TW201446660A - Anaerobic treatment method - Google Patents

Abstract

Provided is an anaerobic treatment method which enables the treatment of organic discharged water having a high solid concentration with high efficiency and at low facility cost. Raw water having a solid concentration of 1000 mg/L or more is treated in an acid generation vessel (1), then the treated water is supplied to a pH adjusting vessel (2) by means of a pump (P1) to adjust the pH value of the water, and then the pH-adjusted water is allowed to pass through a reaction vessel (3), in which a fluid non-biological carrier (4) is filled, in an upward flow direction by means of a pump (P2). A portion of outflowing water from the reaction vessel (3) is circulated into the pH adjusting vessel (2) as circulating water, and the remainder of the outflowing water is discharged to the outside of the system as treated water.

Description

Anaerobic treatment

The present invention relates to an anaerobic treatment method which has fluidity in a reaction tank, fills a non-biological carrier, forms a biofilm on the surface of the non-biological carrier, and circulates the treated water under anaerobic conditions.

An anaerobic treatment method for organic drainage is to form a small-sized sludge having a large sedimentation density at a high density in a reaction tank, and to cause an organic wastewater containing dissolved BOD to flow upward in water to form a sludge layer. The UASB (Upflow Anaerobic Sludge Blanket) method in which the contact is carried out in a state of high load and high speed processing. The method separates the solid organic matter with slow digestion speed and additionally treats only the dissolved organic matter with high digestion speed by high-load high-speed treatment by using the anaerobic treatment of small granular sludge with high anaerobic microbial density. method. In order to develop the UASB method, an EGSB (Expanded Granule Sludge Blanket) which uses a highly high reaction tank, then passes water at a high flow rate, develops a sludge layer at a high expansion rate, and then performs anaerobic treatment at a high load. )law.

UASB method, EGSB method, etc. A method in which sludge containing anaerobic microorganisms is maintained in a small granular form, which is proliferated and treated. Compared with the case where the sludge is kept in a fixed bed or a fluidized bed on a carrier, the method can achieve high sludge holding concentration, and can be operated at a high load and adjusted by the processing system in operation. The residual sludge can be operated in a short time and is an effective anaerobic treatment.

However, in the case of using a small-sized sludge, when a high-concentration SS component is contained in the drainage, as described in Patent Document 1, it is precipitated by a pretreatment, a pressurized float, a coagulation sediment, a vibrating mesh, and a rotation. After the solid matter is removed by a screen or the like, anaerobic treatment must be performed. The small particle method of UASB, EGSB, etc., when flowing into a high concentration of SS, the SS component causes the small particle layer to be lifted up and causes small particles to flow out.

The anaerobic treatment of the wastewater containing a high concentration of SS is to digest the anaerobic sludge. However, in order to decompose the solid matter, the residence time must be 10 days or more, and it is necessary to have an extremely large reaction tank.

The anaerobic treatment method using a carrier is a method using a fixed bed carrier. In the case of methane fermentation treatment, the organic waste is used for the immobilization of anaerobic microorganisms mainly composed of methanogens, which is used for a carrier made of a synthetic resin which is hydrophilically treated with ozone gas. A microorganism, a methane fermentation treatment method for organic waste subjected to methane fermentation.

However, when an organic wastewater containing a high concentration of SS flows into a fixed bed of the carrier, there is a problem that the SS component is fixed to the surface of the carrier to cause clogging.

In this regard, the method of using a non-biological carrier of fluidity can prevent the carrier from flowing out of the reaction tank by a mechanical method such as a sieve, and the small-concentration COD can be drained or made small because the carrier surface can be ensured as a breeding place for microorganisms. The drainage of the particles disintegrated also has the advantage of being suitable for use.

The fluid non-biological carrier used in the treatment is described in Patent Document 3, which is obtained by the following foams of (I) and/or (II) having a size of 1.0 to 5.0 mm. A fluid non-biological carrier having a precipitation rate of 100 to 500 m/hr.

(I) a foam containing 30 to 95% by weight of a resin component mainly composed of a polyolefin resin and 5 to 70% by weight of a hydrophilizing agent of a cellulose-based powder, and having a foam having a surface in a melt fracture state , (II) A foam containing 30 to 95% by weight of a resin component mainly composed of a polyolefin resin, 4 to 69% by weight of a hydrophilizing agent of a cellulose-based powder, and 1 to 30% by weight of an inorganic powder, and having a surface melting A foam in a broken state.

[Practical Technical Literature] [Patent Literature]

[Patent Document 1] Japanese Patent Laid-Open No. 5-253594

[Patent Document 2] Japanese Special Open 2003-260446

[Patent Document 3] Japanese Special Opening 2012-110843

As described above, the treatment is contained in an anaerobic treatment method using small particles. In the organic drainage of the high-concentration SS, since the high-concentration SS component cannot be introduced into the small-particle-groove, it is necessary to provide a solid-liquid separation device such as a sedimentation tank in advance, which causes an increase in the cost of the entire equipment. The anaerobic treatment method of Patent Document 3 does not describe organic drainage which treats a high SS concentration.

The present invention is directed to providing an anaerobic treatment method capable of efficiently treating organic wastewater having a high concentration of solids at low equipment cost.

The anaerobic treatment method of the present invention has a step of treating organic drainage having a solid concentration of 1000 to 30,000 mg/L in an anaerobic reaction tank having a fluid non-biological carrier.

In the present invention, it is preferred that the organic wastewater is circulated in the reaction vessel so that the solid matter removal treatment is not required.

The size of the carrier is 1.0 to 5.0 mm, and the precipitation speed of the carrier is 100 to 500 m/hr.

The hydrodynamic retention time (HRT) of the reaction tank is preferably from 1 to 120 hr.

The organic wastewater may be passed through the acid generation tank and then passed through the reaction tank.

The reaction tank is preferably a fully mixed type reaction tank or an upward flow type reaction tank.

In the present invention, the non-biological carrier can be caused to flow in the anaerobic reaction tank by flowing the organic wastewater having a high solid concentration in the reaction vessel having the non-biological carrier, and the anaerobic treatment can be efficiently performed.

The non-biological carrier used in the present invention, when compared with small particles, is precipitated even in a drain containing a high concentration of the SS component because of its large specific gravity and rapid precipitation rate. Since the generated gas and the water flow are appropriately stirred and mixed, the thickness of the biofilm is increased to cause natural peeling, and the problem of floating or flow path blockage due to biofilm enlargement can be avoided.

The SS component in the organic wastewater may also precipitate and accumulate inside the reaction tank, but it may be prevented by the use of a fully mixed reaction tank or by increasing the flow velocity of the liquid when the reaction tank is upflowed. problem.

The SS component in organic drainage may also be hydrolyzed by microorganisms and converted into a soluble component. At this time, the solubilized component is subjected to anaerobic biological treatment in the same manner as the originally dissolved component. By making the hydrodynamic retention time of the anaerobic tank 1 to 120 hr, the efficiency of the hydrolysis reaction of the microorganisms by the SS component in the organic drainage can be improved.

The fluid non-biological carrier can be adhered to the carrier by using a sedimentation speed of 1 to 5 mm and a temperature of 100 to 500 m/hr to prevent the carrier from being blocked due to floating, flowing out and solid solution of the carrier, and is formed well. The fluid bed is subjected to a stable and effective anaerobic treatment.

[In order to implement the invention]

Hereinafter, embodiments of the present invention will be described in detail.

In the present invention, an organic drainage having a high solid concentration is circulated in an anaerobic reaction tank filled with a fluid non-biological carrier, and a biofilm is formed on the surface of the non-biological carrier to treat the organic drainage.

The water to be treated to be treated in the present invention is a liquid having a high solid content and containing an organic substance which can be treated by anaerobic treatment by contact with an anaerobic microorganism. The solid concentration is 1000 mg/L or more (for example, 1000 to 30000 mg/L, particularly preferably 1000 to 5000 mg/L). The COD _cr concentration of the organic drainage is preferably 1000 to 60,000 mg/L, particularly preferably about 3,000 to 15,000 mg/L.

The drainage system includes waste water from food factories, organic wastewater such as chemical plants, and semiconductor plant drainage, but is not limited by these.

When a polymer component such as sugar or protein is contained in the water to be treated, an acid generating tank for decomposing the polymer into a low molecular organic acid of acetic acid or propionic acid may be provided as in the anaerobic treatment apparatus used in the following examples. As a pretreatment means for a reaction tank filled with a fluid non-biological carrier.

In this case, the treatment conditions of the acid formation tank differ depending on conditions such as the biodegradability of the water to be treated, and the pH is 5 to 8 (preferably 5.5 to 7.0), and the temperature is 20 to 40 ° C (preferably). The temperature is 25~35°C), and the HRT is 2~24hr (preferably 2~8hr).

When the acid generation tank is sufficiently reduced in molecular weight, the treatment in the reaction tank filled with the fluid non-biological carrier in the subsequent stage can be favorably performed.

When the methanol-producing bacteria containing only methanol, acetic acid or the like is a drainable compound, the treated water can be circulated in a reaction tank filled with a direct-flowing non-biological carrier without requiring an acid generating tank.

In the present invention, the reaction tank in which the above-mentioned fluid non-biological carrier is filled and the water to be treated is circulated may be a full-mixing type reaction tank using a stirrer, an upward flow type reaction tank in a gas-mixing tank by a water flow, or the like.

The processing conditions of the completely mixed type reaction tank and the upward flow type reaction tank are not particularly limited insofar as the processing efficiency can be obtained. For example, the following conditions can be set.

<fully mixed reaction tank>

Carrier filling rate: 10~30%

HRT: 1.0~24hr

Tank load: 4.0~12.0kg-COD _cr /m ³ /day

Sludge load: 0.8~3.0kg-COD _cr /kg-VSS/day

pH: 6.5~7.5

Temperature: 25~38°C

<Upflow reaction tank>

Carrier filling rate: 10~80%

HRT: 1.0~24hr

Rising flow rate (LV): 1.0~20m/hr

Tank load: 4.0~32kg-COD _cr /m ³ /day

Sludge load: 0.8~3.0kg-COD _cr /kg-VSS/day

pH: 6.5~7.5

Temperature: 25~38 °C.

The fluid non-biological carrier used in the anaerobic treatment method of the present invention is preferably a size of 1.0 to 5.0 mm and a sedimentation rate of 100 to 500 m/hr.

When the size of the carrier is too large, the surface area per unit volume of the reaction tank becomes Small, and when it is too small, the sedimentation speed becomes slow and it becomes difficult to separate from the treated water. The size of the carrier used in the present invention is preferably 2.5 to 4.0 mm.

The size of the carrier is usually referred to as the "particle size". For example, the rectangular carrier is the length of its long side, the square carrier is the length of one side, and the cylindrical carrier is the larger of the diameter or the height of the cylinder. . Further, in the case of a carrier having a different shape other than the shape, when the carrier is sandwiched by two parallel plates, the interval between the plates at the portion where the plate is the largest is the interval.

In the present invention, the average size of the carrier is 1.0 to 5.0 mm, preferably 2.5 to 4.0 mm, and the size of all the carriers may not be within the range.

When the precipitation speed of the carrier is too small, it is likely to float due to water flow or gas generation, and it is accumulated in a residue like water surface. In other words, when a method using a non-biological carrier is used, since a biofilm is formed on the surface and a gas generating reaction is performed inside the biofilm, the apparent specific gravity of the carrier does not become small with the formation of the biofilm. When considering the influence of the biofilm, it is necessary to determine the specific gravity of the carrier itself and the precipitation rate. On the other hand, when the precipitation speed of the carrier is too large, the contact efficiency with the water to be treated is deteriorated, and sufficient treatment efficiency cannot be obtained, or the solid matter is accumulated on the deposited layer of the carrier to cause a problem of blockage of the flow path. The preferred precipitation rate of the carrier used in the present invention is from 100 to 500 m/hr.

The sedimentation rate of the carrier is obtained by immersing the carrier in water (clean water such as tap water), taking out the precipitate, and putting it into a measuring cylinder to which water (water such as tap water) is added, and determining the sedimentation distance per unit time. The value of the present invention is determined in the present invention by 10 to 20 vectors, and the average value thereof is used as the precipitation rate.

The carrier used in the present invention is not particularly limited as long as it is a sedimentation rate and a carrier size which satisfy the above-mentioned specified conditions and can retain bacteria. It may be a foam, an unfoamed body or a gel. In particular, those formed by the foams of the following (I) and/or (II) are preferably formed by the resin foam, and it is easy to adjust the specific gravity or the particle diameter.

(I) a foam containing 30 to 95% by weight of a resin component mainly composed of a polyolefin resin and 5 to 70% by weight of a hydrophilizing agent of a cellulose-based powder, and having a foam having a surface in a melt fracture state ( The following is described as "foam (I)")

(II) a foam containing 30 to 95% by weight of a resin component mainly composed of a polyolefin resin, 4 to 69% by weight of a hydrophilizing agent of a cellulose-based powder, and 1 to 30% by weight of an inorganic powder, and having a surface melting A foam in a body fracture state (hereinafter referred to as "foam (II)").

The polyolefin resin may be either a foam or a hydrophilizing agent as long as the precipitation rate or the carrier size satisfies the above specified conditions. The material of the gel is not particularly limited, and examples thereof include polyvinyl alcohol (PVA), polyethylene glycol (PEG), acrylamide, and polyacrylic acid.

Here, the melt fracture refers to a phenomenon in which irregularities are generated on the surface of a molded article (a state having no smooth surface) when it is generally known to form a plastic. For example, when the plastic material is extruded and formed, the internal pressure of the extruder is significantly increased and the extrusion speed is significantly increased, or when the temperature of the plastic material is too low, irregular irregularities are generated on the surface of the molded article, and At the same time, the phenomenon of surface gloss is lost.

The resin components constituting the foams (I) and (II) are polyethylene (hereinafter referred to as It is preferably "PE"), polypropylene (hereinafter abbreviated as "PP"), ethylene-vinyl acetate copolymer (hereinafter abbreviated as "EVA"), and the like. These resins may be used singly or as a mixture of a suitable combination. Further, the resin component constituting the foams (I) and (II) may be added with another thermoplastic resin component to the polyolefin resin. Other thermoplastic resin components, such as polystyrene (hereinafter referred to as "PS"), polyethylene terephthalate, polyvinyl chloride, polyvinyl chloride, polycarbonate, polyurethane, polyfluorene Amine, polyoxymethylene, polylactic acid, polymethyl methacrylate, ABS resin, and the like.

The resin component constituting the foams (I) and (II) is more preferably polyethylene, and may be a mixture of PE and other polyolefin-based resins, for example, a mixture of PE and PP, a mixture of PE and EVA, and PE. And a mixture of PP and EVA, a mixture of PE and PP and PS, a mixture of PE and PP and EVA and PS, or a mixture of these and other thermoplastic resins. Specifically, the composition ratio (weight ratio) of the other thermoplastic resin containing PE, PP, EVA, and PS is 0.1 to 100% of the thermoplastic resin containing PE:PP:EVA:PS when the total amount of the resin is 100: 40~0:20~0:15~0 is better. Further, in order to improve the abrasion resistance of the carrier, it is preferred to contain 10% by weight or more of the EVA in the resin component. Moreover, these resin components may also be recycled resins.

A cellulose-based powder as a hydrophilizing agent, for example, wood powder, cellulose powder, hemp cellulose powder, etc., such as sawdust powder, microcrystalline cellulose (Avicel), powdered cellulose (Arbocel trade name), paper powder, cellulose Beads, microcrystalline cellulose, microfibrillated cellulose, etc., are preferably used with wood flour. These may be used alone or in combination of two or more in any ratio. use.

The shape of the hydrophilizing agent may be spherical, elliptical, wedge-shaped, whisker-like, fibrous, or the like, and may be other shapes. Further, the particle size of the hydrophilizing agent is preferably 200 mesh, preferably 100 mesh, more preferably 40 mesh.

In the present invention, the hydrophilizing agent has a function of imparting a water immersing function to the foam having the closed cells, and therefore the hydrophilizing agent is preferably protruded without being exposed on the surface of the foam. Here, the exposure means that the surface of the partial hydrophilizing agent appears on the surface of the foam, and the protrusion means that the partial affinity agent protrudes from the surface of the foam. In other words, the exposed or protruding means that all or part of the hydrophilizing agent is buried in the foam and the surface of the partially hydrophilizing agent appears on the surface of the foam, or a part of the hydrophilizing agent protrudes from the surface of the foam. The meaning of the state.

The inorganic powder used in the foam (II), for example, barium sulfate, calcium carbonate, zeolite, talc, titanium oxide, potassium titanate, aluminum hydroxide or the like, is preferably a barium sulfate. These inorganic powders may be used singly or in combination of two or more kinds of inorganic powders.

When the specific gravity obtained from the apparent volume is smaller or larger than the above lower limit value, the precipitation speed prescribed by the above-described present invention cannot be satisfied. The specific gravity obtained from the apparent volume of the foam is measured by taking the weight of the foam having an apparent volume of 30 ml in a cylinder of 50 ml, and calculating the weight (unit: g/ml). The proportion. This is because the foams (I) and (II) have a melt fracture state on the surface thereof, and it is extremely difficult to measure the true volume. In the following, the specific gravity obtained from the apparent volume of the foam is simply referred to as "specific gravity".

In the foams (I) and (II), the polyolefin resin, the hydrophilizing agent, and the inorganic powder are melted and kneaded, and the mixture obtained by melt kneading is foamed and cut into a specified size. Made.

The foaming agent is, for example, sodium bicarbonate (sodium hydrogencarbonate), azobiscarbonylguanamine or the like. The foaming agent is not limited to these, such as a chemical foaming agent or a physical foaming agent.

1‧‧‧acid generator tank

2‧‧‧pH adjustment slot

3,3’,3”‧‧‧reaction tank

4‧‧‧Liquid non-biological carriers

[Fig. 1] is a system diagram showing the configuration of an anaerobic treatment apparatus used in the examples and comparative examples.

[Fig. 2] is a system diagram showing the configuration of an anaerobic treatment apparatus used in the embodiment.

[Fig. 3] is a system diagram showing the configuration of the anaerobic treatment device used in the comparative example.

[Fig. 4] is a view showing the results of the examples.

[Fig. 5] is a graph showing the results of a comparative example.

[Fig. 6] is a graph showing the results of the examples.

[Fig. 7] is a graph showing the results of a comparative example.

In the following, the invention will be more specifically described by way of examples and comparative examples.

[Examples] [Examples 1 to 3, Comparative Examples 1 to 4]

According to the anaerobic treatment device shown in Fig. 1, the food system drainage with COD _cr concentration: 5000 mg/L, SS: 1500 mg/L, TN: 250 mg N/L, TP: 30 mg/L, pH: 5.0 was used. Raw water, water test.

The anaerobic treatment device is configured to treat the raw water in the acid generating tank 1 and then feed the pH P ₁ to the pH adjusting tank 2 for pH adjustment, and the pump P ₂ is filled with the fluid non-biocarrier 4 The reaction tank 3 is treated by flowing the pH adjustment water upward. The effluent water from the partial reaction tank 3 is used as circulating water, circulated in the pH adjusting tank 2, and the remaining portion is discharged as treated water to the outside of the system. In the acid generating tank 1 and the pH adjusting tank 2, sodium hydroxide is added as an alkali agent for adjusting the pH. 1A, 2A are pH meters, 1B, 2B are mixers, and 3A is a sieve.

The processing conditions of the acid generating tank 1, the pH adjusting tank 2, and the reaction tank 3 are as follows.

<acid formation tank>

Capacity: 5L

HRT: 4hr

pH: 6.5

Temperature: 35 ° C

<pH adjustment tank 2>

Capacity: 1L

pH: 7.0

<reaction tank>

Capacity: about 7.5L (15cm in diameter and 50cm in height)

HRT: 6hr

Rising flow rate (LV): 3~4m/hr

pH: 7.0

Carrier filling rate: 40%

The method of using the fluid non-biological carrier is as shown in Table 1, and the polyolefin-based resin which is a constituent material of the foam is made of polyethylene, and the hydrophilizing agent is made of wood powder having an elliptical shape and passing through 100 mesh. The inorganic powder is barium sulfate. Moreover, the carriers are all in the shape of a cylinder, and the size of the carrier is the height of the cylinder.

The amount of treated water was about 30 L/Day, and at the beginning of the treatment, the carrier with the microorganisms was filled in the reaction tank 3 at a filling rate of 40%.

The temporal changes of the COD _cr concentration in Example 1 and Comparative Example 4 are shown in Fig. 4 (Example 1) and Fig. 5 (Comparative Example 4).

<observation>

In Examples 1 to 3, the clogging phenomenon was not caused by the floating and solidification of the carrier, and the treatment was carried out in a stable manner. (The COD _cr concentration change is exemplified by the only example shown in Fig. 4 of Example 1. Regarding the examples 2 and 3, it was confirmed that the COD _cr concentration change was approximately the same as in the first embodiment). In Comparative Example 1, the carrier was floated due to SS and could not be processed. In Comparative Example 2, the carrier was solid-melted and blocked by SS, and the treatment could not be performed. In Comparative Example 3, the carrier was floated due to SS and could not be processed. In Comparative Example 4, although the carrier was not blocked by the floating or solid solution, the COD _cr concentration of the treated water shown in Fig. 5 was higher and the irregularity was larger than that of the first example of Example 1, resulting in treatment. Reduced ability.

[Example 4]

As shown in Fig. 2, except that the pH adjusting tank 2 is not provided, and the reaction tank is the following fully mixed type reaction tank 3' (the carrier is preliminarily attached to the microorganisms in the same manner as in the first to third embodiments), In the same manner as in the first embodiment, the above-mentioned food system drainage treatment was carried out. 3C is a pH meter and 3B is a mixer. The change in COD _cr concentration over time is shown in Figure 6.

When the carrier having a small precipitation rate is used in a completely mixed type, the concentration of the treated water is deteriorated under a long period of operation due to the adhesion and floating of the SS, and when the carrier having a large deposition rate is used, in order to uniformly flow the carrier in the reaction tank, The subject of great energy is needed.

<fully mixed reaction tank>

Capacity: about 7.5L

HRT: 6hr

pH: 7.0

Carrier filling rate: 40%

Temperature: 35 ° C

[Comparative Example 5]

As shown in Fig. 3, the above-described food-based drainage treatment was carried out in the same manner as in Example 1 except that the reaction vessel was the small particle reaction vessel 3" described below. 4' indicates small particles, and 3D indicates gas-solid liquid separation device. (GSS). The COD _cr concentration changes with time as shown in Fig. 7. In Comparative Example 5, since small particles rise by SS and flow out to the reaction tank, the sludge in the reaction tank is reduced to reduce the processing capacity, resulting in water quality. deterioration.

<small particle slot>

Capacity: about 7.5L

HRT: 6hr

pH: 7.0

Temperature: 35 ° C

Small particles: small particles of UAS equipment invested in 4L beer factory

The present invention will be described in detail with reference to the specific embodiments thereof, and it is understood that various modifications may be made without departing from the spirit and scope of the invention.

The present invention is based on Japanese Patent Application No. 2013-066782, filed on March 27, 2013, which is incorporated herein by reference.

1‧‧‧acid generator tank

1A, 2A‧‧‧ pH meter

1B, 2B‧‧‧ blender

3A‧‧‧ screen

2‧‧‧pH adjustment slot

3‧‧‧Reaction tank

4‧‧‧Liquid non-biological carriers

Claims (11)

An anaerobic treatment method, which is an anaerobic treatment method for treating organic drainage having a solid concentration of 1000 to 30000 mg/L in an anaerobic reaction tank having a fluid non-biological carrier, which is characterized by the size of the aforementioned carrier It is 1.0 to 5.0 mm, and the precipitation speed of the carrier is 100 to 500 m/hr. The anaerobic treatment method according to claim 1, which is circulated in the reaction tank so that the organic wastewater is not subjected to solid matter removal treatment. The anaerobic treatment method according to claim 1 or 2, wherein the hydrodynamic retention time of the reaction tank is from 1 to 120 hr. The anaerobic treatment method according to any one of claims 1 to 3, wherein the organic wastewater is passed through the acid formation tank and then circulated in the reaction tank. The anaerobic treatment method according to any one of claims 1 to 4, wherein the aforementioned reaction tank is a fully mixed reaction tank. The anaerobic treatment method according to any one of claims 1 to 4, wherein the aforementioned reaction tank is an upward flow type reaction tank. The anaerobic treatment method of claim 1, wherein the organic wastewater has a COD _cr concentration of 1000 to 60,000 mg/L. The anaerobic treatment method according to claim 4, wherein the processing conditions of the acid generating tank are pH values of 5 to 8, temperature of 20 to 40 ° C, and hydrodynamic retention time of 2 to 24 hr. The anaerobic treatment method of claim 5, wherein the processing conditions of the above-mentioned fully mixed reaction tank are as follows, the carrier filling rate: 10 to 30%, the hydrodynamic retention time: 1.0 to 24 hr, the tank load: 4.0 to 12.0 kg. -COD _cr /m ³ /day Sludge load: 0.8~3.0kg-COD _cr /kg-VSS/day pH value: 6.5~7.5 Temperature: 25~38°C. The anaerobic treatment method of claim 6, wherein the processing condition of the upward flow type reaction tank is as follows, the carrier filling rate: 10 to 80%, the hydrodynamic retention time: 1.0 to 24 hr, the rising flow rate (LV): 1.0. ~20m/hr tank load: 4.0~32kg-COD _cr /m ³ /day Sludge load: 0.8~3.0kg-COD _cr /kg-VSS/day pH value: 6.5~7.5 Temperature: 25~38°C. The anaerobic treatment method according to claim 1, wherein the carrier is formed of the following foams of (I) and/or (II), and (I) contains a resin component mainly composed of a polyolefin resin. 95% by weight of a foaming agent of 5 to 70% by weight of a hydrophilizing agent of a cellulose-based powder, having a foam having a melt fracture state on the surface, and (II) containing a polyolefin-based resin as a main component The foam having 30 to 95% by weight of the resin component, 4 to 69% by weight of the hydrophilizing agent of the cellulose-based powder, and 1 to 30% by weight of the inorganic powder has a foam having a surface in a melt fracture state.