JPH09122683A - Method for anaerobic treatment - Google Patents
Method for anaerobic treatmentInfo
- Publication number
- JPH09122683A JPH09122683A JP28324195A JP28324195A JPH09122683A JP H09122683 A JPH09122683 A JP H09122683A JP 28324195 A JP28324195 A JP 28324195A JP 28324195 A JP28324195 A JP 28324195A JP H09122683 A JPH09122683 A JP H09122683A
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- sludge
- water
- pipeline
- granule sludge
- content
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- Y02W10/12—
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は嫌気性処理法に係
り、特にＵＡＳＢ( Upflow Anaerobic Sludge Blanket
：上向流式嫌気性汚泥床）型嫌気性処理装置における
処理において、グラニュール汚泥を浮上流出させずに、
反応槽内に安定に保持することにより、処理の安定化、
効率化を図る方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an anaerobic treatment method, and more particularly to UASB (Upflow Anaerobic Sludge Blanket).
: Upflow-type anaerobic sludge bed) type anaerobic treatment device
Stabilizing the process by keeping it stable in the reaction tank,
Regarding the method of improving efficiency.
【０００２】[0002]
【従来の技術及び先行技術】ＵＡＳＢ法は、菌の付着担
体を用いることなく、嫌気性微生物をグラニュールと呼
ばれる粒状の汚泥として反応槽内に汚泥床（スラッジブ
ランケット）を形成し、原水を反応槽下部より上向流で
通水して処理する方法であり、従来、主にビール、製糖
等の食品産業排水の処理法として利用されている。ＵＡ
ＳＢ法は、他の嫌気性処理法、即ち、固定床又は流動床
式嫌気性処理法等と比較して、反応槽内の汚泥保持濃度
が高く、しかも閉塞のおそれのない方法であり、既に数
多くの実績を挙げている。2. Description of the Related Art The UASB method forms a sludge bed (sludge blanket) in a reaction tank by converting anaerobic microorganisms into granular sludge called granules without using an adherent carrier of bacteria to react raw water. This is a method of treating water by flowing upward from the bottom of the tank, and has been conventionally used mainly as a method of treating wastewater from the food industry such as beer and sugar production. UA
The SB method has a higher sludge retention concentration in the reaction tank and is free from clogging compared with other anaerobic treatment methods, that is, a fixed bed or fluidized bed type anaerobic treatment method. Has many achievements.
【０００３】しかし、ＵＡＳＢ法では、グラニュール汚
泥の密度が水よりも小さい状態になってグラニュール汚
泥が浮上し、反応槽上部にスカムとなって堆積したり、
処理水と共に反応槽から流出したりすることにより、処
理に必要な汚泥量が確保できなくなるという問題が生じ
ている。特に、粒径が２ｍｍ以上の大きなグラニュール
汚泥では、内部から発生するガスが外部に放出されずに
グラニュール汚泥内部に溜り、上記のような浮上現象が
起き易く、このため、運転開始後数年経過して、グラニ
ュール汚泥が大粒子に成長した装置ではこのような問題
が起こり易い。However, in the UASB method, the density of the granule sludge becomes smaller than that of water, and the granule sludge floats up and accumulates as scum on the upper part of the reaction tank.
There is a problem that the amount of sludge necessary for the treatment cannot be secured because it flows out from the reaction tank together with the treated water. In particular, in the case of large granule sludge having a particle size of 2 mm or more, the gas generated from the inside accumulates inside the granule sludge without being released to the outside, and the above-mentioned floating phenomenon easily occurs. Such a problem is likely to occur in a device in which granule sludge has grown into large particles over the years.
【０００４】グラニュール汚泥内部にガスが溜る直接の
原因は、グラニュール汚泥内部に空洞が生じることにあ
る。この空洞が生じる原因は、グラニュール汚泥内部の
菌体が基質不足により自己分解するため、及び、グラニ
ュール汚泥内部に捕捉された有機性ＳＳが徐々に分解す
るため、とされている。The direct cause of the accumulation of gas inside the granulated sludge is the formation of cavities inside the granulated sludge. It is said that the cause of this cavity is that the bacterial cells inside the granulated sludge self-decompose due to lack of substrate, and that the organic SS trapped inside the granular sludge gradually decomposes.
【０００５】こうした空洞に起因するグラニュール汚泥
の浮上防止策として、本出願人は先に、ＵＡＳＢ反応槽
内に鉄塩又はカルシウム化合物を添加し、グラニュール
汚泥の空洞をこれらの金属の析出物により充填して気泡
が溜らないようにする方法を提案した（特願平６−２８
７９０７号。以下「先願」という。）。As a measure for preventing the floating of granule sludge due to such cavities, the present applicant first added an iron salt or a calcium compound in the UASB reaction tank, and made the cavities of the granule sludge into precipitates of these metals. We have proposed a method to prevent air bubbles from accumulating by applying (Japanese Patent Application No. 6-28).
No. 7907. Hereinafter, it is referred to as “first application”. ).
【０００６】上記先願の方法においては、特に鉄塩の添
加が有効であり、原水有機物濃度に比例したある濃度範
囲で鉄塩及び必要に応じて硫酸塩を添加することによ
り、グラニュール汚泥の空洞を硫化鉄（ＦｅＳ）によっ
て充填し、浮上を効果的に防止することができる。In the method of the above-mentioned prior application, it is particularly effective to add an iron salt, and by adding an iron salt and, if necessary, a sulfate in a certain concentration range proportional to the concentration of raw water organic matter, The cavity can be filled with iron sulfide (FeS) to effectively prevent levitation.
【０００７】[0007]
【発明が解決しようとする課題】しかしながら、上記先
願の方法では、鉄塩の添加量が最適化されておらず、鉄
塩の過剰添加による問題が生じていた。即ち、過剰量の
鉄塩を添加することにより、汚泥中に占める菌体の割合
が低下して、全汚泥当りの活性が低下するという問題が
生じる。このように鉄塩の過剰添加は、装置の処理効率
を低下させる可能性がある。However, in the method of the above-mentioned prior application, the addition amount of the iron salt was not optimized, and there was a problem due to the excessive addition of the iron salt. That is, the addition of an excessive amount of iron salt causes a problem that the proportion of bacterial cells in the sludge is reduced and the activity per total sludge is reduced. Thus, the excessive addition of iron salt may reduce the treatment efficiency of the device.
【０００８】本発明は、上記先願の方法における問題点
を解決し、より信頼性の高いグラニュール汚泥の浮上防
止対策をとることができる嫌気性処理法を提供すること
を目的とする。It is an object of the present invention to solve the problems in the method of the above-mentioned prior application and to provide an anaerobic treatment method capable of taking a more reliable measure for preventing floating of granule sludge.
【０００９】[0009]
【課題を解決するための手段】本発明の嫌気性処理法
は、グラニュール汚泥で形成されたスラッジブランケッ
トに有機性排水を上向流通水して嫌気性処理する方法に
おいて、グラニュール汚泥の全固形物質に対する鉄の含
有率が３重量％以上となるように、該有機性排水に鉄塩
及び／又は硫酸イオン源を添加することを特徴とするも
のである。The anaerobic treatment method of the present invention is a method for anaerobic treatment by upwardly circulating organic waste water to a sludge blanket formed of granule sludge. It is characterized in that an iron salt and / or a sulfate ion source is added to the organic wastewater so that the iron content with respect to the solid substance is 3% by weight or more.
【００１０】本発明者らは、種々のＵＡＳＢ実装置内の
グラニュール汚泥の性状を様々な角度から調査、分析し
た結果、図２に示す如く、汚泥の浮上性は汚泥のＴＳ
（全固形物質）中のＦｅ含有割合が３重量％未満の場合
に高く、５重量％以上であれば殆ど浮上しないことを見
出した。なお、図２及び後掲の図４に示す浮上ポテンシ
ャルとは、汚泥の浮上傾向を数値化したもので、酢酸基
質１，０００ｍｇ／Ｌ入りフラスコにグラニュール汚泥
を約２０ｍＬ入れ、３５℃で２４時間嫌気的に静置培養
した後、浮上汚泥と沈澱汚泥のＶＳＳ重量を測定し、浮
上汚泥の全体に占める割合を重量％で表示したものであ
る。The present inventors have investigated and analyzed the properties of granule sludge in various UASB actual equipment from various angles, and as a result, as shown in FIG.
It has been found that the Fe content in (total solid matter) is high when the content is less than 3% by weight, and that when the content is 5% by weight or more, it hardly floats. Note that the flotation potential shown in FIG. 2 and FIG. 4 below is a numerical representation of the flotation tendency of sludge. After statically culturing anaerobically for a period of time, the VSS weights of the flotation sludge and the settled sludge were measured, and the ratio of the flotation sludge to the whole was expressed in% by weight.
【００１１】Ｆｅ塩を添加していてもＳＯ4 2- 不足等に
よりＴＳ中のＦｅ含有率が３重量％未満に維持されてい
る限りはグラニュール汚泥は浮上傾向となり、Ｆｅ添加
のみでは浮上防止効果は得られない。従って、この場合
には、Ｆｅ塩と共にＳＯ4 2-の添加が必要である。Even if the Fe salt is added, as long as the Fe content in TS is kept below 3% by weight due to lack of SO 4 2-, the granulated sludge tends to float, and only the addition of Fe prevents floating. No effect. Therefore, in this case, it is necessary to add SO 4 2− together with the Fe salt.
【００１２】調査した汚泥には、連続的にＦｅ塩及びＳ
Ｏ4 2- を添加することにより、ＴＳ中に１０重量％以上
のＦｅ含有率に達したものもあったが、汚泥の浮上防止
の観点からは、Ｆｅ含有率は１０重量％以上でなくとも
十分効果が得られる。Ｆｅ塩及びＳＯ4 2- を過剰に添加
すると、ＴＳ中のＦｅ含有率はそれに比例して大きくな
るが、反面、菌体含有率（ＴＳに占めるＶＳＳの割合）
が低下し、結果として反応槽中の保持菌体量が低下す
る。従って、浮上防止効果と反応槽中の保持菌体量の維
持の面から、特に汚泥中のＦｅ含有率は５〜１０重量％
であることが好ましい。The sludge investigated contained Fe salt and S continuously.
By adding O 4 2- , some Fe content ratio in TS reached 10% by weight or more, but from the viewpoint of preventing the sludge from floating, the Fe content may be 10% by weight or more. The effect is fully obtained. When Fe salt and SO 4 2− are added excessively, the Fe content in TS increases in proportion to it, but on the other hand, the cell content (VSS ratio in TS)
Is decreased, and as a result, the amount of retained bacterial cells in the reaction tank is decreased. Therefore, the Fe content in the sludge is particularly 5 to 10% by weight from the viewpoint of the effect of preventing floating and the maintenance of the amount of the retained cells in the reaction tank.
It is preferred that
【００１３】グラニュール汚泥内のＦｅ含有率を上記範
囲に維持することにより、グラニュール汚泥の沈降性が
著しく向上し、反応槽内の汚泥濃度を例えばＶＳＳとし
て７〜１０万ｍｇ／Ｌ程度に、飛躍的に増加させること
ができる。また、ガスを内包することによる汚泥の浮上
を防ぐことができるため、１５〜２０ｋｇ−ＣＯＤCr／
ｍ3 ／日以上での高負荷処理が可能となる。同時に、低
濃度排水に対しては、排水の滞留時間を低下させること
が可能となる。By maintaining the Fe content in the granule sludge within the above range, the sedimentation property of the granule sludge is remarkably improved, and the sludge concentration in the reaction tank is, for example, VSS of about 70 to 100,000 mg / L. , Can be increased dramatically. Moreover, since it is possible to prevent the sludge from floating due to the inclusion of gas, it is possible to obtain 15 to 20 kg-COD Cr /
High load processing is possible at m 3 / day or more. At the same time, it is possible to reduce the retention time of the wastewater for low-concentration wastewater.
【００１４】本発明においては、グラニュール汚泥中の
Ｆｅ含有率を上記範囲として、反応槽（水槽の水容量）
のＣＯＤCr容量負荷を１０ｋｇ／ｍ3 ／日以上、特に１
５ｋｇ／ｍ3 ／日以上、とりわけ２０ｋｇ／ｍ3 ／日以
上とし、反応槽（水槽の水容量）における被処理排水の
滞留時間が４時間以内、特に３時間以内、とりわけ２時
間以内となるように運転を行うのが好ましい。In the present invention, the Fe content in the granulated sludge is set within the above range, and the reaction tank (water capacity of the water tank) is set.
COD Cr capacity load of 10 kg / m 3 / day or more, especially 1
5 kg / m 3 / day or more, especially 20 kg / m 3 / day or more, so that the residence time of the treated wastewater in the reaction tank (water capacity of the water tank) is 4 hours or less, particularly 3 hours or less, particularly 2 hours or less. It is preferable to carry out the operation.
【００１５】[0015]
【発明の実施の形態】以下に本発明を詳細に説明する。DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below in detail.
【００１６】本発明の方法においては、グラニュール汚
泥のスラッジブランケットに上向流通水して嫌気性処理
する有機性排水に、グラニュール汚泥中のＴＳに対する
Ｆｅ含有率が３重量％以上、好ましくは５〜１０重量％
以上となるように、Ｆｅ塩及び／又はＳＯ4 2- 源を添加
する。In the method of the present invention, the organic wastewater for anaerobic treatment by upwardly flowing water to the sludge blanket of the granulated sludge has an Fe content of 3% by weight or more with respect to TS in the granulated sludge, preferably 5-10% by weight
As mentioned above, the Fe salt and / or the SO 4 2− source is added.
【００１７】本発明においてＦｅ塩としては、ＦｅＣｌ
3 ，ＦｅＳＯ4 ，Ｆｅ2 （ＳＯ4 ）3 等が好適に用いら
れ、また、ＳＯ4 2- 源としては、Ｎａ2 ＳＯ4 等の硫酸
塩やＨ2 ＳＯ4 を用いることができる。In the present invention, the Fe salt is FeCl.
3 , FeSO 4 , Fe 2 (SO 4 ) 3 and the like are preferably used, and as the SO 4 2− source, sulfates such as Na 2 SO 4 and H 2 SO 4 can be used.
【００１８】本発明においては、Ｆｅ塩及び／又はＳＯ
4 2- 源の添加により、グラニュール汚泥内にＦｅＳの結
晶をＦｅ含有率が３重量％以上、好ましくは５〜１０重
量％となるように、成長させて、汚泥の比重を高め、そ
の沈降性を改善することができる。In the present invention, Fe salt and / or SO
4 By adding a 2- source, FeS crystals are grown in the granulated sludge so that the Fe content is 3% by weight or more, preferably 5 to 10% by weight, the specific gravity of the sludge is increased, and the sedimentation thereof is performed. The sex can be improved.
【００１９】グラニュール汚泥中のＦｅ含有率が３重量
％以上、好ましくは５〜１０重量％となるようにＦｅ塩
及び／又はＳＯ4 2- 源の添加量を調整するためには、反
応槽内のグラニュール汚泥を定期的にサンプリングして
Ｆｅ含有率を測定し、この測定値に基いて、Ｆｅ塩及び
／又はＳＯ4 2- 源の添加量を制御するのが好ましい。こ
の場合、グラニュール汚泥のＦｅ含有率の測定法として
は、グラニュール汚泥を硫酸及び硝酸の混合液に加熱溶
解させて、原子吸光法などで分析する方法が最も一般的
である。In order to adjust the addition amount of the Fe salt and / or SO 4 2- source so that the Fe content in the granulated sludge is 3% by weight or more, preferably 5 to 10% by weight, the reaction tank is used. It is preferable to periodically sample the granulated sludge in the inside to measure the Fe content and to control the added amount of the Fe salt and / or the SO 4 2− source based on the measured value. In this case, the most general method for measuring the Fe content of the granulated sludge is to heat and dissolve the granulated sludge in a mixed solution of sulfuric acid and nitric acid, and then analyze by atomic absorption method or the like.
【００２０】本発明において、被処理水へのＦｅ塩及び
／又はＳＯ4 2- 源の添加位置は、酸生成槽流出水のＵＡ
ＳＢ反応槽流入直前の部分が最も好適である。In the present invention, the position of addition of the Fe salt and / or SO 4 2− source to the water to be treated is determined by the UA of the acid generation tank outflow water.
The most suitable part is just before the SB reaction tank.
【００２１】なお、Ｆｅ塩及び／又はＳＯ4 2- 源は、必
ずしも試薬として添加する必要はなく、これらを含む他
系統の排水を被処理水に混入させることにより、Ｆｅ塩
及び／又はＳＯ4 2- 源を添加するようにすることもでき
る。[0021] Incidentally, the Fe salts and / or SO 4 2-sources need not necessarily be added as a reagent, by mixing the waste water other strains containing these to the water to be treated, Fe salts and / or SO 4 It is also possible to add a 2- source.
【００２２】本発明においては、Ｆｅ塩及び／又はＳＯ
4 2- 源の添加によりグラニュール汚泥中のＴＳに対する
Ｆｅ含有率を３重量％以上、好ましくは５〜１０重量％
とすることによる高負荷処理化で、反応槽（水槽の水容
量）のＣＯＤCr容量負荷を１０ｋｇ／ｍ3 ／日以上、特
に１５ｋｇ／ｍ3 ／日以上、とりわけ２０ｋｇ／ｍ3／
日以上とし、反応槽（水槽の水容量）における被処理排
水の滞留時間が４時間以内、特に３時間以内、とりわけ
２時間以内となるように運転を行うのが好ましい。In the present invention, Fe salt and / or SO
4 Fe source content of TS in granulated sludge is 3% by weight or more, preferably 5 to 10% by addition of 2- source
The COD Cr capacity load of the reaction tank (water capacity of the water tank) is 10 kg / m 3 / day or more, particularly 15 kg / m 3 / day or more, especially 20 kg / m 3 /
It is preferable to carry out the operation so that the retention time of the waste water to be treated in the reaction tank (water capacity of the water tank) is 4 hours or less, particularly 3 hours or less, and particularly 2 hours or less.
【００２３】[0023]
【実施例】以下に実施例及び比較例を挙げて、本発明を
より具体的に説明する。The present invention will be described more specifically with reference to the following examples and comparative examples.
【００２４】実施例１ ビール工場のＵＡＳＢ反応槽から採取したグラニュール
汚泥（平均粒径：約１．５ｍｍ）を用いて、図１に示す
装置により、鉄塩の添加効果を調べた。Example 1 Using granule sludge (average particle size: about 1.5 mm) collected from a UASB reaction tank of a beer factory, the effect of adding an iron salt was examined by the apparatus shown in FIG.
【００２５】まず、内径１０ｃｍ、高さ１００ｃｍの実
験用ＵＡＳＢ反応槽（容量：９Ｌ）１を準備し、これら
に上記の汚泥を静止容量として３Ｌ充填した。原水とし
ては、ビール工場の仕込系排水（ＣＯＤCr：１８，００
０ｍｇ／Ｌ）をＣＯＤCr濃度が１，５００ｍｇ／Ｌにな
るように水道水で希釈したものを用い、この原水を配管
１１より酸生成槽（容量：２．５Ｌ）２にて処理した
後、配管１２よりＵＡＳＢ反応槽１に導入し、配管１３
より処理水を系外に取り出すと共に、処理水の一部を配
管１４より酸生成槽２に循環した。循環比は、酸生成槽
流入水量１Ｑに対し、ＵＡＳＢ反応槽流入水量２Ｑ、循
環水量１Ｑとなるようにした。なお、酸生成槽２では、
ｐＨが６．５となるようにＮａＯＨを添加した。First, an experimental UASB reaction tank (capacity: 9 L) 1 having an inner diameter of 10 cm and a height of 100 cm was prepared, and 3 L of the above sludge was filled therein as a static capacity. As raw water, brewery system wastewater (COD Cr : 18,000)
0 mg / L) was diluted with tap water so that the COD Cr concentration became 1,500 mg / L, and this raw water was treated through a pipe 11 in an acid generation tank (capacity: 2.5 L) 2. It is introduced into the UASB reaction tank 1 from the pipe 12, and the pipe 13
Further, the treated water was taken out of the system, and a part of the treated water was circulated to the acid generation tank 2 through the pipe 14. The circulation ratio was such that the amount of inflow water of the acid production tank was 1Q, and the amount of inflow water of the UASB reaction tank was 2Q and the amount of circulation water was 1Q. In the acid production tank 2,
NaOH was added to bring the pH to 6.5.
【００２６】また、ＵＡＳＢ反応槽１の流入直前の配管
１２の酸生成槽流出水に、配管１５よりＦｅ塩としてＦ
ｅＣｌ3 ・６Ｈ2 ＯをＦｅ3+換算で約５ｍｇ／Ｌ添加し
た。水道水中にはＳＯ4 2- イオンが８〜１０ｍｇ／Ｌ含
まれていたため、ＳＯ4 2- 源の添加は行わなかった。Further, in the acid generation tank outflow water of the pipe 12 immediately before the inflow of the UASB reaction tank 1, the Fe salt as F salt is supplied from the pipe 15.
About 5 mg / L of eCl 3 .6H 2 O in terms of Fe 3+ was added. Since SO 4 2− ion was contained in the tap water at 8 to 10 mg / L, the SO 4 2− source was not added.
【００２７】通水量を段階的に増加させて滞留時間を４
時間から１．５時間まで短縮させることにより、図３の
如く、容積負荷を９ｋｇ−ＣＯＤCr／ｍ3 ／日から２４
ｋｇ−ＣＯＤCr／ｍ3 ／日まで増加させ、ＵＡＳＢ反応
槽内の汚泥のＦｅ含有率（図４）、浮上ポテンシャル
（図５）及び保持汚泥量（図６）の変化、Ｆｅ含有率と
処理性能（図７）の関係を調べた。なお、実験温度は３
５℃とした。The residence time is increased to 4 by gradually increasing the water flow rate.
By reducing the time from 1.5 hours to 1.5 hours, the volume load is changed from 9 kg-COD Cr / m 3 / day to 24 as shown in FIG.
kg-COD Cr / m 3 / day, changes in Fe content (Fig. 4), flotation potential (Fig. 5) and retained sludge amount (Fig. 6) in sludge in the UASB reactor, Fe content and treatment The relationship of performance (Fig. 7) was investigated. The experimental temperature is 3
5 ° C.
【００２８】実施例２ Ｆｅの過剰添加の例として、ＦｅＣｌ3 ・６Ｈ2 Ｏの代
りに、ＦｅＳＯ4 をＦｅ2+換算で５０ｍｇ／Ｌ添加した
こと以外は、実施例１と同様に実験を行った。Example 2 As an example of excessive addition of Fe, an experiment was conducted in the same manner as in Example 1 except that FeSO 4 was added in an amount of 50 mg / L in terms of Fe 2+ instead of FeCl 3 .6H 2 O. It was
【００２９】比較例１ Ｆｅ無添加の例として、ＦｅＣｌ3 ・６Ｈ2 Ｏを添加し
なかったこと以外は実施例１と同様に実験を行った。Comparative Example 1 An experiment was conducted in the same manner as in Example 1 except that FeCl 3 .6H 2 O was not added as an example in which Fe was not added.
【００３０】図３〜７の結果より次のことが明らかであ
る。From the results of FIGS. 3 to 7, the following is clear.
【００３１】即ち、図４，５に示すように、Ｆｅを添加
した実施例１，２では、Ｆｅ含有率が３．５重量％を超
えた４３日目以降から汚泥の浮上ポテンシャルが低下
し、実験を終了した９０日目ではほぼゼロになった。実
施例１において、実験終了時のグラニュール汚泥中のＦ
ｅ含有率は約８重量％であった。これに対し、Ｆｅ無添
加の比較例１では浮上ポテンシャルが殆ど低下せずに、
終了時にも約２６％あった。なお、Ｆｅ含有率は１重量
％以下であった。That is, as shown in FIGS. 4 and 5, in Examples 1 and 2 in which Fe was added, the floating potential of sludge decreased from the 43rd day after the Fe content exceeded 3.5% by weight, It was almost zero on the 90th day when the experiment was completed. In Example 1, F in the granule sludge at the end of the experiment
The e content was about 8% by weight. On the other hand, in Comparative Example 1 in which Fe is not added, the floating potential is hardly decreased,
It was about 26% at the end. The Fe content was 1% by weight or less.
【００３２】また、負荷量は、図３に示す如く、９，１
８，２４ｋｇ−ＣＯＤCr／ｍ3 ／日と１ヵ月間隔で３段
階に上昇させたが、図７に示す如く、実施例１ではいず
れの条件においても８０％以上の溶解性ＣＯＤCr除去率
を維持した。実施例２では、汚泥の沈降性は向上した
が、汚泥中のＶＳＳ含有率が低下して菌体保持量が低下
した結果、２４ｋｇ−ＣＯＤCr／ｍ3 ／日の条件では除
去率は７０％以下に低下した。これに対し、比較例１で
は汚泥の浮上流出が継続したため、図６に示す如く、反
応槽内の汚泥保持量が徐々に減少し、２４ｋｇ−ＣＯＤ
Cr／ｍ3 ／日の負荷条件では除去率が５０％以下に悪化
した。The load amount is 9, 1 as shown in FIG.
Although it was increased in 3 steps at a monthly interval of 8,24 kg-COD Cr / m 3 / day, as shown in FIG. 7, in Example 1, a soluble COD Cr removal rate of 80% or more was obtained under all conditions. Maintained. In Example 2, the sludge settling property was improved, but the VSS content rate in the sludge was decreased and the cell retention amount was decreased. As a result, the removal rate was 70% under the conditions of 24 kg-COD Cr / m 3 / day. Fell below. On the other hand, in Comparative Example 1, since the sludge floated and flowed out continuously, as shown in FIG. 6, the sludge holding amount in the reaction tank gradually decreased to 24 kg-COD.
Under Cr / m 3 / day load condition, the removal rate deteriorated to 50% or less.
【００３３】実施例２及び比較例１の除去率が実施例１
と比較して悪かったのは、反応槽内の菌体保持量が少な
かったためであることが、図６から明らかである。The removal rates of Example 2 and Comparative Example 1 are the same as those of Example 1.
It is clear from FIG. 6 that the deterioration compared with Example 1 was due to the small amount of bacterial cells retained in the reaction tank.
【００３４】なお、ＵＡＳＢ反応槽の容積負荷量９ｋｇ
−ＣＯＤCr／ｍ3 ／日の場合、被処理水の滞留時間は４
時間であり、負荷量１８ｋｇ−ＣＯＤCr／ｍ3 ／日では
滞留時間２時間、負荷量２５ｋｇ−ＣＯＤCr／ｍ3 ／日
では滞留時間１．４時間である。The volume load of the UASB reaction tank is 9 kg.
-In the case of COD Cr / m 3 / day, the residence time of the treated water is 4
Time is 2 hours for a load of 18 kg-COD Cr / m 3 / day, and 1.4 hours for a load of 25 kg-COD Cr / m 3 / day.
【００３５】[0035]
【発明の効果】以上詳述した通り、本発明の嫌気性処理
法によれば、ＵＡＳＢ法による有機性排水の処理におい
て、グラニュール汚泥の沈降性を高め、汚泥の浮上、流
出を確実に防止してＵＡＳＢ反応槽内の汚泥保持量を高
く維持することにより、高負荷処理を安定して行うと共
に、処理水中への汚泥の流入を防止して、高水質処理水
を得ることが可能となる。As described in detail above, according to the anaerobic treatment method of the present invention, in the treatment of organic wastewater by the UASB method, the sedimentation property of granule sludge is enhanced, and the flotation and outflow of sludge are surely prevented. By maintaining a high sludge retention amount in the UASB reaction tank, it is possible to stably perform high-load treatment, prevent sludge from flowing into the treated water, and obtain high-quality treated water. .
【００３６】特に、本発明の嫌気性処理法によれば、Ｆ
ｅ塩及び／又はＳＯ4 2- 源の添加量の最適化が図れるた
め、過剰添加によるコスト向上を回避できると共に、過
剰添加による汚泥の活性低下、菌体保持量の低下を防止
して、高い処理性能を安定に維持することができる。Particularly, according to the anaerobic treatment method of the present invention, F
Since the amount of e-salt and / or SO 4 2- source added can be optimized, cost increase due to excessive addition can be avoided, sludge activity reduction and bacterial cell retention amount reduction due to excessive addition can be prevented, and high The processing performance can be stably maintained.
【図１】実施例１，２及び比較例１で用いた実験装置を
示す系統図である。FIG. 1 is a system diagram showing an experimental device used in Examples 1 and 2 and Comparative Example 1.
【図２】グラニュール汚泥中のＦｅ含有率と汚泥の浮上
ポテンシャルとの関係を示すグラフである。FIG. 2 is a graph showing the relationship between the Fe content in the granulated sludge and the floating potential of the sludge.
【図３】実施例１，２及び比較例１における容積負荷の
経時変化を示すグラフである。FIG. 3 is a graph showing changes over time in volume load in Examples 1 and 2 and Comparative Example 1.
【図４】実施例１，２及び比較例１におけるグラニュー
ル汚泥中のＦｅ含有率の経時変化を示すグラフである。FIG. 4 is a graph showing changes over time in the Fe content in the granulated sludge in Examples 1 and 2 and Comparative Example 1.
【図５】実施例１，２及び比較例１における汚泥の浮上
ポテンシャルの経時変化を示すグラフである。FIG. 5 is a graph showing changes with time in the floating potential of sludge in Examples 1 and 2 and Comparative Example 1.
【図６】実施例１，２及び比較例１における汚泥保持量
の経時変化を示すグラフである。FIG. 6 is a graph showing changes over time in the amount of sludge retained in Examples 1 and 2 and Comparative Example 1.
【図７】実施例１，２及び比較例１における溶解性ＣＯ
ＤCr除去率の経時変化を示すグラフである。FIG. 7: Soluble CO in Examples 1 and 2 and Comparative Example 1
It is a graph which shows the time-dependent change of a DCr removal rate.
１ ＵＡＳＢ反応槽 ２ 酸生成槽 1 UASB reaction tank 2 Acid generation tank
Claims (1)
ブランケットに有機性排水を上向流通水して嫌気性処理
する方法において、 グラニュール汚泥の全固形物質に対する鉄の含有率が３
重量％以上となるように、該有機性排水に鉄塩及び／又
は硫酸イオン源を添加することを特徴とする嫌気性処理
法。1. A method for anaerobic treatment by upwardly circulating organic wastewater to a sludge blanket formed of granule sludge, wherein the iron content of the total solid matter of the granule sludge is 3 or less.
An anaerobic treatment method, characterized in that an iron salt and / or a sulfate ion source is added to the organic waste water so as to be at least wt%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28324195A JP3814851B2 (en) | 1995-10-31 | 1995-10-31 | Anaerobic treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28324195A JP3814851B2 (en) | 1995-10-31 | 1995-10-31 | Anaerobic treatment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH09122683A true JPH09122683A (en) | 1997-05-13 |
| JP3814851B2 JP3814851B2 (en) | 2006-08-30 |
Family
ID=17662924
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP28324195A Expired - Fee Related JP3814851B2 (en) | 1995-10-31 | 1995-10-31 | Anaerobic treatment |
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| Country | Link |
|---|---|
| JP (1) | JP3814851B2 (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001252686A (en) * | 2000-03-10 | 2001-09-18 | Kurita Water Ind Ltd | Anaerobic treatment method for organic waste water |
| JP2006247601A (en) * | 2005-03-14 | 2006-09-21 | Tokyo Gas Co Ltd | Methanation method and apparatus |
| CN102260022A (en) * | 2011-06-02 | 2011-11-30 | 江苏加德绿色能源有限公司 | Biological enhanced brewery wastewater biotreatment device and method |
| CN102351381A (en) * | 2011-08-16 | 2012-02-15 | 复旦大学 | Device and method for treating sulfate wastewater |
| JP2012076001A (en) * | 2010-09-30 | 2012-04-19 | Kuraray Co Ltd | Anaerobic wastewater treatment apparatus |
| CN102583931A (en) * | 2012-03-19 | 2012-07-18 | 盐城同济环科固体废物处理处置有限公司 | Dual-circulation two-grade anaerobic digestion system and application thereof |
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1995
- 1995-10-31 JP JP28324195A patent/JP3814851B2/en not_active Expired - Fee Related
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001252686A (en) * | 2000-03-10 | 2001-09-18 | Kurita Water Ind Ltd | Anaerobic treatment method for organic waste water |
| JP2006247601A (en) * | 2005-03-14 | 2006-09-21 | Tokyo Gas Co Ltd | Methanation method and apparatus |
| JP2012076001A (en) * | 2010-09-30 | 2012-04-19 | Kuraray Co Ltd | Anaerobic wastewater treatment apparatus |
| CN102260022A (en) * | 2011-06-02 | 2011-11-30 | 江苏加德绿色能源有限公司 | Biological enhanced brewery wastewater biotreatment device and method |
| CN102351381A (en) * | 2011-08-16 | 2012-02-15 | 复旦大学 | Device and method for treating sulfate wastewater |
| CN102583931A (en) * | 2012-03-19 | 2012-07-18 | 盐城同济环科固体废物处理处置有限公司 | Dual-circulation two-grade anaerobic digestion system and application thereof |
| WO2013146853A1 (en) * | 2012-03-30 | 2013-10-03 | 栗田工業株式会社 | Method for treating fat-containing wastewater |
| JP2013208559A (en) * | 2012-03-30 | 2013-10-10 | Kurita Water Ind Ltd | Method for treating oil-and-fat-containing wastewater |
| JP2014023984A (en) * | 2012-07-25 | 2014-02-06 | Sumitomo Heavy Industries Environment Co Ltd | Methane fermentation system and methane fermentation method |
| JP2014133210A (en) * | 2013-01-10 | 2014-07-24 | Swing Corp | Anaerobic treatment method and anaerobic treatment apparatus of organic effluent |
| JP2016007595A (en) * | 2014-06-26 | 2016-01-18 | 住友重機械工業株式会社 | Anaerobic wastewater treatment method and anaerobic wastewater treatment apparatus |
| JP2015120169A (en) * | 2015-03-30 | 2015-07-02 | 株式会社東芝 | Water treatment system |
| CN105884022A (en) * | 2016-06-17 | 2016-08-24 | 中国工程物理研究院材料研究所 | Method and device for treating complicated waste water by iron enhanced microorganisms |
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