater such as sewage and industrial wastewater after methane fermentation.

  The technology for aerobic biological treatment after high-concentration organic wastewater such as industrial wastewater is subjected to methane fermentation treatment, compared to the conventional technology that performs aerobic biological treatment alone. 2) It has the advantage of being able to recover methane gas and effectively use it as thermal energy, and has become popular in recent years. As a methane fermentation treatment method, the UASB (Up-flow Anaerobic Sludge Blanket) method is particularly widespread. However, when the UASB method is applied, the organic matter concentration of wastewater is generally targeted for CODcr 2000 mg / L or more. This is because, when the organic matter concentration in the organic wastewater is low, the methane fermentation process generates heating energy that brings the temperature inside the UASB tank to the optimum temperature (35 ° C) in order to maintain the activity of the microorganisms responsible for methane fermentation. This is because there are restrictions such as that it is impossible to cover with biogas, and that the water flow rate is maintained at 0.5 to 2.0 m / h for maintaining granular sludge.

On the other hand, in warming regions such as Brazil, India, and Southeast Asia, there have been cases where UASB treatment of low-concentration organic wastewater such as sewage (for example, CODcr 400 to 1000 mg / L) has been observed. FIG. 14 shows an example of an apparatus 201 that performs low-concentration organic wastewater treatment with methane fermentation and aerobic organisms. First, the UASB treatment is performed in the UASB tank 10 ′, and the easily decomposable organic matter in the waste water is decomposed into methane gas and collected. In the UASB treated water 2, organic substances that cannot be decomposed by the UASB treatment remain. Therefore, an aerobic biological treatment is performed using the subsequent reaction tank 20 ′ and the sedimentation basin 30 to finish these residual organic substances. It should be noted that the low-concentration organic wastewater has a larger amount of water at the same organic substance amount (concentration × water amount) than the high-concentration organic wastewater. Therefore, when low concentration organic wastewater is subjected to UASB treatment, the amount of CH ₄ and CO ₂ gas generated in the UASB treated water 2 is larger than that of high concentration organic wastewater. As a result, when the UASB treated water 2 is in contact with the atmosphere, a part of the dissolved methane is released into the atmosphere (see FIG. 15). In the subsequent aerobic biological treatment, the dissolved methane remaining from the aeration tank 21a constituting the reaction tank 20 ′ is diffused into the atmosphere together with the aerated air (see FIG. 16).

FIG. 17 shows the relationship between the water temperature and the solubility of methane in water. The partial pressure of methane and carbon dioxide here is 0.75 atm for the former and 0.25 atm for the latter. As the water temperature decreases, the solubility of methane in water increases. The solubility of methane in water at a water temperature of 20 ° C. is 24.8 (mL-CH ₄ / L-water). When domestic wastewater (CODcr 400 mg / L) is treated at 20 ° C. with HRT 10 h, 40 to 60% of the generated methane gas is dissolved in the UASB treated water as dissolved methane. Methane gas is known as one of the powerful greenhouse gases, and the greenhouse effect is said to be about 21 times that of CO ₂ . The effect of dissolved methane emission on global warming is significant.

  As a conventional technique for handling dissolved methane, there is a technique disclosed in Patent Document 1. In patent document 1, the method and apparatus which can collect | recover efficiently the dissolved methane contained in the dissolved methane containing waste water by the mass transfer effect | action which is a physical effect | action are provided. That is, the dissolved methane-containing wastewater is supplied from the upper part of the porous water retaining member disposed in the gas phase and brought into gas-liquid contact, and the dissolved methane-containing wastewater is transferred from the dissolved methane-containing wastewater to the gas phase. Dissolved methane recovery method and apparatus for gasifying and recovering dissolved methane contained in the gas. With this conventional technique, dissolved methane can be recovered at low cost.

JP 2008-168264 A

As described above, it is highly necessary to prevent dissolved methane in the methane fermentation treated water from being released into the atmosphere. However, in the prior art of Patent Document 1, since a physical gas-liquid diffusion operation is performed, if an attempt is made to increase the recovery rate of dissolved methane, the concentration of methane gas to be recovered increases due to an increase in the amount of blown air. It is necessary to treat the exhaust gas.
Then, this invention aims at providing the organic waste water treatment apparatus and the organic waste water treatment method which can process easily the methane which generate | occur | produced by the methane fermentation process and which melt | dissolved in the methane fermentation treated water without dissipating in air | atmosphere. And

The organic waste water treatment apparatus 101 according to the first aspect of the present invention for solving the above-described problem includes a methane fermentation treatment tank 10 for subjecting organic waste water to methane fermentation treatment, as shown in FIGS. An immersion type reaction tank 20 that performs aerobic biological treatment of the methane fermentation treated water 2 treated in the fermentation treatment tank 10 and a solid-liquid separation device 30 that separates the mixed liquid 3 in the reaction tank 20 into a solid and liquid. The methane fermentation treatment tank 10 is configured to prevent the methane dissolved in the methane fermentation treated water 2 in the methane fermentation treatment tank 10 from being diffused into the atmosphere, and the dissolved methane to be diffused into the atmosphere. It has the supply part 13 which supplies the methane fermentation treated water 2 to the reaction tank 20, maintaining the state prevented.
The “organic wastewater” may be high concentration organic wastewater such as food factory wastewater or low concentration organic wastewater such as domestic wastewater. In the present specification, “high concentration organic wastewater” refers to wastewater having a CODcr value of 1000 mg / L or more, and “low concentration organic wastewater” refers to wastewater having a CODcr value of 1000 mg / L or less. This is defined as the concentration range of organic wastewater where the influence of dissolved methane is large. “Preventing emission” is not limited to completely preventing emission but also includes suppressing emission. “Methane fermentation treatment tank” refers to a tank that performs anaerobic treatment in the range of ORP of −330 mV or less. The “reaction tank for aerobic biological treatment” refers to a tank that performs an organic treatment in a range of ORP of +50 mV to 100 mV or more.

If comprised in this way, it is methane produced by the methane fermentation process, Comprising: It can prevent that the methane which is not collect | recovered as methane gas but dissolves in treated water diffuses out of a methane fermentation treatment tank. Further, the dissolved methane can be transferred to a reaction tank without being diffused into the atmosphere, and can be oxidatively decomposed into carbon dioxide and water in the reaction tank.
In addition, the methane fermentation treatment water at the time of processing low concentration organic wastewater contains more dissolved methane compared with the methane fermentation treatment water at the time of processing high concentration organic wastewater. Therefore, this invention has a higher effect with respect to low concentration organic waste water. For example, it is effective for inflow sewage having a CODcr value of 400 to 1000 mg / L.

The organic waste water treatment apparatus 102 according to the second aspect of the present invention is the same as the waste water treatment apparatus 101 according to the first aspect of the present invention described above. For example, as shown in FIGS. An anaerobic tank 41 for processing and an aerobic tank 21b for aerobic biological treatment are provided. The anaerobic tank 41 and the aerobic tank 21b have a configuration in which the aerobic treated water treated in the aerobic tank 21b flows into the anaerobic tank 41 from the aerobic tank 21b. The supply unit 13 included in the methane fermentation treatment tank 10 supplies the methane fermentation treated water 2 to the anoxic tank 41.
In the present specification, “aerobic treated water” refers to treated water that has been subjected to aerobic biological treatment in a reaction tank (aerobic tank or aeration tank). “Anoxic tank” means that ORP is in the range of −50 mV to −200 mV, and there is no molecular oxygen for performing denitrification in the biological nitrogen removal method, but bound oxygen such as nitrate ions is present. A tank that is in a state (anoxic state). “Aerobic tank” refers to a tank that performs aerobic treatment in the range of ORP of 50 mV to 100 mV or more (particularly +200 mV to 400 mV when a nitrification reaction is involved).

If comprised in this way, the dissolved methane contained in methane fermentation treated water will be transferred to a reaction tank, without being lost by diffusion. In the aerobic tank of the reaction tank, NH ₄ -N is oxidized to NO ₂ -N and NO ₃ -N by nitrifying bacteria, and a nitrifying solution is generated. By flowing methane fermentation water containing dissolved methane and nitrification liquid into the oxygen-free tank, the oxygen-free tank is used to dehydrogenate intermediate products (such as methanol) generated by the oxidation of dissolved methane. Can be used as a nitrification solution. Thus, dissolved methane can be effectively used for denitrification treatment.
Normally, in biological nitrogen treatment, the ammonia contained is nitrified in an aerobic tank and converted to nitrous acid or nitric acid. Thereafter, nitrous acid and nitric acid are denitrified in an oxygen-free tank to remove nitrogen gas. This denitrification treatment is performed using a hydrogen donor in organic matter contained in the waste water. However, the organic matter contained in the methane fermentation treated water after the methane fermentation treatment is small. Therefore, when the methane fermentation treated water is to be treated with biological nitrogen, there is a shortage of hydrogen donors used for denitrification treatment in an oxygen-free tank. The present invention solves this shortage of hydrogen donors and can favorably perform denitrification treatment in an oxygen-free tank.

  The organic waste water treatment apparatus 103 according to the third aspect of the present invention is the downstream of the methane fermentation treatment tank 10 as shown in FIGS. 8 and 9, for example, in the waste water treatment apparatus 102 according to the second aspect of the present invention. And the dissolved methane collection | recovery tank 70 provided in the upstream of the reaction tank 40 is provided. The dissolved methane recovery tank 70 includes a gas blowing device 71 for blowing one gas or two or more mixed gases of carbon dioxide, nitrogen, air, and inert gas into the methane fermentation treated water 2 in the dissolved methane recovery tank 70. And a supply unit 72 for supplying the methane gas recovered by blowing the gas to the oxygen-free tank 41.

  If comprised in this way, dissolved methane can be expelled from methane fermentation treated water and collect | recovered as methane gas by blowing gas other than methane gas, such as a carbon dioxide, nitrogen, air, and an inert gas, into a dissolved methane collection | recovery tank. Furthermore, in the case of dissolved methane, the amount of methane supplied to the anoxic tank is determined by the amount of methane fermentation treatment water, whereas when recovered as methane gas, the amount of methane supplied to the anoxic tank is adjusted. can do.

  The organic waste water treatment apparatus 103 according to the fourth aspect of the present invention is the downstream of the methane fermentation treatment tank 10 as shown in FIGS. 8 and 10 in the waste water treatment apparatus 102 according to the second aspect of the present invention. And the dissolved methane collection | recovery tank 80 provided in the upstream of the reaction tank 40 is provided. The dissolved methane recovery tank 80 has a supply unit 82 that causes the methane fermentation treated water 2 to naturally flow down due to a height difference and supplies methane gas recovered by degassing caused by the natural flow to the oxygen-free tank 41.

  If comprised in this way, a negative pressure will arise in a dissolved methane collection | recovery tank by the natural flow of methane fermentation treated water. Thereby, since dissolved methane deaerates from methane fermentation treated water, it can collect | recover as methane gas. Furthermore, in the case of dissolved methane, the amount of methane supplied to the anoxic tank is determined by the amount of methane fermentation treatment water, whereas when recovered as methane gas, the amount of methane supplied to the anoxic tank is adjusted. can do.

  The organic waste water treatment apparatus 104 according to the fifth aspect of the present invention is the waste water treatment apparatus 102 according to the second aspect of the present invention, for example, as shown in FIG. A suction device 46 is further provided for sucking a gas phase portion generated in the methane fermentation treatment tank 10 when moving from the treatment tank 10 to the oxygen-free tank 41. The suction device 46 includes a supply unit 47 that supplies methane gas collected by sucking the gas phase part to the oxygen-free tank 41.

  If comprised in this way, the inside of the methane fermentation processing tank 10 will become a more negative pressure by the suction | inhalation of the suction device 46, and it can prevent more that the methane dissolved in methane fermentation treated water diffuses out of a tank. Furthermore, in the case of dissolved methane, the amount of methane supplied to the anoxic tank is determined by the amount of methane fermentation treatment water, whereas when recovered as methane gas, the amount of methane supplied to the anoxic tank is adjusted. can do.

  The organic waste water treatment apparatus 105 according to the sixth aspect of the present invention is the downstream of the methane fermentation treatment tank 10 in the waste water treatment apparatus 101 according to the first aspect of the present invention as shown in FIG. And a methane oxidation tank 90 provided upstream of the reaction tank 20. The methane oxidation tank 90 has a carrier on which methane oxidizing bacteria are immobilized.

  If comprised in this way, it can have the methane oxidation microbe fixed in the methane oxidation tank. Therefore, the amount of methane oxidizing bacteria can be increased, and as a result, the size of the tank for oxidizing methane can be made compact.

  The organic waste water treatment apparatus 106 according to the seventh aspect of the present invention is the downstream of the methane fermentation treatment tank 10 in the waste water treatment apparatus 101 according to the first aspect of the present invention as shown in FIG. And a methane oxidation tank 90 provided upstream of the reaction tank 20. The methane oxidation tank 90 has a carrier on which methane oxidizing bacteria are immobilized, and has an inflow portion through which the aerobic treated water 4 processed in the reaction tank 20 and solid-liquid separated by the solid-liquid separator 30 flows into the tank. Have.

  If comprised in this way, in the methane oxidation tank 90, the dissolved methane contained in the methane fermentation treated water is oxidized by the dissolved oxygen contained in the aerobic treated water. Furthermore, nitric acid and nitrous acid produced by nitrification contained in the aerobic treated water are satisfactorily denitrified due to the presence of intermediate products (such as methanol) produced by oxidation of dissolved methane.

  The organic waste water treatment method according to the eighth aspect of the present invention includes, for example, as shown in FIG. 1, a methane fermentation treatment step of subjecting the organic waste water 1 to methane fermentation treatment; and methane fermentation treated in the methane fermentation treatment step. A biological treatment step for aerobic biological treatment of methane dissolved in the treated water 2; after the methane fermentation treatment step, the methane fermentation treated water 2 is added to the biological treatment step in a state in which the methane is prevented from being released into the atmosphere. And a supplying step.

  If comprised in this way, it is methane produced by the methane fermentation treatment process, Comprising: It can prevent that the methane which is not collect | recovered as methane gas but dissolves in treated water diffuses in air | atmosphere. Furthermore, the dissolved methane can be transferred to a biological treatment process without being released into the atmosphere, and can be oxidatively decomposed into carbon dioxide and water in the biological treatment process.

  The organic wastewater treatment method according to the ninth aspect of the present invention is the wastewater treatment method according to the eighth aspect of the present invention, for example, as shown in FIG. A denitrification treatment step and an aerobic treatment step for aerobic biological treatment. The biological treatment step includes a step of supplying the aerobic treatment water in the aerobic treatment step to the denitrification treatment step. In the step of supplying the methane fermentation treated water 2 to the biological treatment step, the methane fermentation treated water 2 is supplied to the denitrification treatment step of the biological treatment step. In the opportunity treatment step, a nitrification solution is generated from ammonia contained in the methane fermentation treated water 2. In the denitrification treatment step, the nitrification solution is denitrified using organic matter generated by oxidation of dissolved methane in the methane fermentation treated water.

If comprised in this way, the dissolved methane contained in methane fermentation treated water will be transferred to a denitrification process, without being lost by diffusion. In the aerobic treatment process, NH ₄ —N is oxidized to NO ₂ —N and NO ₃ —N by nitrifying bacteria, and a nitrifying solution is generated. By transferring the methane fermentation treated water containing dissolved methane and the nitrification solution to the denitrification treatment process, intermediate products (such as methanol) generated by oxidation of the dissolved methane are removed from the denitrification treatment process. It can be used as a donor to denitrify the nitrification solution. In this way, the dissolved methane is effectively utilized for the denitrification treatment.

  According to the present invention, methane generated by methane fermentation treatment and dissolved in methane fermentation treatment water can be easily treated without being released into the atmosphere. Therefore, it is possible to prevent methane from being released into the atmosphere and contribute to global warming countermeasures.

It is a block diagram of the organic waste water treatment equipment 101 which concerns on the 1st Embodiment of this invention. 1 is a schematic view of a UASB tank 10. FIG. 1 is a schematic view of a reaction tank 20 and a sedimentation basin 30. FIG. It is a block diagram of the organic waste water treatment equipment 102 which concerns on the 2nd Embodiment of this invention. 1 is a schematic view of a reaction tank 40 and a sedimentation basin 30. FIG. 1 is a schematic view of a reaction tank 50 and a sedimentation basin 30. FIG. 1 is a schematic view of a reaction tank 60 and a sedimentation basin 30. FIG. It is a block diagram of the organic waste water treatment equipment 103 which concerns on the 3rd Embodiment of this invention. 3 is a schematic view of a dissolved methane recovery tank 70. FIG. 3 is a schematic view of a dissolved methane recovery tank 80. FIG. It is a block diagram of the organic waste water treatment equipment 104 which concerns on the 4th Embodiment of this invention. It is a block diagram of the organic waste water treatment equipment 105 which concerns on the 5th Embodiment of this invention. It is a block diagram of the organic waste water treatment equipment 106 which concerns on the 6th Embodiment of this invention. It is a block diagram of the conventional apparatus 201 which processes organic wastewater to a methane fermentation process and an aerobic biological process. It is the schematic of the conventional UASB tank 10 '. It is the schematic of the conventional reaction tank 20 'and the sedimentation basin 30. It is a graph which shows the relationship between water temperature and the solubility with respect to the water of methane. It is a figure which shows the table | surface (Table 1) of the inflowing sewage state used in Examples 1-4 and Comparative Examples 1-4. It is a figure which shows the table | surface (Table 2) of the experimental conditions of Example 1 and Comparative Example 1. It is a figure which shows the table | surface (Table 3) of the experimental result of Example 1 and the comparative example 1. FIG. It is a figure which shows the table | surface (Table 4) of the experimental conditions of Example 2 and Comparative Example 2. It is a figure which shows the table | surface (Table 5) of the experimental result of Example 2 and Comparative Example 2. FIG. It is a figure which shows the table | surface (Table 6) of the experimental conditions of Example 3 and Comparative Example 3. It is a figure which shows the table | surface (Table 7) of the experimental result of Example 3 and Comparative Example 3. FIG. It is a figure which shows the table | surface (Table 8) of the experimental conditions of Example 4 and Comparative Example 4. It is a figure which shows the table | surface (Table 9) of the experimental result of Example 4 and the comparative example 4. FIG. It is a figure which shows the table | surface (Table 10) of the experimental conditions of Example 5 and Comparative Example 5. It is a figure which shows the table | surface (Table 11) of the experimental result of Example 5 and Comparative Example 5. FIG.

  Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or corresponding parts are denoted by the same or similar reference numerals, and redundant description is omitted. Further, the present invention is not limited to the following embodiments. In particular, any of the UASB method, the fixed bed method, and the fluidized bed method can be applied to the methane fermentation treatment. In the following embodiments, a UASB method that is most suitable for methane fermentation treatment will be described as an example.

  The organic waste water treatment apparatus and the organic waste water treatment method of the present invention are for the purpose of preventing dissolved methane from being released into the atmosphere without being recovered in the treated water without being recovered by the methane fermentation treatment. This was realized by a configuration in which dissolved methane was transferred to a subsequent aerobic biological treatment in a state where it was prevented from being released to the outside of the tank and processed in the aerobic biological treatment.

  With reference to FIG. 1, the organic waste water treatment equipment 101 which concerns on the 1st Embodiment of this invention is demonstrated. The organic wastewater treatment apparatus 101 includes a UASB tank 10 as a methane fermentation treatment tank, a reaction tank 20, and a sedimentation basin 30 as a solid-liquid separator. As shown in FIG. 1, the organic waste water 1 is first subjected to methane fermentation in a UASB tank 10. Next, the UASB treated water 2 as the methane fermentation treated water is subjected to an aerobic biological treatment in the reaction tank 20. The mixed liquid 3 flowing out from the reaction tank 20 is solid-liquid separated in the sedimentation basin 30, and the supernatant liquid (aerobic treated water 4) is discharged after being subjected to chlorine sterilization or the like.

  FIG. 2 shows the UASB tank 10. The UASB tank 10 has a lid 11 at the top and a GSS (gas-solid-liquid separator) 12 inside. Furthermore, it has the piping 13 as a supply part for transferring the UASB treated water 2. In the UASB tank 10, the easily decomposable organic matter in the organic waste water 1 is decomposed into methane gas and carbon dioxide in the sludge bed 14 composed of methane fermentation microorganisms. The generated methane gas or the like is recovered via the GSS 12 and used effectively.

  However, part of the methane gas dissolves in the UASB treated water 2 and exists as dissolved methane. This dissolved methane may be released from the surface of the UASB treated water 2 and diffused into the atmosphere. For this reason, the UASB tank 10 has the cover part 11 in an upper part, and prevents that dissolved methane is diffused from the inside of the UASB tank 10 in air | atmosphere. In addition, the cover part 11 may seal the UASB tank 10 completely, or may be sealed with a gap that does not prevent the dissolved methane from being released into the atmosphere. That is, the lid 11 only needs to prevent the gas in the UASB tank 10 from flowing out of the tank, and there may be a gap through which air flows from the outside of the tank into the tank, such as when the inside of the tank has a negative pressure. . Specifically, the upper portion of the UASB tank 10 may be covered with a lid fixed with bolts as the lid portion 11.

  Furthermore, the UASB treated water 2 is transferred to the reaction tank 20 in a state where dissolved methane is prevented from being diffused into the atmosphere. That is, as shown in FIG. 2, the UASB treated water 2 is transferred to the reaction tank 20 through the pipe 13 of the UASB tank 10 without contacting the atmosphere. Thus, the UASB tank 10 can transfer the UASB treated water 2 to the reaction tank 20 while preventing the dissolved methane contained in the UASB treated water 2 from being diffused outside the tank. In addition, as a supply part of the UASB tank 10, a water channel having a lid may be used instead of the pipe 13. In addition, when the UASB tank 10 and the reaction tank 20 are installed adjacent to each other, the supply unit is a part where the UASB treated water 2 flows out of the UASB tank 10.

The reaction tank 20 is preferably an immersion type processing tank. “Immersion type” means activated sludge treatment or biofilm treatment for supplying aerobic biological treatment by supplying air, oxygen-enriched air, pure oxygen, or the like while the treatment tank is filled with a treatment solution. . That is, it refers to a treatment method in which the treatment reaction is performed while immersed in a treatment solution. Specific examples of submerged aerobic biological treatment include floating aerobic biological treatment (continuous activated sludge treatment, batch activated sludge treatment, oxidation method, biofilm treatment, etc.), fluidized bed biological treatment (inclusive) Immobilization method, bond immobilization method, etc.).
Therefore, for example, a biofilm treatment, such as a sprinkling filter bed, in which the treatment liquid is sprinkled on the filter medium and brought into contact with oxygen in the atmosphere is not included. In the case of a treatment such as a trickling filter, the ratio of gas in the treatment tank is high (the ratio of gas and liquid in the space other than the filter medium is 60 to 95% for gas and 40 to 5% for liquid), so UASB treatment Before the dissolved methane contained in the water 2 is decomposed by the methane oxidizing bacteria, it is physically easily diffused from the UASB treated water 2 and discharged into the atmosphere. For this reason, in order to prevent discharge | emission of methane, the equipment which processes a methane separately is needed and it is not preferable.
The “state filled with the treatment liquid” does not necessarily mean a state where the treatment tank is filled with the treatment liquid. Regardless of whether the processing liquid stays in the processing tank or flows in the processing tank, at least the processing liquid may be in a state of being stored in the processing tank. In addition, “air, oxygen-enriched air, pure oxygen, or the like” may be any gaseous oxidant that supplies oxygen into the treatment liquid and enables an oxidation reaction.

  As an example of the aerobic biological treatment, a case where the UASB treated water 2 is treated with activated sludge using the reaction tank 20 and the sedimentation basin 30 shown in FIG. 3 will be described. The reaction tank 20 has an aeration tank (that is, an aerobic tank) 21a for aerobic biological treatment, and an aeration line 22 for supplying oxygen into the tank. Furthermore, it has the cover part 23 which prevents that the gas in a tank diffuses in air | atmosphere. The UASB treated water 2 is supplied from the UASB tank 10 via the pipe 13 to the aeration tank 21a. The outlet of the pipe 13 is arranged so as to be under the water surface of the aeration tank 21a. Further, the outlet of the pipe 13 is preferably installed at a position closer to the bottom of the aeration tank. For example, in the case of an aeration tank having an effective water depth of 5 m, a position within 1 m, preferably within 50 cm from the bottom of the aeration tank is preferable. That is, it is preferable that the dissolved methane contained in the UASB treated water 2 stays longer in the aeration tank 21a. Furthermore, when the rate at which dissolved methane is biologically decomposed in the aeration tank 21a and the speed at which the dissolved methane is physically released from the aeration tank 21a are taken into consideration, the emission rate is faster. Therefore, it is preferable to install a lid 23 (or cover) on the upper part of the aeration tank 21a to prevent the dissolved methane from being diffused outside the tank. By carrying out like this, the dissolved methane contained in the UASB treated water 2 can be efficiently oxidized and decomposed by the methane oxidizing bacteria, and methane emission due to physical emission can be prevented. The dissolved methane contained in the UASB treated water 2 is decomposed into water and carbon dioxide by the methane oxidizing bacteria present in the activated sludge in the aeration tank 21a. Thus, the organic waste water treatment apparatus 101 can be oxidatively decomposed and mineralized by the methane oxidizing bacteria in the aeration tank 21a without releasing the dissolved methane contained in the UASB treated water 2 into the atmosphere.

FIG. 3 shows the sedimentation basin 30. The sedimentation basin 30 includes a sedimentation tank 31 and a return sludge pump 32.
In the sedimentation site 30, the mixed liquid 3 that has flowed out of the reaction tank 20 is separated into aerobic treated water 4 (that is, activated sludge treated water 4) that is a supernatant and activated sludge 5 that precipitates. A part of the precipitated activated sludge 5 is returned to the aeration tank 21a as the return sludge 5 by the return sludge pump 32. The aerobic treated water 4 is discharged after the disinfection treatment or the like is performed.
In addition, as above-mentioned, the liquid mixture 3 is a liquid mixture containing the aerobic treated water 4 and the activated sludge 5. In the present specification, the aerobic treated water contained in the mixed liquid 3 is also referred to as aerobic treated water 4. That is, the aerobic treated water 4 refers to treated water that has been subjected to aerobic biological treatment in a reaction tank (aeration tank or aerobic tank).

  The organic waste water treatment apparatus 101 according to the first embodiment has been described as an apparatus that includes the reaction tank 20 and the sedimentation site 30 (solid-liquid separation device) shown in FIG. I can't. For example, a batch activated sludge method that also serves as a reaction tank as a solid-liquid separator may be used. Further, a membrane separation activated sludge method (MBR) using a biofilm instead of a sedimentation basin as a solid-liquid separator may be used. In the case of MBR, a membrane separation apparatus equipped with a biofilm is installed outside the reaction tank in place of the sedimentation basin, or is installed inside the reaction tank to perform solid-liquid separation. In biological nitrogen treatment, if the NOx-N concentration of treated water is 10 mg / L or more, a problem of sludge floating due to denitrification occurs in the sedimentation basin. However, when MBR is applied, the above problem does not occur because solid-liquid separation of sludge is performed with a membrane. The solid-liquid separation device also includes a biofilm filtration device used in a submerged fixed bed system. That is, when the aerobic treatment is an immersion type fixed bed system or the like, in order to immobilize aerobic organisms, a subsequent settling basin or the like may be removed. In that case, the biofilm filtration device becomes a solid-liquid separation device that performs solid-liquid separation.

  With reference to FIG. 4, the organic waste water treatment apparatus 102 which concerns on the 2nd Embodiment of this invention is demonstrated. The organic waste water treatment apparatus 102 includes a reaction tank 40 in place of the reaction tank 20 in the organic waste water treatment apparatus 101 of FIG. Since the UASB tank 10 and the sedimentation place 30 are the same, description is abbreviate | omitted.

  FIG. 5 shows the reaction tank 40. The reaction tank 40 has an oxygen-free tank 41 in front of the aerobic tank 21b which is an aeration tank. Specifically, the tank is partitioned by a partition plate 44, and continuously one oxygen-free tank 41 and three aerobic tanks 21b, that is, an oxygen-free tank 41 / aerobic tank 21b / aerobic tank 21b / aerobic tank 21b. To be configured. The anaerobic tank 41 has an underwater stirrer 42, and the aerobic tank 21b has an aeration line 22 similar to the aeration tank 21a. Furthermore, the oxygen-free tank 41 preferably has a lid 43 that prevents dissolved methane from being diffused into the atmosphere from the tank.

In general, in methane fermentation treatment, easily decomposable organic substances in the wastewater are decomposed and removed and recovered as methane gas. On the other hand, if organic substances such as proteins are contained in the wastewater, these are decomposed and NH. _4- N will remain in the methane fermentation treated water. In the methane fermentation treated water containing NH ₄ -N, the BOD / NH ₄ -N ratio is low, and in the subsequent aerobic biological treatment, the nitrification reaction of NH ₄ -N (oxidation of ammoniacal nitrogen) proceeds. When the aerobic biological treatment is activated sludge treatment, if the nitrification reaction proceeds and the NOx-N concentration in the activated sludge treatment liquid increases, problems such as sludge floating due to denitrification occur in the sedimentation basin after the reaction tank. To do.
Furthermore, in regions where nitrogen regulation is severe, there are cases where biological nitrogen treatment is applied in aerobic biological treatment after methane fermentation treatment. In this case, as described later, since a hydrogen donor is insufficient in the denitrification step, it is necessary to add an external substrate such as methanol, which causes a problem that a running cost is required.

  In the reaction tank 40 of the organic waste water treatment apparatus 102, biological nitrogen treatment is performed using the aerobic tank 21b and the anoxic tank 41 together with the oxidative decomposition of dissolved methane in the aerobic tank 21b. Biological nitrogen treatment is divided into a nitrification process in which ammonia is oxidized to nitrous acid and nitric acid by nitrifying bacteria, and a denitrification process in which nitrous acid and nitric acid are converted to nitrogen gas by denitrifying bacteria. The nitrification process is processed in the aerobic tank 21b, and the denitrification process is processed in the oxygen-free tank 41. Specifically, as shown in FIG. 5, the mixed liquid 3 containing the nitrification liquid nitrified in the aerobic tank 21b is returned to the anoxic tank 41 using the circulation pump 45, mixed with the UASB treated water 2 and denitrified. To do.

The denitrification treatment is performed using a hydrogen donor in organic matter contained in the waste water. Therefore, in biological nitrogen treatment, raw water (drainage containing organic matter) before treatment is usually supplied to an anoxic tank and used as a hydrogen donor, and then transferred to an aerobic tank. However, in methane fermentation treatment, easily degradable organic substances are converted into methane gas by absolute anaerobic bacteria (obligate anaerobic bacteria). Therefore, there are few organic substances contained in methane fermentation treated water. Therefore, when the biological nitrogen treatment is performed on the methane fermentation treated water, there arises a problem that the hydrogen donor for denitrification is deficient in the oxygen-free tank. In order to solve these problems, the organic wastewater treatment apparatus 102 of the present application uses dissolved methane contained in the methane fermentation treated water (UASB treated water 2) as a hydrogen donor for denitrification. Methane oxidizing bacteria are known to produce organic substances such as methanol as intermediate products in the process of decomposing methane as follows.
CH ₄ → CH ₃ OH → HCHO → HCOOH → CO ₂
Source: Ikuo Kato, Mitsuyoshi Ueda: Development of microbial functions Chapter 2 Microorganisms that protect the environment p. 39-p. 43 Kyoto University Academic Press (2008)
Furthermore, when the methane load is high or the oxygen supply is insufficient in the methane oxidation treatment, the methane is not decomposed into carbon dioxide and water by the methane oxidizing bacteria, and may stop in the state of intermediate products (such as methanol). .

In the present invention, this intermediate product (mainly methanol) is considered to have acted as a hydrogen donor. That is, NH ₄ —N is oxidized to NO ₂ —N and NO ₃ —N by nitrifying bacteria in the aerobic tank 21 b. The mixed liquid 3 containing this nitrification liquid is returned to the anoxic tank 41 by the circulation pump 45 and mixed with the UASB treated water 2. The mixed liquid 3 contains dissolved oxygen (DO). In the anaerobic tank 41, dissolved methane contained in the UASB treated water 2 is methane oxidized by dissolved oxygen (DO) contained in the mixed solution 3. However, since oxygen supply is insufficient with respect to the amount of methane, it is considered that oxidized methane exists as an intermediate product (such as methanol). This intermediate product acts as a hydrogen donor for denitrification, and it is considered that the denitrification process proceeded in the oxygen-free tank 41.
In actual methane oxidation treatment, when methane is not decomposed into carbon dioxide and water and stops in the state of an intermediate product (methanol or the like), specifically, at DO level, 0.5 to 1 mg / L or less It is. Methane load in the water temperature _{16 ℃, 0.1~0.2mgCH 4 / gMLVSS /} d or more, the water temperature _{20 ℃, 0.13~0.26mgCH 4 / gMLVSS /} d or more, the water temperature 25 ° C., 0.26 ˜0.45 mg CH ₄ / gMLVSS / d or more is a standard.
In the organic waste water treatment apparatus 102, the shortage of hydrogen donor for denitrification can be sufficiently reinforced by an intermediate product such as methanol that is considered to be generated by oxidation of dissolved methane. Therefore, it is possible to prevent the problem of sludge floating in the sedimentation basin 30 from occurring. Moreover, since it is not necessary to add an external substrate, the running cost can be reduced as compared with the conventional apparatus. Furthermore, when the circulation pump 45 is used, there is an advantage that the amount of the mixed liquid 3 to be returned can be easily adjusted.

For example, when sewage of CODcr 400 mg / L is subjected to UASB treatment under conditions of a water temperature of 20 ° C. and HRT of 10 h, at a CODcr removal rate of 50%, half of the removed CODcr can be recovered as methane gas and the other half is dissolved in the UASB treated water. Accordingly, the CODcr concentration of the dissolved methane gas is about 100 mg / L. On the other hand, the UASB treated water has a soluble BOD of 40 mg / L, a soluble CODcr of 100 mg / L, and NH ₄ -N is around 30 mg / L, and the UASB treated water-soluble BOD containing dissolved methane is 120 mg / L (BOD / CODcr = 0 .8)). UASB-treated water BOD / NH ₄ −N = 4.0, which makes it possible to supply a sufficient hydrogen donor for biological nitrogen treatment. Thus, in this Embodiment using the reaction tank 40 shown in FIG. 5, dissolved methane can be used effectively.

  In addition, when processing a methane fermentation treated water using a membrane separation activated sludge method (MBR), and installing a membrane separation apparatus in the reaction tank 40, a membrane separation apparatus is used for the final treatment tank of the aerobic tank 21b. (The same applies to the reaction tanks 50 and 60).

  The reaction tank 50 will be described with reference to FIG. In the organic waste water treatment apparatus 102, the reaction tank 50 shown in FIG. 6 may be used instead of the reaction tank 40 shown in FIG. In the reaction tank 50, an anaerobic tank 41 is provided in front of the aerobic tank 21b, and arranged so that step denitrification can be performed alternately with the anaerobic tank 41 / aerobic tank 21b / anaerobic tank 41 / aerobic tank 21b. And biological nitrogen treatment. If comprised in this way, biological nitrogen treatment will be attained, without providing the circulation pump 45 (refer FIG. 5) which requires motive power. The UASB treated water 2 containing dissolved methane is supplied to the anoxic tank 41, respectively. In this way, nitrification is performed in the aerobic tank 21b and denitrification is performed in the anaerobic tank 41. That is, the mixed liquid 3 containing dissolved oxygen and nitrification liquid in the aerobic tank 21b flows into the anoxic tank 41 immediately after that, and further mixed with the UASB treated water 2 containing dissolved methane to perform denitrification treatment. The number of aerobic tanks 21b and anaerobic tanks 41 is preferably 2 or more respectively, and the number of tanks is set according to the TN (Total Nitrogen) concentration level of aerobic treated water 4. It is preferable to set. The final processing tank is an aerobic tank 21b. In the aerobic tank 21b of the final processing tank, a finishing process of the remaining organic matter is performed. Moreover, as shown in FIG. 6, it is preferable to provide a lid portion 43 in the aerobic tank 21b because it is possible to prevent undecomposed dissolved methane from being diffused into the atmosphere from the inside of the tank. The gas or the like (exhaust gas) in the tank is preferably supplied separately to an exhaust gas treatment device (not shown) via a pipe or the like. Examples of the exhaust gas treatment method include biological deodorization treatment, chemical solution cleaning, and physical treatment such as activated carbon.

  The reaction tank 60 will be described with reference to FIG. In the organic waste water treatment apparatus 102, the reaction tank 60 shown in FIG. 7 may be used instead of the reaction tank 40 shown in FIG. In the reaction tank 60, an aerobic tank 21b is provided at the top of the tank, and the aerobic tank 21b / anaerobic tank 41 / aerobic tank 21b / anaerobic tank 41 / aerobic tank 21b are arranged. Perform nitrogen treatment. If comprised in this way, biological nitrogen treatment will be attained, without providing the circulation pump 45 (refer FIG. 5) which requires motive power. The UASB treated water 2 containing dissolved methane is supplied to the anoxic tank 41, respectively. In this way, nitrification is performed in the aerobic tank 21b and denitrification is performed in the anoxic tank 41. The number of aerobic tanks 21b and anaerobic tanks 41 is preferably 2 or more, and the number of tanks is preferably set according to the TN concentration level of aerobic treated water 4. The final processing tank is an aerobic tank 21b.

  With reference to FIG. 8, the organic waste water treatment equipment 103 which concerns on the 3rd Embodiment of this invention is demonstrated. The organic waste water treatment apparatus 103 includes a dissolved methane recovery tank 70 between the UASB treatment tank 10 and the reaction tank 40 (50, 60) in the organic waste water treatment apparatus 102 of FIG. A part or all of the UASB treated water 2 is passed through the dissolved methane recovery tank 70 (solid arrow), and a gas other than methane gas is blown into the UASB treated water 2 in the dissolved methane recovery tank 70. A mixed gas containing methane gas released from the UASB treated water 2 (dotted arrow) is collected and blown into the anoxic tank 41 of the reaction tank 40 (50, 60). An apparatus (not shown) such as a blower or a fan is used for collecting and blowing methane gas.

  FIG. 9 shows a dissolved methane recovery tank 70. The dissolved methane recovery tank 70 includes a gas blowing line 71 as a gas blowing apparatus for blowing a gas other than methane gas, and a pipe 72 as a supply unit that supplies a mixed gas containing methane gas to the oxygen-free tank 41. The dissolved methane recovery tank 70 is a bubble tower type. The UASB treated water 2 is retained in the dissolved methane recovery tank 70, and a gas other than methane gas is blown from the lower part to drive out the dissolved methane, thereby recovering methane. The gas other than methane gas is preferably carbon dioxide, nitrogen, air, other inert gas, or a mixed gas of two or more thereof, particularly preferably carbon dioxide and nitrogen. In the organic waste water treatment apparatus 103, since the dissolved methane contained in the UASB treated water 2 is supplied as a gaseous methane gas to the anoxic tank 41, the amount of methane gas to be blown can be adjusted.

  Instead of the dissolved methane recovery tank 70, a dissolved methane recovery tank 80 shown in FIG. 10 may be used. The dissolved methane recovery tank 80 has a pipe 82 as a supply unit that supplies a mixed gas containing methane gas to the anoxic tank 41. The dissolved methane recovery tank 80 has a multi-stage tank configuration in which the tank is tilted so that the natural flow of the UASB treated water 2 is possible using the height difference and the inside of the tank is partitioned by a partition plate 81. The natural flow creates a negative pressure in the tank, and the dissolved methane is degassed. Or the dissolved methane collection | recovery tank 80 is good also as a cascade structure which makes a step difference in a tank, makes a level difference, and can flow naturally. Specifically, the water channel for transferring the UASB treated water 2 may be provided with a height difference and further provided with a lid.

  With reference to FIG. 11, the organic waste water treatment equipment 104 which concerns on the 4th Embodiment of this invention is demonstrated. The organic waste water treatment device 104 is further provided with a blower 46 as a suction device in the organic waste water treatment device 102 of FIG. The blower 46 has a pipe 47 as a supply unit that supplies a mixed gas containing methane gas to the oxygen-free tank 41. In the organic waste water treatment apparatus 104, the gas phase part in the pipe 13 of the UASB treatment tank 10 is sucked using a blower, and a part of the dissolved methane is recovered as methane gas. The recovered methane gas is blown into the anoxic tank 41. In addition, it is good also as a structure which attracts | sucks the gaseous-phase part in the UASB processing tank 10 main body with a blower. In the organic waste water treatment apparatus 104, the dissolved methane contained in the treated water is supplied to the anoxic tank 41 as a gaseous methane gas, so that the amount of methane gas to be blown can be adjusted. Further, the suction of the blower makes the inside of the UASB treatment tank 10 including the pipe 13 more negative pressure, and it is possible to further prevent the dissolved methane from being released to the outside of the UASB treatment tank 10.

With reference to FIG. 12, the organic waste water treatment apparatus 105 which concerns on the 5th Embodiment of this invention is demonstrated. The organic waste water treatment apparatus 105 is further provided with a methane oxidation tank 90 in the organic waste water treatment apparatus 101 of FIG.
When the dissolved methane contained in the UASB-treated water 2 is to be treated with methane oxidizing bacteria, the amount of organisms is small when carried out by a floating method such as activated sludge treatment, so the treatment tank needs to be enlarged. As a countermeasure against this, methane oxidizing bacteria may be immobilized on a carrier for treatment. In FIG. 12, a gas blowing line for supplying UASB treated water 2 containing dissolved methane from a tank bottom to a methane oxidation tank 90 having a carrier on which methane oxidizing bacteria are immobilized, and further supplying oxygen into the tank. To supply air from the bottom to treat the dissolved methane. Dissolved methane is decomposed into water and carbon dioxide by immobilized methane oxidizing bacteria. In addition, the supply amount of the UASB treated water 2 may be either a part or the whole amount. When supplying the whole quantity to the methane oxidation tank 90, the reaction tank 20 of FIG.
In the organic waste water treatment apparatus 105, the methane oxidation tank 90 has a carrier on which methane oxidizing bacteria are immobilized, so that the amount of methane oxidizing bacteria can be increased, resulting in a compact tank size for oxidizing dissolved methane. be able to. As the immobilization carrier used in the methane oxidation tank 90, pumice, activated carbon, plastic filter media, or the like can be used. A carrier having an uneven surface is suitable for bioadhesiveness. The size of the carrier is 5 to 20 mm, preferably 7 to 12 mm.

  With reference to FIG. 13, the organic waste water treatment apparatus 106 which concerns on the 6th Embodiment of this invention is demonstrated. The organic waste water treatment apparatus 106 further includes a methane oxidation tank 90 that does not blow air in the organic waste water treatment apparatus 101 of FIG. The methane oxidation tank 90 has a carrier on which methane oxidizing bacteria and denitrifying bacteria are immobilized. Further, the methane oxidation tank 90 has a pipe as a supply unit that supplies the aerobic treated water 4 processed in the reaction tank 20 and solid-liquid separated in the sedimentation place 30 to the methane oxidation tank 90. In the organic waste water treatment apparatus 106, the UASB treated water 2 and the aerobic treated water 4 containing dissolved methane are supplied to the methane oxidation tank 90 from the bottom of the tank. The aerobic treated water 4 contains a large amount of nitrous acid and nitric acid that have undergone a nitrification reaction, and further contains 4 to 8 mg / L of dissolved oxygen. In the methane oxidation tank 90, dissolved methane contained in the UASB treated water 2 is oxidized by the methane oxidizing bacteria, while the nitrification liquid (including nitrous acid and nitrate nitrogen) contained in the aerobic treated water 4 is denitrifying bacteria. Is denitrified. In addition, the supply amount of the UASB treated water 2 may be either a part or the whole amount. In the organic waste water treatment device 106, the amount of methane oxidizing bacteria and denitrifying bacteria can be increased by using immobilized bacteria instead of floating bacteria in the methane oxidation tank 90, resulting in a compact tank size. be able to.

In the above embodiment, an example of an apparatus that effectively uses dissolved methane for biological nitrogen treatment has been described. However, the amount of dissolved methane depends on the amount of dissolved liquid water, the water temperature, and the gas composition ratio of CH ₄ and CO ₂ . Therefore, in the above embodiment, it may be insufficient for use as a hydrogen donor for denitrification in the aerobic tank 41. In such a case, a part of the methane gas generated in the UASB tank 10 that is not dissolved in the UASB treated water 2 and recovered as methane gas may be supplied to the anoxic tank 41.

  Examples of the present invention will be described below. However, the embodiments of the present invention are not limited to the following embodiments. In Examples 1 to 4 and Comparative Example 4, the inflow sewage shown in Table 1 of FIG. 18 is used as organic waste water, and a UASB tank (effective capacity 940 L) and an activated sludge tank (effective total capacity 940 L) as a reaction tank. ) Was used for the experiment. In each example, UASB treated water (methane fermentation treated water) was transferred to a submerged reaction tank and biological treatment was performed in a state where dissolved methane was prevented from being diffused into the atmosphere. On the other hand, in Comparative Examples 1 to 3, the dissolved methane is transferred to the submerged reaction tank without being prevented from being diffused into the atmosphere, that is, in a state where the UASB treated water is in contact with the atmosphere, and biological treatment is performed. It was.

[Example 1 / Comparative Example 1]
Table 2 in FIG. 19 shows the experimental conditions. FIG. 1 shows the configuration of the apparatus used in Example 1. The experiment was conducted at a water temperature of 18 to 29 ° C. and a water amount of 333 L / d (HRT for 8 hours for both UASB treatment and activated sludge treatment).
Table 3 in FIG. 20 shows the measurement results of the dissolved methane concentration. The dissolved methane concentration was measured by a head space GC (gas chromatography) method. In Example 1, the UASB tank _26.6mL-CH 4 / L, UASB process water 2 (activated sludge raw water) in _26.3mL-CH 4 / L, in the activated sludge treated water 4 _0mL-CH 4 / L there were. On the other hand, in Comparative Example 1, 26.6 mL-CH ₄ / L in the UASB tank, 5.9 mL-CH ₄ / L in the UASB treated water 2 (activated sludge raw water), and 0 mL-CH _{4 in} the activated sludge treated water _4. / L. In Example 1, dissolved methane is mineralized by activated sludge treatment without being released from the UASB treated water 2 into the atmosphere.

[Example 2 / Comparative Example 2]
Table 4 in FIG. 21 shows the experimental conditions. 4 and 5 show the configuration of the apparatus used in the second embodiment. In Comparative Example 2, the UASB treated water 2 was supplied to the anoxic tank 41 in the state of being in contact with the atmosphere in the apparatus of FIG.
Table 5 in FIG. 22 shows the experimental results. UASB process water 2 _NH 4 -N26mg / L, with respect to T-N34mg / L, the activated sludge treated water 4 of Example _2, NH 4 -N5mg / _L, was T-N10mg / L. The activated sludge treated water 4 of Comparative Example _2, NH 4 -N5mg / _L, was T-N25mg / L. In Example 2, since the denitrification in the anaerobic tank 41 can be performed satisfactorily, the TN removal rate is 70.6%, whereas in Comparative Example 2, nitrification proceeds in the aerobic tank 21b. However, the denitrification in the oxygen-free tank 41 was insufficient for the hydrogen donor, so that the TN removal rate was 26.5%.

[Example 3 / Comparative Example 3]
Table 6 in FIG. 23 shows the experimental conditions. 4 and 6 show the configuration of the apparatus used in Example 3. FIG. In Comparative Example 3, the UASB treated water 2 was supplied to the anoxic tank 41 in the state of being in contact with the atmosphere in the apparatus of FIG.
Table 7 in FIG. 24 shows the experimental results. _NH 4 -N28mg / L of UASB process water 2, while T-N39mg / L, the activated sludge treated water 4 of Example _3, NH 4 -N6mg / _L, was T-N10mg / L. The activated sludge treated water 4 of Comparative Example _3, NH 4 -N6mg / _L, was T-N25mg / L. In Example 3, since the denitrification in the anoxic tank 41 can be performed well, the TN removal rate is 74.4%, whereas in Comparative Example 3, nitrification proceeds in the aerobic tank 21b. However, the denitrification in the oxygen-free tank 41 was insufficient for the hydrogen donor, so the TN removal rate was 35.9%.

[Example 4 / Comparative Example 4]
Table 8 in FIG. 25 shows the experimental conditions. FIG. 13 shows the configuration of the apparatus used in Example 4. As an experimental machine for the methane oxidation tank 90, a transparent column made of vinyl chloride having a diameter of 60 mm and a height of 1.5 m was used. 0.94 L of garden pumice (hereinafter referred to as pumice) was filled as a filter medium. A filter medium (pumice) having a particle size of 5 to 15 mm was used. The porosity was 48%. The UASB treated water 2 and the activated sludge treated water 4 were supplied to the transparent column at a ratio of 1.6: 1 without aeration. On the other hand, in Comparative Example 4, only the UASB treated water 2 was supplied to the transparent column with ventilation.
Table 9 in FIG. 26 shows the experimental results. In Comparative Example 4 (average water temperature 25 ° C.), the inflow water to the transparent column was TN 42 mg / L and NH ₄ —N 26.3 mg / L, whereas the outflow water from the transparent column was TN 40.9 mg. / L, NH ₄ —N 22.5 mg / L, and there is almost no change in the properties of the influent and effluent with respect to the denitrification treatment.
In Example 4 (average water temperature 25 ° C.), the inflow water to the transparent column was T-N 37.7 mg / L, NH ₄ —N 17 mg / L, NO ₃ —N 11 mg / L, while the outflow water from the transparent column was T _{-N28.6mg / L, NH 4 -N15.9mg /} L, a NO 3 -N0.6mg / L, the denitrification treatment, T-N removal rate 24.1% results.

[Example 5 / Comparative Example 5]
Table 10 in FIG. 27 shows the experimental conditions. 4 and 5 show the configuration of the apparatus used in Example 5. FIG. In Example 5, the UASB treated water 2 of the food production wastewater was caused to flow into the oxygen-free tank in a state where dissolved methane was prevented from being released into the atmosphere. In Comparative Example 5, dissolved methane was allowed to flow into the anoxic tank without preventing the methane from being diffused into the atmosphere, that is, in a state where the UASB treated water 2 was in contact with the atmosphere.
Table 11 in FIG. 28 shows the experimental results. UASB process water 2 _NH 4 -N28mg / L, with respect to T-N37mg / L, the activated sludge treated water 4 of Example _5, NH 4 -N0.5mg / _L, was T-N8.5mg / L . In the activated sludge treated water 4 of Comparative Example 5, they were NH ₄ -N 0.5 mg / L and TN 22 mg / L. In Example 5, denitrification in the anaerobic tank 41 can be satisfactorily performed, so that the TN removal rate is 77.0%, whereas in Comparative Example 5, nitrification proceeds in the aerobic tank 21b. However, the denitrification in the oxygen-free tank 41 was deficient in hydrogen donors, so that the TN removal rate was 40.5%. Thus, a high TN removal rate was also obtained in the treatment of food production wastewater.

1 Organic drainage
2 UASB treated water, methane fermentation treated water 3 Liquid mixture
4 Aerobic treated water, activated sludge treated water
5 activated sludge, return sludge
10, 10 'UASB tank, methane fermentation treatment tank 11, 23, 43 Lid
12 GSS
13, 47, 72, 82 Piping, supply unit 14 Sludge bed 20, 20 ', 40, 50, 60 Reaction tank 21a Aeration layer 21b Aerobic layer
22 Aeration line
30 Solid-liquid separator, sedimentation basin
31 Precipitation tank 32 Return sludge pump 41 Oxygen-free tank 42 Underwater agitator 44, 81 Partition plate 45 Circulation pump 46 Blower 70, 80 Dissolved methane recovery tank 71 Gas blowing line 90 Methane oxidation tank 101, 102, 103, 104, 105, 106 Organic wastewater treatment equipment

Claims (4)

A methane fermentation tank for methane fermentation of organic wastewater;
A submerged reaction tank for aerobic biological treatment of the methane fermentation treated water treated in the methane fermentation treatment tank;
A solid-liquid separation device for solid-liquid separation of the mixed liquid in the reaction vessel;
The methane fermentation treatment tank is configured to prevent the methane dissolved in the methane fermentation treatment water in the methane fermentation treatment tank from being diffused into the atmosphere and the dissolved methane from being diffused into the atmosphere. A supply unit for supplying the methane fermentation treated water while maintaining the state,
A methane oxidation tank provided on the downstream of the methane fermentation treatment tank and upstream of the reaction tank and having a carrier on which methane oxidizing bacteria are immobilized ;
The methane oxidation tank has an inflow portion for allowing the aerobic treated water treated in the reaction tank and solid-liquid separated by the solid-liquid separation device to flow into the tank.
Organic wastewater treatment equipment. The reaction tank has an anaerobic tank for denitrification treatment and an aerobic tank for aerobic biological treatment,
The anaerobic tank and the aerobic tank have a configuration in which the aerobic treated water treated in the aerobic tank flows into the anaerobic tank from the aerobic tank,
The methane fermentation treated water is supplied to the anoxic tank,
The organic waste water treatment apparatus according to claim 1. A methane fermentation treatment process for methane fermentation of organic wastewater;
A biological treatment step of treating the methane fermentation treated water treated in the methane fermentation treatment step with an aerobic biological treatment;
After the methane fermentation treatment step, supplying the methane fermentation treatment water in a state in which methane dissolved in the methane fermentation treatment water is prevented from being diffused into the atmosphere;
A methane oxidation step of decomposing the dissolved methane with immobilized methane oxidizing bacteria after the methane fermentation treatment step and before the biological treatment step ;
The methane oxidation step includes an inflow step for causing the aerobic treated water that has been treated and solid-liquid separated in the biological treatment step to flow into the methane oxidation step.
Organic wastewater treatment method. The biological treatment step has a denitrification treatment step for denitrification treatment and an aerobic treatment step for aerobic biological treatment,
The biological treatment step has a step of supplying the aerobic treatment water in the aerobic treatment step to the denitrification treatment step,
In the biological treatment step, the methane fermentation treated water is supplied to the denitrification treatment step of the biological treatment step,
In the aerobic treatment step, a nitrification solution is generated from ammonia contained in the methane fermentation treated water,
In the denitrification treatment step, the nitrification solution is denitrified using an organic substance generated by oxidation of dissolved methane in the methane fermentation treated water.
The organic waste water treatment method according to claim 3 .

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