WO2014156216A1 - Méthode de traitement anaérobie - Google Patents

Méthode de traitement anaérobie Download PDF

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Publication number
WO2014156216A1
WO2014156216A1 PCT/JP2014/050228 JP2014050228W WO2014156216A1 WO 2014156216 A1 WO2014156216 A1 WO 2014156216A1 JP 2014050228 W JP2014050228 W JP 2014050228W WO 2014156216 A1 WO2014156216 A1 WO 2014156216A1
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WO
WIPO (PCT)
Prior art keywords
carrier
treatment method
anaerobic treatment
water
tank
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Application number
PCT/JP2014/050228
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English (en)
Japanese (ja)
Inventor
孝明 徳富
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栗田工業株式会社
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Filing date
Publication date
Application filed by 栗田工業株式会社 filed Critical 栗田工業株式会社
Priority to JP2015508103A priority Critical patent/JPWO2014156216A1/ja
Priority to KR1020157025604A priority patent/KR20150137061A/ko
Priority to CN201480018707.3A priority patent/CN105102378A/zh
Publication of WO2014156216A1 publication Critical patent/WO2014156216A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/286—Anaerobic digestion processes including two or more steps
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2806—Anaerobic processes using solid supports for microorganisms
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH

Definitions

  • the present invention relates to an anaerobic treatment method in which a non-biological carrier having fluidity is filled in a reaction tank, a biological film is formed on the surface of the non-biological carrier, and the treated water is passed under anaerobic conditions. .
  • a sludge blanket is formed by forming granular sludge with high density and high sedimentation in the reaction tank, and upwardly circulating organic wastewater containing soluble BOD.
  • the UASB (Upflow Anaerobic Sludge Blanket) method is used, which performs high-load and high-speed processing by contacting with a high-pressure anaerobic sludge blanket.
  • solid organic substances with a low digestion rate are separated and treated separately, and only soluble organic substances with a high digestion rate are processed at high speed with high load by anaerobic treatment using granular sludge with high anaerobic microorganism density. It is.
  • EGSB Exanded
  • Granule Sludge Blanket
  • Anaerobic treatment using granular sludge is a method of treating sludge containing anaerobic microorganisms in a granular state and growing it. This method can achieve a high sludge retention concentration compared to the treatment with a fixed bed or fluidized bed that holds sludge on the carrier, so that it can be operated at a high load, and surplus sludge from an already operating treatment system. It is an efficient anaerobic treatment method that can be started up in a short period of time.
  • An anaerobic treatment method using a carrier includes a method using a fixed bed carrier.
  • methane is obtained by using immobilized microorganisms in which anaerobic microorganisms mainly composed of methane bacteria are supported on a carrier made of a synthetic resin material hydrophilically treated with ozone gas.
  • a method for methane fermentation treatment of organic waste for fermentation is described.
  • Patent Document 3 As a fluid non-biological carrier used for such treatment, Patent Document 3 comprises the following foam (I) and / or (II), and the carrier has a size of 1.0 to 5.0 mm. A flowable non-biological carrier is described in which the sedimentation rate of the carrier is 100-500 m / hr.
  • An object of the present invention is to provide an anaerobic treatment method capable of treating organic wastewater with a high solid matter concentration efficiently and at low equipment costs.
  • the anaerobic treatment method of the present invention includes a step of treating an organic wastewater having a solid concentration of 1000 to 30000 mg / L in an anaerobic reaction tank having a fluid non-biological carrier.
  • the size of the carrier is 1.0 to 5.0 mm, and the sedimentation speed of the carrier is 100 to 500 m / hr.
  • the hydraulic retention time (HRT) of the reaction vessel is preferably 1 to 120 hr.
  • the organic wastewater may be passed through the acid generation tank and then into the reaction tank.
  • the reaction vessel is preferably a complete mixing type reaction vessel or an upward flow type reaction vessel.
  • the organic waste water having a high solid concentration is passed through a reaction tank having a non-biological carrier, thereby allowing the non-biological carrier to flow in the anaerobic reaction tank and efficiently performing the anaerobic treatment. .
  • the non-biological carrier used in the present invention has a larger specific gravity and faster settling speed than granules, it can settle even in wastewater containing a high concentration of SS components. Since the generated gas and water flow are appropriately stirred and mixed, when the thickness of the biofilm is increased, the separation occurs naturally, and the floating and blockage of the flow path due to the enlargement of the biofilm can be avoided.
  • the SS component in the organic wastewater may also settle and accumulate inside the reaction tank, but it can be mixed using a fully mixed reaction tank, or in the case of an upward flow reaction tank, the rising flow rate of the liquid can be increased. By increasing the size, the accumulation of SS can be prevented.
  • ⁇ SS components in organic wastewater may also be hydrolyzed by microorganisms and converted to soluble components.
  • the solubilized component is subjected to anaerobic biological treatment in the same manner as the originally included soluble component.
  • a fluid non-biological carrier that satisfies a size of 1 to 5 mm and a sedimentation speed of 100 to 500 m / hr, a sufficient amount of microorganisms are attached to the carrier, and then the carrier floats, flows out, and adheres. It is possible to prevent clogging and form a good fluidized bed, and to perform a stable and efficient anaerobic treatment.
  • organic wastewater having a high solid matter concentration is passed through an anaerobic reaction tank filled with a fluid non-biological carrier, and a biological film is formed on the surface of the non-biological carrier to treat the organic waste water. .
  • the water to be treated in the present invention is a liquid having a high solid matter concentration and containing an organic substance that can be treated by anaerobic treatment by contacting with anaerobic microorganisms.
  • the solid concentration is 1000 mg / L or more, for example, 1000 to 30000 mg / L, particularly 1000 to 5000 mg / L.
  • the COD Cr concentration in the organic waste water is preferably about 1000 to 60000 mg / L, particularly about 3000 to 15000 mg / L.
  • Such wastewater includes, but is not limited to, wastewater from food factories, organic wastewater from chemical factories, semiconductor factory wastewater, and the like.
  • the treatment conditions of the acid generation tank vary depending on conditions such as biodegradability of the water to be treated, but pH 5 to 8, preferably 5.5 to 7.0, temperature 20 to 40 ° C., preferably 25 to A temperature of 35 ° C. and HRT of 2 to 24 hours, preferably 2 to 8 hours is suitable.
  • the treatment in the reaction tank filled with the fluid non-biological carrier in the subsequent stage proceeds well.
  • the reaction tank filled with the above-described fluid non-biological carrier and into which the water to be treated is passed is a fully mixed reaction tank using a stirrer or the like, an upward mixing in the tank with water flow and generated gas.
  • a flow reaction tank or the like can be used.
  • the processing conditions in the complete mixing type reaction tank and the upward flow type reaction tank are not particularly limited as long as desired processing efficiency can be obtained.
  • the following conditions can be set.
  • the fluid abiotic carrier used in the anaerobic treatment method of the present invention preferably has a size of 1.0 to 5.0 mm and a sedimentation speed of 100 to 500 m / hr.
  • the particularly preferred size of the carrier used in the present invention is 2.5 to 4.0 mm.
  • the size of the carrier is usually referred to as “particle size”.
  • particle size For example, in the case of a rectangular parallelepiped carrier, the length of its long side is referred to, and in the case of a cubic carrier, the length of one side thereof is defined. In the case of a cylindrical carrier, the larger one of the diameter and the height of the cylinder is meant. Further, in the case of a carrier having an irregular shape other than these shapes, when the carrier is sandwiched between two parallel plates, the interval between the plates where the interval between the plates becomes the largest is given.
  • the average size of the carrier may be 1.0 to 5.0 mm, preferably 2.5 to 4.0 mm, and all the carrier sizes are not in this range. Also good.
  • the sedimentation speed of the carrier is too small, it will easily float due to water flow and generated gas, and will accumulate in the form of scum near the water surface. That is, in the case of a method using a non-biological carrier, a biofilm is formed on the surface, and a reaction in which gas is generated proceeds inside the biofilm, so that the apparent specific gravity of the carrier decreases with the formation of the biofilm. In consideration of the influence of this biofilm, it is necessary to determine the specific gravity and sedimentation rate of the carrier itself. Conversely, if the sedimentation rate of the carrier is too high, the contact efficiency with the water to be treated will be poor, and sufficient treatment efficiency will not be obtained, or solid matter will accumulate in the deposited layer of the carrier and the channel will be blocked. coming out.
  • the preferred sedimentation rate of the carrier used in the present invention is 100 to 500 m / hr.
  • the sedimentation speed of the carrier is the amount of sedimentation by submerging the carrier in water (fresh water such as tap water), taking it into a graduated cylinder in water (fresh water such as tap water) This is a value obtained by measuring the distance. In the present invention, 10 to 20 carriers were measured, and the average value was taken as the sedimentation velocity.
  • the carrier used in the present invention is not particularly limited as long as the sedimentation rate and the carrier size satisfy the above-mentioned predetermined conditions and can retain bacteria. Foam, unfoamed or gel bodies are also possible. In particular, it is made of a foam of the following (I) and / or (II), and if it is made of such a resin foam, it is preferable in terms of easy adjustment of specific gravity and particle size.
  • 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 for cellulose powder, the surface of which has a melt fracture state ( Hereinafter, it may be referred to as “foam (I)”.
  • a foam comprising 30 to 95% by weight of a resin component mainly composed of a polyolefin resin, 4 to 69% by weight of a hydrophilizing agent for cellulose powder, and 1 to 30% by weight of an inorganic powder, Has a melt fractured state (hereinafter sometimes referred to as “foam (II)”)
  • the polyolefin resin may not be a foam and may not contain a hydrophilizing agent as long as the sedimentation rate and the size of the carrier satisfy the above predetermined conditions.
  • a hydrophilizing agent as long as the sedimentation rate and the size of the carrier satisfy the above predetermined conditions.
  • melt fracture is generally known as a phenomenon in which irregularities are generated on the surface of a molded product during plastic molding (a state having no smooth surface).
  • melt fracture is generally known as a phenomenon in which irregularities are generated on the surface of a molded product during plastic molding (a state having no smooth surface).
  • the extrusion molding of plastic material when the internal pressure of the extruder becomes extremely high, the extrusion speed becomes extremely large, or the temperature of the plastic material becomes too low, irregular irregularities on the surface of the molded product This refers to a phenomenon in which surface gloss or surface gloss is lost.
  • Preferred resin components constituting the foams (I) and (II) are polyethylene (hereinafter sometimes simply abbreviated as “PE”), polypropylene (hereinafter simply abbreviated as “PP”). And ethylene-vinyl acetate copolymer (hereinafter sometimes simply referred to as “EVA”). These resins may be used alone or as a mixture appropriately combined. Further, the resin component constituting the foams (I) and (II) may be one obtained by adding another thermoplastic resin component to a polyolefin resin.
  • PE polyethylene
  • PP polypropylene
  • EVA ethylene-vinyl acetate copolymer
  • thermoplastic resin components polystyrene (hereinafter sometimes abbreviated as “PS”), polyethylene terephthalate, polyvinyl chloride, polyvinylidene chloride, polycarbonate, polyurethane, polyamide, polyacetal, polylactic acid, polymethyl methacrylate , ABS resin and the like.
  • Polyethylene is particularly preferable as the resin component constituting the foams (I) and (II), but a mixture of PE and other polyolefin resins, for example, a mixture of PE and PP, a mixture of PE and EVA, PE and It may be a mixture of PP and EVA, a mixture of PE, PP and PS, a mixture of PE, PP, EVA and PS, or a mixture obtained by further mixing other thermoplastic resins.
  • These resin components may be recycled resins.
  • cellulose-based powder examples include wood powder, cellulose powder, hemp cellulose powder and the like, and sawdust, avicel, arbocel, paper powder, cellulose beads, microcrystalline cellulose, microfibrillated cellulose and the like are exemplified.
  • wood flour any of these may be used alone, or two or more of them may be mixed and used in an arbitrary ratio.
  • the shape of the hydrophilizing agent is spherical, elliptical, wedge-shaped, whisker-shaped, fibrous or the like, but other shapes may be used.
  • the particle size of the hydrophilizing agent is 200 mesh pass product, preferably 100 mesh pass product, more preferably 40 mesh pass product.
  • the hydrophilizing agent has a role of imparting a water permeation function to the foam having closed cells.
  • the hydrophilizing agent is desirably exposed or protruded from the surface of the foam.
  • exposure means that part of the surface of the hydrophilizing agent appears on the foam surface
  • protrusion means that part of the hydrophilizing agent protrudes from the foam surface.
  • being exposed or protruding means that the whole or part of the hydrophilizing agent is buried in the foam and a part of the surface of the hydrophilizing agent appears on the foam surface, or It means a state in which a part of the hydrophilizing agent protrudes from the foam surface.
  • Examples of the inorganic powder used for the foam (II) include barium sulfate, calcium carbonate, zeolite, talc, titanium oxide, potassium titanate, and aluminum hydroxide, and barium sulfate is particularly preferable. Any of these inorganic powders may be used alone, or two or more kinds of inorganic powders may be used.
  • the specific gravity obtained from the apparent volume of the foam is a value (unit: g / ml) obtained by measuring 30 ml of the foam in an apparent volume in a 50 ml graduated cylinder and calculating the weight. It shall be shown. This is because the foams (I) and (II) have a melt-lacquered state on the surface, and it is very difficult to measure the true volume.
  • specific gravity obtained from the apparent volume of the foam is simply referred to as “specific gravity”.
  • Foams (I) and (II) are prepared by melting and kneading the above-mentioned polyolefin resin, hydrophilizing agent, and further inorganic powder, and further foaming a mixture obtained by melting and kneading the foaming agent. It can be manufactured by cutting into a size.
  • foaming agents examples include sodium bicarbonate (sodium bicarbonate) and azodicarbonamide.
  • a foaming agent is not restricted to these, A chemical foaming agent, a physical foaming agent, etc. are mentioned.
  • Examples 1 to 3 Comparative Examples 1 to 4
  • food wastewater having a COD Cr concentration of 5000 mg / L, SS: 1500 mg / L, TN: 250 mg N / L, TP: 30 mg / L, pH: 5.0 is discharged.
  • a water flow test was conducted as raw water.
  • the treatment conditions of the acid generation tank 1, the pH adjustment tank 2, and the reaction tank 3 were as follows. ⁇ Acid production tank> Capacity: 5L HRT: 4 hours pH: 6.5 Temperature: 35 ° C
  • the specifications of the flowable non-biological carrier used are as shown in Table 1.
  • Polyolefin resin is used as the constituent material of the foam and polyethylene is used as the hydrophilizing agent.
  • Wood powder was used, and barium sulfate was used as the inorganic powder.
  • Each carrier has a cylindrical shape, and the size of the carrier is the height of the column.
  • the amount of treated water was about 30 L / day, and at the start of the treatment, the reaction tank 3 was filled with a carrier with microorganisms attached at a filling rate of 40%.
  • FIG. 4 (Example 1) and FIG. 5 (Comparative Example 4) show the changes over time in the COD Cr concentration of Example 1 and Comparative Example 4.
  • Example 1 the carrier can be stably processed without causing a blocking phenomenon due to the floating and fixing of the carrier.
  • the COD Cr concentration change is representatively shown in FIG. 4 only for Example 1. As for Examples 2 and 3, it was recognized that the COD Cr concentration change was almost the same as Example 1.
  • Comparative Example 2 the carrier floated due to SS and became unprocessable.
  • Comparative Example 2 the carrier was fixed and blocked by SS, making it impossible to process.
  • Comparative Example 3 the carrier floated due to SS and became unprocessable.
  • Comparative Example 4 no clogging due to floating and sticking of the carrier was observed, but as shown in FIG. 5, the COD Cr concentration of the treated water was higher than that of FIG. Has fallen.
  • Example 4 As shown in FIG. 2, the pH adjustment tank 2 was not installed, and the reaction tank was the following fully mixed reaction tank 3 ′ (microorganisms were previously attached to the carrier as in Examples 1 to 3).
  • the food wastewater was treated in the same manner as in Example 1 except that. 3C is a pH meter, and 3B is a stirrer.
  • FIG. 6 shows the change over time in the COD Cr concentration.
  • a carrier with a low sedimentation rate SS adheres and floats, so the concentration of treated water deteriorates during long-term operation. If a carrier with a high sedimentation rate is used, the carrier flows uniformly in the reaction vessel. Therefore, it is a problem that much energy is required for stirring.
  • ⁇ Completely mixed reaction tank> Capacity: Approximately 7.5L HRT: 6 hr pH: 7.0
  • Carrier filling rate 40% Temperature: 35 ° C
  • FIG. 3 shows the food wastewater was treated in the same manner as in Example 1 except that the reaction vessel was the following granule reaction vessel 3 ′′. 4 'is a granule, and 3D is a gas-solid-liquid separator (GSS).
  • FIG. 7 shows the change over time in the COD Cr concentration.
  • the granule was raised by SS and flowed out of the reaction tank, the sludge in the reaction tank was reduced and the treatment capacity was lowered, so the water quality deteriorated.

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  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biological Treatment Of Waste Water (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

L'invention concerne une méthode de traitement anaérobie qui permet le traitement d'eau refoulée avec de la matière organique ayant une concentration en solides élevée avec un rendement élevé et un faible coût des installations. De l'eau brute ayant une concentration en solides supérieure ou égale à 1000 mg/L est traitée dans une cuve à production d'acide (1), puis l'eau traitée est fournie à une cuve d'ajustement de pH (2) grâce à une pompe (P1) afin d'ajuster la valeur du pH de l'eau, puis l'eau à pH ajusté peut traverser une cuve de réaction (3), qui est remplie d'un vecteur non biologique fluide (4), dans une direction d'écoulement vers le haut grâce à une pompe (P 2). Une partie de l'eau sortant de la cuve de réaction (3) est mise en circulation dans la cuve d'ajustement de pH (2) comme eau de circulation, et le reste de l'eau sortant est refoulée vers l'extérieur du système comme eau traitée.
PCT/JP2014/050228 2013-03-27 2014-01-09 Méthode de traitement anaérobie WO2014156216A1 (fr)

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JP2015508103A JPWO2014156216A1 (ja) 2013-03-27 2014-01-09 嫌気性処理方法
KR1020157025604A KR20150137061A (ko) 2013-03-27 2014-01-09 혐기성 처리 방법
CN201480018707.3A CN105102378A (zh) 2013-03-27 2014-01-09 厌氧性处理方法

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JP2013-066782 2013-03-27
JP2013066782 2013-03-27

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2016007574A (ja) * 2014-06-24 2016-01-18 オルガノ株式会社 嫌気性生物処理装置および嫌気性生物処理方法
JP2017176958A (ja) * 2016-03-29 2017-10-05 株式会社クラレ 担体を利用した排水処理方法
JP2018015692A (ja) * 2016-07-26 2018-02-01 水ｉｎｇ株式会社 有機性廃水の嫌気性処理方法
JP2020157278A (ja) * 2019-03-28 2020-10-01 住友重機械エンバイロメント株式会社 嫌気処理装置及び嫌気処理方法

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CN110776694A (zh) * 2019-11-30 2020-02-11 苏州和塑美科技有限公司 一种环境友好型水净化功能母粒及其制备方法

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JPS61171600A (ja) * 1985-01-25 1986-08-02 Kurita Water Ind Ltd 汚泥など高濃度有機性廃液の処理方法
JPS61242696A (ja) * 1985-04-19 1986-10-28 Kubota Ltd メタン発酵方法
JPH02207899A (ja) * 1989-02-07 1990-08-17 Akua Runesansu Gijutsu Kenkyu Kumiai 分離装置を組み込んだ嫌気性二相式廃水処理システム
JPH0490897A (ja) * 1990-08-03 1992-03-24 Snow Brand Milk Prod Co Ltd 高濃度有機性排水の嫌気性処理方法
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JPH05138192A (ja) * 1991-11-21 1993-06-01 Sanki Eng Co Ltd 有機性の懸濁物質を含む高濃度有機性廃水の嫌気性処理方法およびその装置
JPH0975982A (ja) * 1995-09-07 1997-03-25 Nisshin Seito Kk 有機性廃水のミックスベッド式嫌気性処理装置
JP2004358391A (ja) * 2003-06-05 2004-12-24 Kurita Water Ind Ltd 有機性廃棄物の処理方法及び処理装置
JP2009066592A (ja) * 2007-08-23 2009-04-02 Nisshinbo Ind Inc 流体処理用担体及びその製造方法
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WO2012070493A1 (fr) * 2010-11-26 2012-05-31 栗田工業株式会社 Procédé de traitement anaérobie
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2016007574A (ja) * 2014-06-24 2016-01-18 オルガノ株式会社 嫌気性生物処理装置および嫌気性生物処理方法
JP2017176958A (ja) * 2016-03-29 2017-10-05 株式会社クラレ 担体を利用した排水処理方法
JP2018015692A (ja) * 2016-07-26 2018-02-01 水ｉｎｇ株式会社 有機性廃水の嫌気性処理方法
JP2020157278A (ja) * 2019-03-28 2020-10-01 住友重機械エンバイロメント株式会社 嫌気処理装置及び嫌気処理方法
JP7266440B2 (ja) 2019-03-28 2023-04-28 住友重機械エンバイロメント株式会社 嫌気処理装置及び嫌気処理方法

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CN105102378A (zh) 2015-11-25
TW201446660A (zh) 2014-12-16
JPWO2014156216A1 (ja) 2017-02-16

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