JP2009183910A - Method and apparatus for treating water containing organic substance - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To reduce thermal energy for heating and alkali consumption for pH maintenance required in an anaerobic treatment. <P>SOLUTION: High temperature blow water discharged from a boiler 13 is added to water containing an organic substance introduced to an anaerobic biological reactor 10 and thus the thermal energy for heating the water containing the organic substance can be saved. The anaerobic biological reactor 10 can comprise a methane fermentation tank 12 storing granule sludge and an acid formation tank 11 connected to each other in series. By employing the granule sludge, a high-load, high-speed operation is made possible. The alkali consumption for neutralizing the pH lowered by acid formation can be decreased by adding the blow water to the acid formation tank 11 or the upstream side thereof. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to a biological treatment method and apparatus for anaerobically treating organic material-containing water, and in particular, anaerobic biological treatment method for introducing an organic matter-containing water into a reaction tank holding granule sludge and performing anaerobic biological treatment. And device.

  Biological treatment methods for organic matter-containing water are roughly classified into anaerobic treatments in which methane fermentation is performed and aerobic treatments in which aerobic microorganisms having a high growth rate are used. Anaerobic treatment is suitable for treatment of organic substance-containing water having a high organic substance concentration, and methane gas is obtained. In recent years, the use of anaerobic treatment is increasing in food factories that discharge high concentration of organic substance-containing water.

  The anaerobic treatment method includes a method using floating sludge and a method using granulated sludge in which microorganisms are granulated. Granule sludge has a high density and a large sedimentation property, so that high-load high-speed treatment is possible using granule sludge. Anaerobic treatment using granular sludge is called UASB (Upflow Anaerobic Sludge Blanket) method. In UASB, organic substance-containing water is introduced into a reaction tank holding a sludge blanket formed of granule sludge, and the mixture is brought into contact with the sludge blanket by flowing upward. Similarly, an EGSB method (Expanded Granule Sludge Blanket) in which a sludge blanket is developed at a high expansion rate is also known as a high-load high-speed anaerobic treatment method using granular sludge.

  In the UASB method using granular sludge, etc., it is important to maintain and propagate the granular sludge in order to stably and satisfactorily treat organic-containing water. If the granule sludge cannot be maintained and propagated in the reaction tank, the treatment performance gradually decreases and may eventually become untreatable.

  Various studies have been conducted to stably maintain and propagate granular sludge in the reaction tank. For example, Patent Document 1 describes a method of preventing granule sludge from floating by adding a calcium compound or an iron salt to raw water introduced into an anaerobic biological reaction tank.

Moreover, in order to prevent the microbial activity of anaerobic sludge from decreasing and stabilize the treatment, the organic substance-containing water introduced into the biological treatment tank is appropriately heated. In this case, since it is necessary to give heat energy in order to heat organic substance containing water to the optimal temperature of anaerobic microorganisms, processing cost rises. Furthermore, in the treatment using granule sludge, when methane fermentation is carried out after removing solid organic substances contained in organic substance-containing water and performing methane fermentation, the pH is lowered during the process of acid generation, so an alkali for neutralization. Addition is required.
JP-A-8-141590

  The above-described chemical addition and warming of the water to be treated for stably performing the anaerobic treatment increase the treatment cost. For this reason, it is required to stabilize the anaerobic treatment by an inexpensive means. An object of this invention is to reduce the cost for the heating and pH maintenance at the time of anaerobic treatment.

  The present inventors can solve the above problems by adding concentrated waste water (boiler blow water) discharged from the boiler to the organic matter-containing water, and depending on the properties of the boiler blow water, by adding this to the organic matter-containing water, The present inventors have found that there are cases where the activity of anaerobic microorganisms can be increased and growth can be promoted, and the present invention has been completed. Specifically, the present invention provides the following.

(1) A method for treating organic matter-containing water in which organic matter-containing water and boiler blow water are introduced into an anaerobic biological reaction tank to treat anaerobic organisms.
(2) The said boiler blow water is a processing method of the organic substance containing water as described in (1) containing phosphoric acid.
(3) The said boiler blow water is a processing method of the organic substance containing water as described in (1) or (2) whose pH is 10-12.
(4) The method for treating organic substance-containing water according to any one of (1) to (3), wherein the boiler blow water is obtained by blowing boiler water to which phosphoric acid and / or potassium hydroxide is added.
(5) The method for treating organic substance-containing water according to any one of (1) to (4), wherein the anaerobic biological reaction tank includes an acid generation tank and a methane fermentation tank holding granule sludge.
(6) The said boiler blow water is a treatment method of the organic substance containing water as described in (5) added to the said organic substance containing water in the said acid production tank or the upstream.
(7) An organic matter-containing water treatment apparatus including an anaerobic biological reaction tank,
An apparatus for treating organic matter-containing water comprising a liquid passage for introducing organic matter-containing water and boiler blow water into the anaerobic biological reaction tank.
(8) The said anaerobic biological reaction tank is a processing apparatus of the organic substance containing water as described in (7) containing the methane fermentation tank which hold | maintains an acid production tank and a granular sludge.
(9) The treatment liquid channel includes the raw water pipe connected to the acid generation tank and the blow pipe connected to the raw water pipe or the acid generation tank. .

  ADVANTAGE OF THE INVENTION According to this invention, the usage-amount of the heat energy required in order to warm a to-be-processed water to the temperature suitable for anaerobic processing can be reduced. Moreover, according to this invention, the usage-amount of the alkali added in order to avoid the pH fall at the time of acid production | generation can be reduced. Therefore, according to the present invention, it is possible to reduce costs for heating and maintaining pH when anaerobic treatment is performed. Furthermore, according to the present invention, it is possible to stabilize the anaerobic treatment by utilizing boiler blow water that has conventionally been required to be treated as waste water for discharging sewage.

  The present invention will be described below with reference to the drawings. FIG. 1 is a schematic diagram of an anaerobic treatment apparatus (hereinafter simply referred to as “treatment apparatus”) 1 of organic substance-containing water according to a first embodiment of the present invention. In this embodiment, the anaerobic biological treatment process is divided into an acid generation process and a methane fermentation process, and the anaerobic biological reaction tank 10 includes an acid generation tank 11 that performs acid generation, and a methane fermentation tank 12 that performs methane fermentation. Are connected in series. A raw water pipe 21 is connected to the acid generation tank 11, and the acid generation tank 11 and the methane fermentation tank 12 are connected to each other by a liquid feeding pipe 22 and a circulating liquid pipe 23. The methane fermentation tank 12 is connected with a treated water pipe 24 for taking out treated water and a gas pipe 25 for taking out generated methane gas.

  The acid producing tank 11 holds acid producing bacteria. On the other hand, granular granule sludge is held in the methane fermentation tank 12. The liquid feeding pipe 22 is connected to the lower part of the methane fermentation tank 12, and the liquid sent from the liquid feeding pipe 22 flows upward in the methane fermentation tank 12. A gas-solid-liquid separator (GSS) is provided at the top of the methane fermentation tank 12, and the top of the GSS protrudes from the liquid level in the methane fermentation tank 12. The gas pipe 25 is connected to the upper part of the methane fermentation tank 12, and the treated water pipe 24 communicates with the inside of the GSS.

  In the methane fermentation tank 12, the part where the GSS is installed is a gas-solid-liquid separation part, and the lower part is a reaction part. In the reaction part, granular sludge is developed to form a sludge blanket. Granule sludge is sludge in which microorganisms containing anaerobic microorganisms are self-granulated to form particles having an average particle size of about 0.5 to 3.0 mm, and has excellent sedimentation properties. A part of the liquid in the reaction section is taken out from the circulating liquid pipe 23 and circulated to the acid generation tank 11, and a part thereof is gas-solid separated by GSS. The liquid that has been gas-solid-liquid separated inside the GSS is taken out from the treated water pipe 24.

  In the present invention, anaerobic biological treatment is performed by adding blow water (boiler blow water) discharged from the boiler to the organic substance-containing water. The boiler blow water may be added to the organic substance-containing water in the anaerobic biological reaction tank 10 or in the preceding stage. In the present embodiment, the boiler blow water is configured to be added to the organic substance-containing water at the front stage of the acid generation tank 11. Specifically, a blow pipe 31 connected to the boiler 13 and discharging boiler blow water is connected to the raw water pipe 21. The raw water pipe 21 and the blow pipe 31 constitute a treatment liquid path for introducing a mixed liquid of organic substance-containing water and boiler blow water into the anaerobic biological reaction tank 10.

  Hereinafter, the processing method of organic substance containing water using this processing device 1 is explained. The organic matter-containing water to be treated includes high-concentration organic matter-containing water that is discharged in the food production process, and the organic matter concentration is about 500 to 30,000 mg / L, particularly about 1,000 to 20,000 mg / L. Organic matter-containing water is a suitable treatment target.

  The organic substance-containing water is sent from the raw water pipe 21 to the acid generation tank 11, and boiler blow water is added through a blow pipe 31 connected to the raw water pipe 21 in the middle thereof. Water treatment chemicals such as a cleansing agent, an oxygen scavenger, and a condensate treatment agent are added to the water supplied to the boiler 13 from the water supply pipe 30. These chemicals added to the boiler water are concentrated while circulating in the boiler water system, and the boiler blow water exhibits an alkalinity of about pH 10-12. Moreover, the boiler blow water discharged | emitted from the boiler 13 is as high as about 60-95 degreeC, and when discarding in a sewage etc., it is necessary to neutralize and cool by various means.

  The present invention utilizes boiler blow water, which conventionally required neutralization treatment by acid addition and cooling treatment by heat exchange, as an additive for stabilizing anaerobic biological treatment. It is calculated | required that the boiler blow water added to organic substance containing water by this invention contains phosphoric acid at least, and it is preferable that phosphoric acid concentration is 5-100 mg / L. The boiler blow water preferably further contains 1% by mass or more of potassium hydroxide, the temperature is preferably 60 to 95 ° C., and the pH is preferably 10 to 12. Moreover, it is preferable that saccharides, nitrogen content, and tannin are also contained in boiler blow water.

  On the other hand, boiler blow water containing a chelating agent or a surfactant is avoided in the present invention. In particular, ethylenediaminetetraacetic acid (EDTA) reduces the activity of granular sludge, so the boiler blow water used in the present invention does not substantially contain a chelating agent such as EDTA or NTA (nitrile triacetic acid) (chelating agent concentration). Is less than 3 mg / L). In this invention, it is good to select the water treatment chemical | medical agent added to boiler water so that boiler blow water may become the said property, and to utilize the boiler blow water obtained as an agent which stabilizes anaerobic biological treatment.

  The amount of boiler blow water added is preferably the total amount from the viewpoint of utilization of thermal energy. The addition position of boiler blow water is not limited to this embodiment. For example, when the precipitation tank which isolate | separates a raw | natural water tank and a solid substance is provided before the acid production tank 11, you may add in the middle of the piping which connects a raw | natural water tank, a precipitation tank, or these tanks. Alternatively, boiler blow water may be added to the liquid in the acid generation tank 11. When boiler blow water is added upstream from the acid generation tank 11 or the acid generation tank 11, the boiler blow water can be used as a pH adjuster (alkali) required for acid generation in the acid generation tank 11, and acid generation Use of heat energy can be achieved. Moreover, you may add boiler blow water in the methane fermenter 12 or in front of it. Specifically, the blow pipe 31 may be connected to the liquid feeding pipe 22 to add the boiler blow water after the acid generation tank 11 and before the methane fermentation tank 12, or to the methane fermentation tank 12. Also good.

  In addition, the present invention can be implemented with an apparatus in which the acid generation tank 11 is omitted and acid generation and methane fermentation are performed in the same reaction tank. In this case, the boiler blow water may be added to the organic substance-containing water in the same reaction tank in which acid generation and methane fermentation are performed or in front.

  Thus, the following merit is acquired by adding boiler blow water to organic substance containing water and performing anaerobic biological treatment. First, boiler blow water can be used for pH adjustment with respect to pH reduction accompanying acid generation. Therefore, conventionally, the amount of alkali used for acid fermentation can be reduced, and neutralization treatment required when discharging boiler blow water into sewage or the like can be eliminated.

  Moreover, since the organic substance-containing water is heated by adding high-temperature boiler blow water to the organic substance-containing water, the biological activity of anaerobic microorganisms, particularly granule sludge can be increased. That is, it is possible to increase the biological activity by reducing the cost of heating the anaerobic biological reaction tank 10, and to eliminate the cooling process required when the boiler blow water is discharged into sewage or the like.

  Here, in order to avoid thermal energy loss and stabilize the anaerobic treatment, it is preferable to add to the anaerobic biological reactor 10 so that the temperature of the boiler blow water does not decrease. As a method of suppressing the temperature drop of boiler blow water and adding it to the anaerobic biological reaction tank 10, there is a method of keeping the temperature of a pipe (here, blow pipe 31) for feeding boiler blow water with a heat insulating material. In addition, when the boiler blow water discharged from the boiler is not sent directly to the anaerobic biological reaction tank, that is, when temporarily storing in the storage tank and pumping up the water, the storage tank should also be a heat insulating material. Keep warm. Furthermore, it is good to shorten the residence time in the storage tank of boiler blow water as a minimum required capacity | capacitance of a storage tank.

  In the acid production tank 11, the organic material-containing water to which the boiler blow water is added is treated with acid producing bacteria to produce an organic acid. The blow pipe 31 is connected not only to the raw water pipe 21 but also to the acid generation tank 11, and in order to adjust the pH of the liquid in the acid generation tank 11, boiler blow water may be added to the acid generation tank 11 as appropriate. Good. The acid-generated liquid is sent from the acid generation tank 11 to the methane fermentation tank 12 via the liquid feeding pipe 22.

  In the methane fermentation tank 12, the sludge blanket is formed by developing the granular sludge retained in the tank by passing the acid-generated liquid in an upward flow. Thereby, the contact efficiency of organic substance containing water and granule sludge becomes high. For this reason, in a UASB in which a sludge blanket having a height of about 3 to 5 m is deployed in a methane fermentation tank having a height of about 5 to 7 m, a sludge load of about 0.1 to 0.7 kg-CODcr / kg-VSS / day is passed through. High-load high-speed processing at a liquid speed of about 0.3 to 1.5 m / h is possible. In the EGSB in which a sludge blanket having a height of about 5 to 18 m is developed in a methane fermentation tank having a height of about 7 to 20 m, a sludge load of 0.1 to 1.0 kg-CODcr / kg-VSS / day, a flow rate of 3 to Processing at about 10 m / h is possible.

The organic load on the methane fermenter 12 is preferably 5 to 30 kg-CODcr / m ³ / day, and particularly preferably 8 to 20 kg-CODcr / m ³ / day. The anaerobic biological reaction tank 10 is preferably operated under anaerobic conditions in which oxygen is not supplied, and the temperature of the liquid in the tank is preferably 25 to 40 ° C, particularly 30 to 38 ° C. In the present invention, the boiler blow water is added to the organic substance-containing water and the liquid sent to the anaerobic biological reaction tank 10 is heated, thereby saving the thermal energy required to bring the anaerobic biological reaction tank 10 to the above temperature.

  In the methane fermentation tank 12, the organic acid produced | generated by the acid production tank 11 is decomposed | disassembled by the function of granule sludge, and the gas containing methane is generated. The mixed solution containing the gas generated in the methane fermentation tank 12 and the grown sludge is gas-solid-liquid separated inside the GSS, and the gas is taken out from the gas pipe 25 to the outside of the methane fermentation tank 12. In addition, the liquid component from which sludge has been separated and clarified is taken out of the methane fermentation tank 12 from the treated water pipe 24. The treated water may be further treated by an aerobic biological treatment apparatus (not shown) provided at a later stage.

  Further, the liquid in the methane fermentation tank 12 is taken out from the circulation liquid pipe 23 and circulated in the acid generation tank 11. In this embodiment, the dispensing pipe 23B is branched from the circulating liquid pipe 23, and a part of the liquid circulated from the methane fermentation tank 12 is injected into the liquid feeding pipe 22 via the dispensing pipe 23B.

<Example 1>
Hereinafter, the present invention will be described in more detail based on examples. In the example, an experimental apparatus 2 shown in FIG. 2 was created by imitating the processing apparatus 1 shown in FIG. As the water to be treated, the anaerobic biological treatment was performed by adding the boiler blow water having the properties shown in Table 2 to the organic substance-containing water having the properties shown in Table 1.

In the table, TOC is the total organic carbon concentration, CODcr is the organic concentration indicated by chemical oxygen consumption, NH ₄ -N is the ammonia nitrogen concentration, PO ₄ -P is the phosphoric acid concentration, and SS is the floating substance. Means concentration. Further, the alkalinity indicated by the acid consumption required for adjusting to pH 8.3 is indicated as p alkali, and the alkalinity indicated by the acid consumption required for adjusting to pH 4.8 is indicated as m alkali. .

  The acid generation tank 11 was constituted by a 500 mL Erlenmeyer flask, placed on the heater H, and appropriately heated. The methane fermentation tank 12 has an inner diameter of 10 cm, a height of 50 m, a reaction part excluding a part where the GSS is installed, and a capacity of the part including the GSS part is 4L.

  Water containing organic matter was passed through the acid generation tank 11 at a CODcr load of 72 g-CODcr / L / day. Moreover, the liquid in the tank taken out from the methane fermentation tank 12 was circulated to the acid generation tank 11 at 3 to 4 mL / min, and boiler blow water was added. The addition ratio of boiler blow water was 2% by mass with respect to circulating water in RUN1, and 10% by mass in RUN2. Although the temperature of boiler blow water was 80 degreeC, it heated with the heater H suitably so that the liquid temperature inside the acid production | generation tank 11 might be set to 35 degreeC. Further, a pH meter P is provided to measure the pH of the liquid in the acid generation tank 11, and a sodium hydroxide solution having a concentration of 1% is appropriately added from the alkali addition pipe 33 so that the value becomes 7. Added to.

  The methane fermentation tank 12 was operated with a CODcr load of 12 g-CODcr / L / day and a sludge load of 0.4 g-CODcr / g-Vss / day (sludge retention amount 30 g-VSS).

  For both RUN1 and RUN2, the granular sludge in the methane fermentation tank 11 was taken out before the start of water flow, was cultured with two kinds of substrates, and the activity was examined. The two types of substrates were an acetic acid substrate and an organic acid mixed (mixed of acetic acid, butyric acid and propionic acid) substrate, respectively. In addition, in RUN1, after 14 days from the start of water flow, in RUN2, after 28 days from the start of water flow, the granule sludge in the methane fermentation tank 11 is taken out, and the activity when each of the above two types of substrates is given is examined. The particle size was measured and the average particle size was determined.

  In the RUN 1 of Example 1, the activity of the granular sludge in the methane fermentation tank 12 is 0.22 kg-CODcr / kg-vss / day before the water flow and 0. It was 27 kg-CODcr / kg-vss / day. Further, in the case of the organic acid mixed substrate, it was 0.38 kg-CODcr / kg-vss / day before water passage, and 0.52 kg-CODcr / kg-vss / day 14 days after the start of water passage. The average particle size of the granular sludge was 1.8 mm at the start of water flow and was 1.8 mm 14 days after the start of water flow.

  In RUN2 of Example 1, the activity of the granular sludge in the methane fermentation tank 12 is the same as that of RUN1 before passing water in the case of an acetic acid substrate, and is 0.28 kg-CODcr / kg-vss / 28 days after the start of passing water. It was a day. Further, in the case of the organic acid mixed substrate, it was the same as RUN1 before water passage, and was 0.53 kg-CODcr / kg-vss / day after 28 days from the start of water passage. The average particle size of the granular sludge was the same as RUN1 at the start of water flow and was 2.1 mm after 28 days from the start of water flow.

<Example 2>
As Example 2, instead of the boiler blow water used in Example 1, boiler blow water further containing an acrylic acid polymer was used. When other conditions were tested in the same manner as in Example 1, in RUN 1 of Example 2, the activity of granular sludge in the methane fermentation tank 12 was 0.25 kg- CODcr / kg-vss / day was 0.27 kg-CODcr / kg-vss / day 14 days after the start of water flow. Further, in the case of the organic acid mixed substrate, it was 0.37 kg-CODcr / kg-vss / day before water passage and 0.48 kg-CODcr / kg-vss / day 14 days after the start of water passage. The average particle size of the granular sludge was 1.8 mm at the start of water flow and 2.0 mm after 14 days from the start of water flow.

  In the RUN 2 of Example 2, the activity of the granular sludge in the methane fermentation tank 12 is the same as that of the RUN 1 before the water flow in the case of the acetic acid substrate, and 0.28 kg-CODcr / kg-vss after 28 days from the start of the water flow. / Day. Further, in the case of the organic acid mixed substrate, it was the same as RUN1 before water passage, and was 0.50 kg-CODcr / kg-vss / day after 28 days from the start of water passage. The average particle size of the granular sludge was the same as RUN1 at the start of water flow and was 2.1 mm after 28 days from the start of water flow.

<Reference Example 1>
As Reference Example 1, instead of the boiler blow water used in Example 1, boiler blow water containing an acrylic acid polymer was used instead of not containing phosphate ions. When other conditions were tested in the same manner as in Example 1, in RUN 1 of Reference Example 1, the activity of the granular sludge in the methane fermentation tank 12 was 0.22 kg- CODcr / kg-vss / day was 0.28 kg-CODcr / kg-vss / day 14 days after the start of water flow. Further, in the case of the organic acid mixed substrate, it was 0.35 kg-CODcr / kg-vss / day before water passage and 0.40 kg-CODcr / kg-vss / day 14 days after the start of water passage. The average particle size of the granular sludge was 1.8 mm at the start of water flow and was 1.8 mm 14 days after the start of water flow.

  In RUN2 of Reference Example 1, the activity of the granular sludge in the methane fermentation tank 12 is the same as that of RUN1 before passing water in the case of an acetic acid substrate, and 0.28 kg-CODcr / kg-vss 28 days after the start of passing water. / Day. Moreover, in the case of the organic acid mixed substrate, it was the same as RUN1 before water flow, and was 0.51 kg-CODcr / kg-vss / day after 28 days from the start of water flow. The average particle diameter of the granular sludge was the same as RUN1 at the start of water flow and was 1.8 mm 28 days after the start of water flow.

<Reference Example 2>
As Reference Example 2, instead of the boiler blow water used in Example 1, boiler blow water containing no chelate agent (EDTA) but no phosphate ions was used. When other conditions were tested in the same manner as in Example 1, in RUN 1 of Reference Example 2, the activity of granular sludge in the methane fermentation tank 12 was 0.24 kg- Although it was CODcr / kg-vss / day, it became 0.21 kg-CODcr / kg-vss / day 14 days after the start of water flow. Further, in the case of the organic acid mixed substrate, it was 0.38 kg-CODcr / kg-vss / day before water passage, but 0.30 kg-CODcr / kg-vss / day after 14 days from the start of water passage. Became. The average particle diameter of the granular sludge was 1.8 mm at the start of water flow, but became 1.7 mm after 14 days from the start of water flow.

  In the RUN 2 of Comparative Example 1, the activity of the granular sludge in the methane fermentation tank 12 is the same as that of the RUN 1 before passing water in the case of an acetic acid substrate, and 0.18 kg-CODcr / kg-vss after 28 days from the start of passing water. / Day. Moreover, in the case of the organic acid mixed substrate, it was 0.20 kg-CODcr / kg-vss / day, the same as RUN1 before water flow, and 28 days after the start of water flow. The average particle diameter of the granular sludge was the same as RUN1 at the start of water flow and was 1.7 mm after 28 days from the start of water flow.

<blank>
Instead of the boiler blow water used in Example 1, pure water heated to 80 ° C. was used as a blank. When other conditions were tested in the same manner as in Example 1, in the case of blank RUN1, the activity of the granular sludge in the methane fermentation tank 12 was 0.22 kg-CODcr / Although it was kg-vss / day, it became 0.20 kg-CODcr / kg-vss / day 14 days after the start of water flow. Further, in the case of the organic acid mixed substrate, 0.38 kg-CODcr / kg-vss / day before the water flow was 0.35 kg-CODcr / kg-vss / day after 14 days from the start of the water flow. Became. The average particle diameter of the granular sludge was 1.8 mm at the start of water flow and was 1.8 mm 14 days after the start of water flow.

  In the case of blank RUN2, the activity of granule sludge in the methane fermenter 12 is the same as that of RUN1 before passing water in the case of an acetic acid substrate, and 0.21 kg-CODcr / kg-vss / day after 28 days from the start of passing water. Met. Moreover, in the case of the organic acid mixed substrate, it was 0.35 kg-CODcr / kg-vss / day, the same as RUN1 before water flow, and 28 days after the start of water flow. The average particle diameter of the granular sludge was the same as RUN1 at the start of water flow and was 1.8 mm 28 days after the start of water flow.

Table 2 shows the properties of boiler blow water or pure water added to the organic-containing water in Examples 1 and 2, Reference Examples 1 and 2, and blanks.

About the granule activity in Example 1, 2, Reference Example 1, 2, and a blank, the result at the time of measuring with an acetic acid substrate is shown in FIG. 3, and the result at the time of measuring with an organic acid substrate is shown in FIG. In both figures, (A) shows the result of RUN1, and (B) shows the result of RUN2. Table 3 shows changes in the average particle diameter of granules in Examples 1 and 2, Reference Examples 1 and 2, and RUN1 and RUN2 of the blank.

Furthermore, about Example 1, 2, Reference Example 1, 2, and a blank, the total usage-amount of the alkali for neutralization used during the experiment period of 28 days and the total usage-amount of the electric power for to-be-processed water heating are shown in Table 4. .

  As shown in Table 4, in Examples 1 and 2 and Reference Examples 1 and 2, it was possible to reduce the amount of neutralizing alkali used and the amount of power used. Moreover, as shown in FIG. 3 and FIG. 4, when boiler blow water does not contain a chelating agent, by adding boiler blow water to organic substance-containing water, not only the amount of alkali used and the amount of power used can be reduced, but also granulated It was shown that the activity can be increased. Furthermore, as shown in Table 3, it was shown that the growth of anaerobic microorganisms can be promoted when the boiler blow water contains phosphoric acid.

  The present invention can be suitably used for the treatment of organic substance-containing water.

The schematic diagram of the anaerobic processing apparatus of the organic substance containing water which concerns on one Embodiment of this invention. The schematic diagram of the anaerobic processing apparatus used for experiment. The graph which shows an experimental result. The graph which shows an experimental result.

Explanation of symbols

1, 2 Anaerobic treatment device 10 Anaerobic biological reaction tank 11 Acid production tank 12 Methane fermentation tank 13 Boiler 21 Raw water pipe (treated liquid channel)
31 Blow piping (treated liquid path)

Claims (9)

  An organic matter-containing water treatment method in which organic matter-containing water and boiler blow water are introduced into an anaerobic biological reaction tank to treat anaerobic organisms.   The said boiler blow water is a processing method of the organic substance containing water of Claim 1 containing phosphoric acid.   The method for treating organic substance-containing water according to claim 1 or 2, wherein the boiler blow water has a pH of 10 or more and 12 or less.   The method for treating organic substance-containing water according to any one of claims 1 to 3, wherein the boiler blow water is obtained by blowing boiler water to which phosphoric acid and / or potassium hydroxide is added.   The said anaerobic biological reaction tank is a processing method of the organic substance containing water in any one of Claim 1 to 4 containing the methane fermentation tank holding an acid production tank and granule sludge.   The said boiler blow water is a treatment method of the organic substance containing water of Claim 5 added to the said organic substance containing water in the said acid production tank or the upstream. An organic matter-containing water treatment apparatus including an anaerobic biological reaction tank,
An apparatus for treating organic matter-containing water comprising a liquid passage for introducing organic matter-containing water and boiler blow water into the anaerobic biological reaction tank.   The said anaerobic biological reaction tank is a processing apparatus of the organic substance containing water of Claim 7 containing the methane fermentation tank which hold | maintains an acid production tank and granule sludge.   The treatment liquid channel according to claim 8, wherein the liquid channel to be treated includes a raw water pipe connected to the acid generation tank, and a blow pipe connected to the raw water pipe or the acid generation tank.