JP3700935B2 - Anaerobic treatment method and apparatus - Google Patents

Description

【００３０】
実施例２
Ｃ，Ｄ系列ともに、傾斜する邪魔板を３ケ取り付け、装置側壁と邪魔板との角度を３０度とし、原水に消泡剤を添加し、散気管から発生ガスを吹き込む、スカムの破壊・除去機能を付加した系列である。
液層部の容量は１ｍ³である。リアクター内の水温は５６℃になるように温度制御されている。原水には、食品工場から排出される有機性廃棄物及び活性汚泥処理設備の余剰汚泥の混合物を用いた。原水のＴＳは１０ｇ／リットル、ＣＯＤ_Cr（以下、ＣＯＤと記す）は１８ｇ／リットルである。Ａ系列及びＢ系列では原水を酸発酵処理した後、リアクターに供給した。Ｃ系列では原水を粉砕機で粉砕し、平均粒径を５０μｍ以下として酸発酵処理した後、リアクターに供給した。Ｄ系列では平均粒径２ｍｍの原水を粉砕しないで酸発酵処理した後、リアクターに供給した。Ｃ系列が本発明法である。
【００３１】
Ｃ，Ｄ系列ともに発生ガスの散気管からの吹き込みは１日当たり２回とし、流出液を原水とともにリアクターに流入させ、通水速度を１ｍ／ｈに設定した。
図５に実験経過と流出液の酢酸濃度、ＣＯＤ分解率の処理成績の変化を示し、（ｇ）はＣＯＤ負荷の変化を、（ｈ）は流出液酢酸濃度の変化を、（ｉ）はＣＯＤ分解率の変化を示す。
Ｃ系列では、１１０日後以降にＣＯＤ負荷１５ｋｇ／ｍ³／ｄで流出液の酢酸濃度が５００ｍｇ／リットル以下、ＣＯＤ分解率７５％の処理が可能であった。
一方、Ｄ系列ではＣＯＤ負荷を１ｋｇ／ｍ³／ｄで運転を行っていたが、２０日後以降、流出液の酢酸濃度が１０００ｍｇ／リットル以上と高くなり、ＣＯＤ分解率が３０％以下に低下した。これは平均粒径２ｍｍの固形分を含む廃水を処理することでリアクター内に固形分が堆積し、グラニュール汚泥が処理水とともに流出し、処理性能が低下したためである。
【００３２】
【発明の効果】
本発明によれば、装置本体側壁との角度が３５度以下、かつ、各占有面積が装置断面積の２分の１以上となる邪魔板により形成されるガス・液・固分離部を多段に有する上向流嫌気性汚泥床処理装置を使用することにより、リアクター内の発生ガス・処理水・汚泥の分離性能が向上し、リアクター内のグラニュール汚泥保持量が高まり、かつ流入する有機性廃棄物を粉砕し、平均粒径２００μｍ以下のスラリーとし、原水を処理水の循環液や系外から供給する希釈水により必要に応じて適宜希釈を行うことにより、一貫して、流入水のリアクター内部における装置断面積基準の通水速度が０．０５〜５ｍ／ｈとなるように調節することができ、それによって原水中の固形分はリアクター内にとどまることなく処理水とともに系外に流出させることができる。
さらに、消泡剤を添加することによって、前記ガス・液・固分離部内部での発泡及びスカムの形成を防止すること、及びガス・液・固分離部内部に酸素を含有しない気体を吹き込むことにより、このガス・液・固分離部内部でのスカムの形成を防止することができる。
これらにより、廃水中の有機性固形分、厨芥、その他の有機性廃棄物を対象とした高性能な上向流嫌気性汚泥床処理が達成できる嫌気性処理方法と、これを実施する装置を提供することができる。
【図面の簡単な説明】
【図１】本発明の上向流嫌気性処理装置の一形態を例示した模式図。
【図２】従来の上向流嫌気性処理装置の一形態を例示した模式図。
【図３】実験に用いたＡ〜Ｃ系列で使用した処理装置を示す図であり、（ａ）はＡ系列で、（ｂ）はＢ系列で、（ｃ）はＣ系列でそれぞれ使用した処理装置である。
【図４】実施例１における実験経過と流出液酢酸濃度とＣＯＤ処理成績の変化を示す図であり、（ｄ）はＣＯＤ負荷の変化を、（ｅ）は流出液酢酸濃度の変化を、（ｆ）はＣＯＤ分解率の変化を示す。
【図５】実施例２における実験経過と流出液酢酸濃度とＣＯＤ処理成績の変化を示す図であり、（ｇ）はＣＯＤ負荷の変化を、（ｈ）は流出液酢酸濃度の変化を、（ｉ）はＣＯＤ分解率の変化を示す。
【符号の説明】
１ 原水送液管
２ リアクター
３ 邪魔板
４ａ 区分スラッジゾーン
４ｂ 区分スラッジゾーン
４ｃ 区分スラッジゾーン
５ ＧＳＳ部
５ａ 気相部
５ｂ 気泡部
６ 発生ガス回収配管
７ 水封槽
８ ガスメータ
９ 処理水配管
１０ 消泡剤
１１ ガスホルダー
１２ 散気管
１３ 発生ガス吹き込み配管
１４ 粉砕機
１５ 有機性廃棄物
２１ 流入原水
２２ リアクター
２３ 汚泥層
２４ 処理水
２５ ＧＳＳ部
２６ ガス排出管
２７ 攪拌装置
２８ 攪拌翼
２９ モーター[0001]
BACKGROUND OF THE INVENTION
The present invention relates to an anaerobic sludge bed treatment method and apparatus for detoxifying organic solid waste, etc. discharged from various factories, sewage, human waste, livestock industry facilities, etc. The present invention relates to a method and apparatus for treating an upflow anaerobic sludge bed having multiple stages of gas / liquid / solid separation sections (hereinafter also referred to as “GSS sections”).
[0002]
[Prior art]
Compared with aerobic treatment such as activated sludge method, the methane fermentation treatment method that treats organic solids, soot, and other organic waste in wastewater does not require energy for aeration and generates excess sludge Since the amount is small and energy can be recovered from the generated biogas, it is excellent in terms of energy saving. However, since methane producing bacteria or methane fermenting bacteria have a small amount of growth and poor sedimentation, microorganisms easily flow out together with the treated water. Therefore, it was difficult to increase the microorganism concentration in the fermenter used for the methane fermentation treatment. Furthermore, there were problems in terms of cost and site.
[0003]
There is an upflow anaerobic sludge bed method (hereinafter also referred to as “UASB”) as a high-efficiency fermenter having a high microorganism concentration. This is a method that has become widespread in recent years. It is characterized by maintaining a high concentration of methane bacteria in the reactor by granulating anaerobic bacteria such as methane bacteria into granules. Even when the concentration of the organic matter in it is considerably high, it can be processed efficiently.
[0004]
[Problems to be solved by the invention]
However, the conventional UASB treatment method (FIG. 2) for organic solids, waste, and other organic waste in wastewater still has the following problems.
(I) When waste water containing organic solids is treated, solids are accumulated in the reactor, and granular sludge flows out together with the treated water, resulting in a reduction in treatment performance.
(B) A scum is formed inside the GSS part, and it becomes difficult to collect the generated gas. In particular, when the load is low and the amount of generated gas is small, the scum destruction / removal action by the generated gas is small and scum is easily formed.
(C) As a result of (b) above, the effect of collecting and discharging the generated gas in the GSS section is lost, causing a large outflow of sludge and causing deterioration of the process.
[0005]
In view of such circumstances, the present invention aims to provide a high-performance upward-flow anaerobic sludge bed treatment method and apparatus for organic solids, waste, and other organic waste in wastewater. And
[0006]
[Means for Solving the Problems]
The present invention has solved the above problems by the means described below.
(1) In a method for anaerobically treating organic waste, a gas / liquid formed by a baffle plate having an angle with the side wall of the apparatus main body of 35 degrees or less and each occupation area being 1/2 or more of the apparatus cross-sectional area · using a solid separation unit upflow anaerobic sludge blanket processing apparatus having the multiple stages, and grinding the organic waste flows, supplied by the following slurry average particle size 200 [mu] m, further, the organic waste An anaerobic treatment method characterized in that treatment is performed by directly or diluting water to be treated .
[0007]
(2) The anaerobic treatment method according to (1), wherein foaming and scum formation are prevented inside the gas / liquid / solid separation part by adding an antifoaming agent to the water to be treated. .
(3) Air that does not contain oxygen is blown into the apparatus to prevent stirring of the sludge layer and formation of scum inside the gas / liquid / solid separation part, and gas that does not contain oxygen blown into the apparatus. The anaerobic treatment method according to the above (1) or (2), wherein the gas / liquid / solid separation part is discharged .
(4) The anaerobic treatment method according to (1), wherein the inflowing organic waste and a part of the treated water of the anaerobic treatment device are mixed and subjected to anaerobic treatment after acid fermentation. .
[0008]
(5) In an upflow anaerobic sludge bed treatment apparatus having gas, liquid, and solid separation sections in multiple stages, the angle with the apparatus side wall is 35 degrees or less, and each occupied area is more than half of the apparatus cross-sectional area. Gas / liquid / solid separation parts formed by the baffle plates to be used are attached in multiple stages, and a pulverizer that pulverizes the inflowing organic waste to an average particle size of 200 μm or less is installed to flow in the water to be treated. An anaerobic treatment apparatus characterized in that a supply pipe is provided at the bottom.
[0009]
The essence of the present invention is that “the inflowing organic waste is pulverized to form a slurry having an average particle size of 200 μm or less, and the raw water is appropriately diluted with the circulating water of the treated water or the dilution water supplied from outside the system. Thus, the solid water content in the raw water can be adjusted so that the flow rate is 0.05 to 5 m / h based on the cross-sectional area of the apparatus inside the reactor. In addition, as an anaerobic treatment device at that time, “the angle with the side wall of the device body is 35 degrees or less and each occupied area is Gas / liquid / solid separation in reactor by using “upward-flow anaerobic sludge bed treatment device with multiple stages of gas / liquid / solid separation part formed by baffle plate that is more than half of the device cross-sectional area” Performance increased It is possible to maintain a high concentration of granular sludge in the reactor, and a high-performance upflow anaerobic sludge bed treatment for organic solids, soot, and other organic waste in wastewater. It can be achieved.
[0010]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, embodiments of the present invention will be described with reference to the drawings, but the present invention is not limited thereto.
FIG. 1 is a diagram illustrating an outline of an embodiment of the upward flow anaerobic treatment apparatus of the present invention that is preferable for carrying out the anaerobic treatment method.
In FIG. 1, one end is fixed to each of the left and right side walls of a cylindrical reactor 2 in which a raw water feed pipe 1 communicates and is closed at the top and bottom, and the other end is connected to the opposite side wall. A baffle plate 3 extending while descending toward the opposite side wall is installed.
[0011]
The baffle plates 3 are alternately provided at three places in the vertical direction on the left and right sides, and form acute slanted section sludge zones 4 a, 4 b, 4 c between the side walls of the reactor 2.
The angle θ formed between the side wall of the reactor 2 and the baffle plate 3 is an acute angle of 35 degrees or less, and the occupied area is ½ or more of the apparatus cross-sectional area.
When the angle exceeds 35 degrees, granular sludge accumulates on the baffle plates 3 in the sludge zones 4a, 4b, and 4c, resulting in insufficient fluidity and formation of dead spaces.
Moreover, when the occupation area of the baffle plate 3 is 1/2 or less, the trapping of the generated gas becomes insufficient, resulting in a problem in the separation of gas and liquid. That is, the gas escapes upward from the center of the reactor 2, and the gas cannot be sufficiently accumulated in the GSS portion 5 described later.
[0012]
The upper part of the divided sludge zones 4a, 4b and 4c forms a GSS part 5. The gas phase part 5a where the generated gas collects when the reaction starts is provided with an outlet to the generated gas recovery pipe 6 that communicates with the outside.
In addition, the discharge port of the generated gas recovery pipe 6 connected from the gas phase part 5a is opened in the water of the water-sealed tank 7 filled with water. The opening position is at an appropriate water depth with different water pressure, and the water sealing tank 7 is provided with a gas meter 8 for measuring the flow rate of the gas discharged from the generated gas recovery pipe 6. A gas holder 11 is provided at the tip of the gas meter 8. Further, a treated water pipe 9 for discharging the supernatant liquid is opened at the upper end of the reactor 2.
[0013]
The reactor 2 is used with granule sludge made of anaerobic bacteria. The anaerobic treatment which is the object of the present invention is an anaerobic treatment in a temperature range of a medium temperature methane fermentation treatment with an optimum temperature of 30 ° C to 35 ° C and a high temperature methane fermentation treatment with an optimum temperature of 50 ° C to 55 ° C. It is targeted. Raw water containing organic solids, waste, and other organic waste 15 in the wastewater, which has been crushed to an average particle size of 200 μm or less, is introduced into the reactor 2 through the feed pipe 1. To do. The raw water is appropriately diluted with the circulating water of the treated water or diluted water supplied from outside the system, and the acid fermentation treatment is performed according to the liquefaction state of the inflowing organic waste 15. 4 hours to 4 days is appropriate.
[0014]
It adjusts so that the water flow rate in the reactor 2 of inflow water may be 0.05-5 m / h. In the reactor 2, the organic waste is decomposed by the anaerobic bacteria, and a decomposition gas is generated. The generated gas is gathered separately in the GSS section 5 at the upper end of each of the divided sludge zones 4a, 4b, 4c, forms a gas phase section 5a in each, and reaches the water sealing tank 7 through the generated gas recovery pipe 6. The amount of the generated gas is recorded by the gas meter 8 and sent to the gas holder 11.
[0015]
Part of the generated gas adheres to the granular sludge in the divided sludge zones 4a, 4b, and 4c, reduces the apparent specific gravity, and accompanies the granular sludge and reaches the water surface of the GSS section 5. Such generated gas forms bubbles and temporarily stays in the water surface bubble portion 5b. The air bubbles gathered in the water surface bubble portion 5b eventually burst, and the generated gas and granulated sludge are separated, and the granular sludge recovers its original specific gravity and is submerged in the water. It is discharged out of the system via the sealing tank 7. The organic matter is decomposed and clarified, and water is discharged from the upper end of the reactor 2 to the outside of the system through the treated water pipe 9.
[0016]
Since the gas pressure in the gas phase part of each GSS part 5 is different, the differential pressure may be adjusted in the water sealing tank 7. It is necessary to keep the water sealing pressure higher in the order closer to the raw water feed side. There are many methods for adjusting the pressure for gas recovery in addition to the method using the water-sealed tank 7. For example, a pressure valve or the like may be used.
In the anaerobic treatment method of the present invention, the generated gas generated in each of the divided sludge zones 4a, 4b, 4c can be recovered, so that the amount of generated gas per unit cross-sectional area of the reactor 2 is reduced.
In particular, the gas amount per unit cross-sectional area of the reactor 2 becomes small at a place closest to the treated water pipe 9 through which treated water flows out. Therefore, the outflow amount of granule sludge can be extremely reduced.
[0017]
In the reactor 2 in which the GSS units 5 are installed in multiple stages, the flow rate of the granular sludge layer is improved by setting the water flow rate to 0.05 to 5 m / h, preferably 0.5 to 5 m / h. The granular sludge of 90% or more in the realter 2 has a particle size of 0.5 to 1.5 mm. Therefore, the organic solid content, waste, and other organic waste 15 in the wastewater are pulverized by a pulverizer 14 to obtain raw water having an average particle size of 200 μm or less, preferably 50 μm or less, thereby forming a granular sludge layer. Since the flow becomes good, the solid content derived from the organic waste is not deposited in the reactor 2 but is subjected to the methane fermentation treatment, and the treated water is increased by increasing the water flow rate to 0.05 to 5 m / h. Leaks with. On the other hand, granular sludge having a larger particle size and specific gravity than the raw water remains in the reactor 2.
[0018]
The anaerobic treatment of the present invention is a medium temperature methane fermentation treatment with an optimum temperature of 30 ° C. to 35 ° C., a high temperature methane fermentation treatment with an optimum temperature of 50 ° C. to 55 ° C., and the water temperature is 30 ° C. or higher. The organic waste 15 in the reactor 2 is pulverized by the pulverizer 14 so that the viscosity of the raw water having an average particle size of 200 μm or less is lowered. Therefore, deterioration of the flow state of the granular sludge layer due to the viscosity of the raw water and outflow of the granular sludge to the outside of the system do not occur.
[0019]
In the case of foaming raw water, the gas phase part 5a and the generated gas recovery pipe 6 in the GSS part 5 are blocked, making it difficult to recover the generated gas. In such a case, foaming in the GSS portion 5 can be suppressed by adding the antifoaming agent 10 to the inflow water to the reactor 2 in advance. Compared with the method in which the antifoaming agent 10 is dropped and sprayed into the GSS section 5, the present method is effective for defoaming in a sealed space. The antifoaming agent 10 has an antifoaming effect according to the raw aqueous state, and is suitable for defoaming the fermentation broth to eliminate the antifoaming effect at an intermediate temperature (30 to 35 ° C.) or high temperature (50 to 55 ° C.). Use no antifoam. As the type of the antifoaming agent 10, any of a silicone-based antifoaming agent and an alcohol-based antifoaming agent can be used. Further, depending on the properties of the raw water, it is possible to prevent the formation of scum by suppressing foaming.
[0020]
When the raw water has a high SS, scum is formed on the surface of the bubble portion in the GSS portion 5 and inside thereof, so that it is difficult to recover the generated gas. In such a case, the generated gas blowing pipe 13 is connected to the diffuser pipe 12, and the generated gas in the gas holder 11 is supplied into the GSS section 5 so that scum can be destroyed or scum can be prevented from being formed. The broken scum is discharged as treated water together with the liquid flow in the reactor 2.
[0021]
Since each of the GSS units 5 can recover the blown gas, the amount of generated gas per unit cross-sectional area of the reactor 2 is small, and particularly in the place closest to the treated water pipe 9 through which the treated water flows out, the per unit cross-sectional area of the reactor 2 The amount of gas is reduced, and the function that can significantly reduce the outflow of granule sludge is not impaired. The air diffuser 12 is disposed below the reactor 2 or below each GSS unit 5. The granular sludge layer is agitated by the blown gas, and the contact between the granular sludge and the influent wastewater becomes good. Especially, when the organic substance load flowing into the reactor 2 main body is small, the amount of gas generated is small. Therefore, the effect of stirring the granular sludge layer by blowing gas is great.
[0022]
The gas blown into the GSS unit 5 to destroy / remove the scum inside the GSS unit 5 does not contain oxygen such as nitrogen gas, and can use a gas that does not affect biological treatment such as methane fermentation. It is desirable to use gas generated by anaerobic treatment. The frequency of blowing the gas depends on the properties of the wastewater, but once a day to once a week, there is an effect of destroying and removing the scum inside the GSS section 5. Moreover, the stirring effect of a sludge layer further increases by making the frequency which blows in gas once or more a day.
[0023]
【Example】
EXAMPLES Hereinafter, although an Example demonstrates this invention concretely, this invention is not limited by these Examples.
[0024]
Example 1
In FIG. 3, the outline | summary of the upward flow anaerobic sludge bed apparatus used for experiment is shown. The A series is a conventional method of anaerobic treatment, and is illustrated as a conventional method in (a). The B series is a conventional method of UASB, and has the structure shown in FIG. 2 as shown in FIG. In the C series, three sloping baffle plates are attached, the angle between the device side wall and the baffle plate is 30 degrees, a defoaming agent is added to the raw water, and a scum destruction / removal function that blows the generated gas from the air diffuser is added. It is a series. The C series is a series based on the present invention, and has the configuration shown in FIG. 1 as shown in (c).
[0025]
The capacity of the liquid layer part is 1 m ³ . The temperature of the water in the reactor is controlled to 56 ° C. The raw water used was a mixture of organic waste discharged from food factories and excess sludge from activated sludge treatment equipment. The raw water TS is 10 g / liter, and COD _Cr (hereinafter referred to as “COD”) is 18 g / liter. In series A and series B, the raw water was subjected to an acid fermentation treatment and then supplied to the reactor. In the C series, raw water was pulverized by a pulverizer, acid-fermented with an average particle size of 50 μm or less, and then supplied to the reactor.
In the C series, the generated gas was blown from the air diffuser twice per day. In Series C, the effluent was introduced into the reactor together with the raw water, and the water flow rate was set to 1 m / h.
[0026]
FIG. 4 shows the course of the experiment and changes in the treatment results of the acetic acid concentration and COD decomposition rate of the effluent, (d) shows the change in COD load, (e) shows the change in effluent acetic acid concentration, and (f) shows the COD. The change in decomposition rate is shown. In the A series, when the COD load was set to 7 kg / m ³ / d after 90 days, the acetic acid concentration in the effluent became as high as 1300 mg / liter due to overload, and the decomposition rate decreased to 30%. When the COD load was 5 kg / m ³ / d after 100 days, the acetic acid concentration in the effluent was stable at 500 mg / liter or less, and the COD decomposition rate was 65%.
[0027]
In the B series, when the COD load was set to 4 kg / m ³ / d after 80 days, the acetic acid concentration in the effluent increased to 1300 mg / liter due to overload, and the COD decomposition rate decreased to 30%. After 90 days, when the COD load was set at 3 kg / m ³ / d, the acetic acid concentration in the effluent was stabilized at 500 mg / liter or less, and the COD decomposition rate became 65%. Foaming and scum formation inside the GSS part were observed, and the recovery of the generated gas was insufficient, and the solid components of raw water were deposited in the reactor, but the COD load input was low and the amount of generated gas was small In addition, the stirring of the sludge layer due to the rise of the generated gas becomes weak. As a result, the dead space of the sludge spreads, the contact between the sludge and the influent wastewater becomes insufficient, and it is difficult to increase the load.
[0028]
On the other hand, the raw water is pulverized by a pulverizer, the average particle size is 50 μm or less, and the GSS part is multistaged to improve granule sludge retention performance. By adding an antifoaming agent, foaming inside the GSS part is achieved. In the C series, which suppresses the formation of scum inside the GSS section by blowing in the generated gas and performs good stirring of the granular sludge layer, the effluent is discharged at a COD load of 15 kg / m ³ / d after 110 days. Treatment with an acetic acid concentration of 500 mg / liter or less and a COD decomposition rate of 75% was possible. In the C series which is the method of the present invention, it is possible to perform a high-load process three times or more compared to the conventional A and B series, and the COD decomposition rate is improved.
Table 1 shows a comparison of processing results for each series.
[0029]
[Table 1]

[0030]
Example 2
For both C and D series, three inclined baffle plates are attached, the angle between the device side wall and the baffle plate is 30 degrees, an antifoaming agent is added to the raw water, and the generated gas is blown from the air diffuser. This is a series with added functions.
The capacity of the liquid layer part is 1 m ³ . The water temperature in the reactor is controlled to 56 ° C. The raw water used was a mixture of organic waste discharged from food factories and excess sludge from activated sludge treatment equipment. The raw water TS is 10 g / liter, and COD _Cr (hereinafter referred to as COD) is 18 g / liter. In series A and series B, the raw water was subjected to an acid fermentation treatment and then supplied to the reactor. In the C series, raw water was pulverized with a pulverizer, acid fermented with an average particle size of 50 μm or less, and then supplied to the reactor. In the D series, raw water having an average particle diameter of 2 mm was subjected to an acid fermentation treatment without being pulverized, and then supplied to the reactor. Series C is the method of the present invention.
[0031]
In both C and D series, the generated gas was blown from the air diffuser twice per day, the effluent was introduced into the reactor together with the raw water, and the water flow rate was set to 1 m / h.
FIG. 5 shows the experimental process, changes in the acetic acid concentration of the effluent, and the processing results of the COD decomposition rate, (g) shows the change in the COD load, (h) shows the change in the effluent acetic acid concentration, and (i) shows the COD. The change in decomposition rate is shown.
In the C series, after 110 days, COD loading of 15 kg / m ³ / d allowed treatment with an acetic acid concentration of effluent of 500 mg / liter or less and a COD decomposition rate of 75%.
On the other hand, in the D series, the operation was performed at a COD load of 1 kg / m ³ / d. However, after 20 days, the acetic acid concentration of the effluent increased to 1000 mg / liter or more and the COD decomposition rate decreased to 30% or less. . This is because by treating wastewater containing solids having an average particle size of 2 mm, solids are deposited in the reactor, and granule sludge flows out together with the treated water, resulting in a reduction in treatment performance.
[0032]
【The invention's effect】
According to the present invention, the gas / liquid / solid separation portion formed by the baffle plate having an angle with the side wall of the apparatus main body of 35 degrees or less and each occupation area being 1/2 or more of the cross-sectional area of the apparatus is provided in multiple stages. By using the upward flow anaerobic sludge bed treatment equipment, the separation performance of the generated gas, treated water and sludge in the reactor is improved, the retained amount of granular sludge in the reactor is increased, and the inflowing organic waste The slurry is pulverized into a slurry with an average particle diameter of 200 μm or less, and the raw water is diluted appropriately as needed with the circulating water of the treated water or the dilution water supplied from outside the system. Can be adjusted so that the water flow rate based on the cross-sectional area of the apparatus becomes 0.05 to 5 m / h, so that the solid content in the raw water flows out of the system together with the treated water without staying in the reactor. Door can be.
Further, by adding an antifoaming agent, preventing foaming and scum formation inside the gas / liquid / solid separation part, and blowing a gas not containing oxygen into the gas / liquid / solid separation part. Thus, the formation of scum inside the gas / liquid / solid separation portion can be prevented.
By these, we provide an anaerobic treatment method that can achieve high-performance upflow anaerobic sludge bed treatment for organic solids, soot, and other organic waste in wastewater, and an apparatus that implements this method can do.
[Brief description of the drawings]
FIG. 1 is a schematic view illustrating one embodiment of an upward flow anaerobic treatment apparatus of the present invention.
FIG. 2 is a schematic view illustrating an example of a conventional upward flow anaerobic treatment apparatus.
FIGS. 3A and 3B are diagrams showing processing apparatuses used in the A to C series used in the experiment, where FIG. 3A is a series A, FIG. 3B is a B series, and FIG. 3C is a process used in the C series; Device.
4 is a graph showing changes in the experimental process, effluent acetic acid concentration, and COD treatment results in Example 1, (d) shows the change in COD load, (e) shows the change in effluent acetic acid concentration, ( f) shows the change in the COD decomposition rate.
FIG. 5 is a graph showing changes in the experimental course, effluent acetic acid concentration and COD treatment results in Example 2, (g) shows the change in COD load, (h) shows the change in effluent acetic acid concentration, ( i) shows the change in the COD decomposition rate.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 1 Raw water feed pipe 2 Reactor 3 Baffle plate 4a Division sludge zone 4b Division sludge zone 4c Division sludge zone 5 GSS part 5a Gas phase part 5b Bubble part 6 Generated gas recovery pipe 7 Water seal tank 8 Gas meter 9 Treated water pipe 10 Defoaming Agent 11 Gas holder 12 Aeration pipe 13 Generated gas blowing pipe 14 Pulverizer 15 Organic waste 21 Inflow raw water 22 Reactor 23 Sludge layer 24 Treated water 25 GSS section 26 Gas discharge pipe 27 Stirrer 28 Stirring blade 29 Motor

Claims (5)

Gas, liquid, and solid separation formed by baffle plates whose angle with the side wall of the device body is 35 degrees or less and each occupied area is more than half of the device cross-sectional area in the method of anaerobically treating organic waste part using upflow anaerobic sludge blanket processing apparatus having the multiple stages, and grinding the organic waste flows, supplied by the following slurry average particle size 200 [mu] m, further, the comprise organic waste An anaerobic treatment method comprising performing treatment by directly or diluting treated water . The anaerobic treatment method according to claim 1 , wherein foaming and scum formation inside the gas / liquid / solid separation part are prevented by adding an antifoaming agent to the water to be treated . Air that does not contain oxygen is blown into the device to prevent sludge layer agitation and scum formation inside the gas / liquid / solid separation section, and gas that does not contain oxygen blown into the device -The anaerobic treatment method according to claim 1 or 2, wherein the anaerobic treatment method is performed by discharging from the solid separation unit . The anaerobic treatment method according to claim 1, wherein an anaerobic treatment is performed after mixing the inflowing organic waste and a part of the treated water of the anaerobic treatment apparatus and subjecting to acid fermentation . In an upflow anaerobic sludge bed treatment device having gas, liquid, and solid separation sections in multiple stages, the angle with the side wall of the device main body is 35 degrees or less, and each occupation area is one half or more of the cross sectional area of the device. Gas / liquid / solid separation parts formed by plates are installed in multiple stages, and a supply pipe for inflowing water to be treated into slurry by installing a crusher for crushing inflowing organic waste to an average particle size of 200 μm or less An anaerobic treatment apparatus characterized by being provided at the bottom.

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