JP2003340498A - Deaeration method for pressure flotation concentrated froth and anaerobic digestion method using the same, and apparatus for these - Google Patents
Deaeration method for pressure flotation concentrated froth and anaerobic digestion method using the same, and apparatus for theseInfo
- Publication number
- JP2003340498A JP2003340498A JP2002153464A JP2002153464A JP2003340498A JP 2003340498 A JP2003340498 A JP 2003340498A JP 2002153464 A JP2002153464 A JP 2002153464A JP 2002153464 A JP2002153464 A JP 2002153464A JP 2003340498 A JP2003340498 A JP 2003340498A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- floss
- froth
- degassing
- pressure
- Prior art date
- 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.)
- Pending
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Degasification And Air Bubble Elimination (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【本発明の属する技術分野】本発明は、加圧浮上濃縮フ
ロスの脱気に係り、特に、水処理及び汚泥処理における
汚泥の加圧浮上濃縮設備において発生するフロスを脱気
処理する方法とそれを用いた嫌気性消化方法及びそれら
の装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to deaeration of pressurized flotation / concentration froth, and more particularly, to a method for deaeration of floss generated in a pressure flotation / concentration facility for sludge in water treatment and sludge treatment. TECHNICAL FIELD The present invention relates to an anaerobic digestion method using sucrose and devices thereof.
【０００２】[0002]
【従来の技術】水処理及び汚泥処理における加圧浮上濃
縮では、微細気泡を抱き込んだ濃縮汚泥であるフロスが
発生する。このフロスは、含気しているため体積が膨ら
み、そのままでは脱水処理等の汚泥処理を行うことが困
難であるため、脱気処理を要する。含気量が多く、撹拌
によって容易に脱気できるため、従来撹拌による脱気が
行われている。このような、従来の撹拌脱気では、目に
みえる気泡は除去できるが、特に高濃度のフロスの場
合、汚泥の粘性が高く、極微細な気泡は撹拌では脱気し
きれない。その結果、後段の槽での汚泥の溢れや脱水性
の悪化、さらに消化処理してる場合は、消化槽での汚泥
の発泡などが起きる場合がある。2. Description of the Related Art In the flotation under pressure by flotation in water treatment and sludge treatment, floss, which is concentrated sludge containing fine bubbles, is generated. Since this floss is aerated, its volume expands, and it is difficult to perform sludge treatment such as dehydration treatment as it is, so deaeration treatment is required. Since it has a large air content and can be easily degassed by stirring, degassing has conventionally been performed by stirring. In such conventional stirring and degassing, visible bubbles can be removed, but particularly in the case of high-concentration froth, sludge has a high viscosity and extremely fine bubbles cannot be completely degassed by stirring. As a result, the sludge may overflow in the subsequent tank, the dehydration property may deteriorate, and if the digestion treatment is performed, the sludge may foam in the digestion tank.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、前記従来技
術の問題点を解決し、濃縮フロス中に含有される気泡や
溶存気体成分を完全に除去でき、消化槽での発泡を抑制
し、消化ガス中に占めるメタンの純度を高めることがで
きるフロスの脱気方法とそれを用いる嫌気性消化方法及
びそれらの装置を提供することを課題とする。DISCLOSURE OF THE INVENTION The present invention solves the above-mentioned problems of the prior art, can completely remove bubbles and dissolved gas components contained in the concentrated froth, and suppresses foaming in the digestion tank, An object of the present invention is to provide a degassing method for floss capable of increasing the purity of methane in digestion gas, an anaerobic digestion method using the same, and an apparatus for them.
【０００４】[0004]
【課題を解決するための手段】上記課題を解決するため
に、本発明では、加圧浮上濃縮設備から排出されるフロ
スを減圧脱気することを特徴とするフロスの脱気方法と
したものである。前記フロスの脱気方法において、減圧
脱気は、真空度を−３３．３ｋＰａ〜−９３．３ｋＰａ
の範囲に減圧して行い、フロスに溶存している二酸化炭
素を０．５ｇ／Ｌ以下まで低減することができる。ま
た、本発明では、活性汚泥による水処理設備で発生する
余剰汚泥を嫌気性消化する方法において、前記余剰汚泥
を加圧浮上濃縮せしめ、得られたフロスを減圧脱気処理
して、フロスに含有される気泡及びの溶存気体成分を系
外に排出し、その脱気汚泥を嫌気性消化処理することと
したものである。さらに、本発明では、活性汚泥による
水処理設備で発生する余剰汚泥を濃縮する加圧浮上濃縮
装置と、該濃縮されたフロスを脱気処理する減圧脱気装
置とからなるフロスの脱気装置としたものであり、また
該装置で得られる脱気汚泥を嫌気性消化処理する汚泥消
化槽とからなる嫌気性消化装置としたものである。前記
装置において、減圧脱気装置は、濃縮フロスを該装置に
連続投入及び連続排出することが可能で、装置内を一定
の真空度に維持しながら効率よく脱気することが可能な
装置であるのがよい。In order to solve the above problems, the present invention provides a degassing method for floss, which is characterized in that degassing is performed for depressurizing the froth discharged from a pressurized flotation / concentration facility. is there. In the degassing method of the floss, the vacuum degassing has a vacuum degree of -33.3 kPa to -93.3 kPa.
It is possible to reduce the carbon dioxide dissolved in the floss to 0.5 g / L or less by reducing the pressure to the range described above. Further, in the present invention, in a method of anaerobically digesting excess sludge generated in a water treatment facility using activated sludge, the surplus sludge is pressure-floated and concentrated, and the obtained floss is subjected to degassing under reduced pressure, and contained in the floss The air bubbles and the dissolved gas components are discharged out of the system, and the degassed sludge is subjected to anaerobic digestion treatment. Furthermore, in the present invention, a degassing device for froth, which comprises a pressure flotation concentrator for concentrating excess sludge generated in a water treatment facility using activated sludge, and a decompression deaerator for degassing the concentrated froth. In addition, it is an anaerobic digester comprising a sludge digestion tank for anaerobic digestion of deaerated sludge obtained by the device. In the above apparatus, the vacuum degassing apparatus is an apparatus capable of continuously feeding and continuously discharging concentrated froth into the apparatus, and capable of efficiently degassing while maintaining a constant degree of vacuum inside the apparatus. Is good.
【０００５】[0005]
【発明の実施の形態】本発明者らは、鋭意検討を重ね、
加圧浮上濃縮のフロスに対して、減圧脱気処理を施すこ
とによって、ほぼ完全に脱気し、体積減量して後段の槽
での汚泥の溢れの抑制、消化槽での発泡の抑制が可能で
あることを見出し、本発明を完成するに至った。すなわ
ち、本発明によれば、活性汚泥法を採用した水処理設備
で発生する余剰汚泥を加圧浮上濃縮せしめ、得られたフ
ロスに減圧脱気処理することで、フロスに含有される気
泡の除去及び二酸化炭素等の溶存気体成分を系外に排出
し、その脱気汚泥を嫌気性消化処理することで、消化槽
での発泡を抑制し、更に消化ガス中に占める二酸化炭素
の割合を減少させることでメタンの純度を高めることが
できる。BEST MODE FOR CARRYING OUT THE INVENTION The present inventors have earnestly studied,
By performing degassing under reduced pressure on the pressure-floating concentrated floss, the degassing can be performed almost completely, and the volume can be reduced to prevent the overflow of sludge in the subsequent tank and the foaming in the digestion tank. Therefore, the present invention has been completed. That is, according to the present invention, excess sludge generated in a water treatment facility adopting the activated sludge method is floated and concentrated under pressure, and the obtained floss is subjected to degassing under reduced pressure to remove bubbles contained in the floss. And dissolved gas components such as carbon dioxide are discharged to the outside of the system, and the degassed sludge is subjected to anaerobic digestion treatment to suppress foaming in the digestion tank and further reduce the proportion of carbon dioxide in the digestion gas. Therefore, the purity of methane can be increased.
【０００６】以下に、本発明の形態を図面に基づいて詳
細に説明する。図１は、本発明のフロスの脱気方法を示
すフロー構成図である。図２は、余剰汚泥を加圧浮上濃
縮し、得られるフロスに減圧脱気処理を施し、その脱気
汚泥を嫌気性消化処理する方法を示すフロー構成図であ
る。図１では、加圧浮上濃縮槽２から発生するフロス３
に減圧脱気処理することで脱気汚泥１０を得る。減圧脱
気装置５において、フロスに減圧脱気処理を施すが、減
圧脱気処理としては、下記に示すような、例えば、特開
平７−１３６４０６号公報に開示されているような脱気
装置を使用することが望ましい。Embodiments of the present invention will be described below in detail with reference to the drawings. FIG. 1 is a flow configuration diagram showing a degassing method for floss according to the present invention. FIG. 2 is a flow configuration diagram showing a method for pressure-floating and concentrating surplus sludge, subjecting the obtained floss to decompression deaeration, and anaerobically digesting the deaerated sludge. In FIG. 1, floss 3 generated from the pressure flotation concentration tank 2
The degassed sludge 10 is obtained by vacuum degassing. In the vacuum degassing apparatus 5, the floss is subjected to vacuum degassing processing. As the vacuum degassing processing, for example, a degassing apparatus as disclosed in JP-A-7-136406 can be used. It is desirable to use.
【０００７】以下において、該脱気装置を使用した液体
の脱気処理プロセスに関し、詳細に説明する。含気した
フロス３は、汚泥ポンプ４により連続的に減圧脱気装置
５に供給される。汚泥ポンプ４は、必ずしも必要ではな
く、自然流下によって該脱気装置５にフロス３を供給す
ることも可能である。該脱気装置５内は、装置上部から
配管接続された真空ポンプ７により、常時真空の状態を
保っている。該装置に供給された処理液は、該装置内で
高速回転する円盤表面で遠心力を受けて加速され、該円
盤上で薄膜状にされる。薄膜状の処理液は、真空下にお
いて効率よく脱気され、さらに該遠心力により該真空容
器内の壁面に衝突することで、脱気効果が促進される。
これらの物理的処理により、フロス中の気泡は除去さ
れ、ヘンリーの法則の基づいて、ガスの溶解平衡反応式
から溶解成分までもが平衡移動し、ガス化されて除去さ
れる。The liquid degassing process using the degassing device will be described in detail below. The aerated floss 3 is continuously supplied to the vacuum degassing device 5 by the sludge pump 4. The sludge pump 4 is not always necessary, and it is also possible to supply the floss 3 to the deaerator 5 by natural flow. The inside of the deaerator 5 is always kept in a vacuum state by a vacuum pump 7 connected by piping from the upper part of the device. The treatment liquid supplied to the apparatus is subjected to a centrifugal force on the surface of the disk rotating at high speed in the apparatus to be accelerated and is made into a thin film on the disk. The thin-film processing liquid is efficiently degassed under vacuum, and further, the centrifugal force collides with the wall surface in the vacuum container to accelerate the degassing effect.
By these physical treatments, the bubbles in the floss are removed, and based on Henry's law, even the dissolved components of the gas from the equilibrium reaction equation to the equilibrium components are moved in equilibrium to be gasified and removed.
【０００８】図２では、活性汚泥法を採用した水処理設
備で発生する余剰汚泥１１を、加圧浮上濃縮槽１２にて
加圧浮上濃縮し、発生するフロス３に、減圧脱気装置１
３を用いて脱気することで得られる脱気汚泥１０を、汚
泥貯槽１４に貯める。そして、汚泥消化槽１５にて嫌気
性消化を施す。余剰汚泥には、微生物の活動により生成
する二酸化炭素が大量に溶存し、飽和濃度を超えると気
泡としてガス化する。この余剰汚泥のフロスを減圧脱気
することで、フロスが抱いている気泡と溶存しているガ
ス成分、特に二酸化炭素を除去し、系外に排出する。そ
の脱気汚泥を嫌気性消化処理することにより、通常得ら
れる消化ガスには、目的とするメタンの他に、二酸化炭
素が３３〜３５％存在し、純度の高いメタンを得るのに
大きな障害となっているが、本方法によれば、嫌気性消
化の前段で極力二酸化炭素を除去することで、汚泥消化
槽内における二酸化炭素量の軽減を図り、メタンの純度
を高めることができる。In FIG. 2, surplus sludge 11 generated in a water treatment facility adopting the activated sludge method is pressure-float-concentrated in a pressure-floatation concentration tank 12, and a defrosting device 1 under reduced pressure is generated in a floss 3 generated.
The degassed sludge 10 obtained by degassing using No. 3 is stored in the sludge storage tank 14. Then, anaerobic digestion is performed in the sludge digestion tank 15. A large amount of carbon dioxide generated by the activity of microorganisms is dissolved in the excess sludge, and when it exceeds the saturated concentration, it is gasified as bubbles. By degassing the floss of this excess sludge under reduced pressure, the gas components dissolved in the bubbles held by the floss, especially carbon dioxide, are removed and discharged from the system. By subjecting the degassed sludge to anaerobic digestion, the digested gas usually obtained contains 33 to 35% of carbon dioxide in addition to the target methane, which is a major obstacle to obtaining high-purity methane. However, according to this method, by removing carbon dioxide as much as possible before the anaerobic digestion, the amount of carbon dioxide in the sludge digestion tank can be reduced and the purity of methane can be increased.
【０００９】[0009]
【実施例】以下、本発明を実施例により具体的に説明す
る。
実施例１
以下に、本発明を実際に組み込んだ加圧浮上濃縮設備に
おいてフロスの脱気を目的として実施した一例を説明す
る。図３に、下水処理場における加圧浮上濃縮のフロス
の脱気を、本発明方法で行なう処理設備のフロー（ａ）
と従来法の処理フロー（ｂ）を併せて示す。本発明方法
及び従来法の処理フローは、共に汚泥の加圧浮上濃縮槽
１２から発生するフロスを各々減圧脱気装置１３、又は
撹拌脱気槽１６にて脱気し、脱気汚泥を汚泥貯槽１４に
貯める。そして汚泥消化槽１５に送り、消化する。本発
明による方法では、減圧脱気装置１３においてフロスを
減圧脱気することでフロスの体積減量と、二酸化炭素の
系外への排出によって汚泥貯槽１４並びに汚泥消化槽１
５での汚泥の発泡を抑制することが可能である。表１に
下水処理場の汚泥処理設備において、本発明方法を採用
した場合の処理成績と、従来方法による処理成績を示
す。EXAMPLES The present invention will be specifically described below with reference to examples. Example 1 Hereinafter, an example in which the present invention is actually incorporated for the purpose of degassing floss in a pressurized flotation / concentration facility will be described. FIG. 3 is a flow chart (a) of a treatment facility for degassing the pressure-floating and concentrating froth in the sewage treatment plant by the method of the present invention.
And the processing flow (b) of the conventional method are also shown. In the processing flow of the method of the present invention and the conventional method, the froth generated from the sludge pressurization flotation tank 12 is degassed by the vacuum degassing device 13 or the stirring degassing tank 16, respectively, and the degassed sludge is stored in the sludge storage tank Save to 14. Then, it is sent to the sludge digestion tank 15 for digestion. In the method according to the present invention, the volume of froth is reduced by degassing the froth in the depressurization deaerator 13, and the sludge storage tank 14 and the sludge digestion tank 1 are discharged by discharging carbon dioxide out of the system.
It is possible to suppress foaming of sludge in No. 5. Table 1 shows the treatment results when the method of the present invention is adopted in the sludge treatment equipment of the sewage treatment plant, and the treatment results by the conventional method.
【００１０】[0010]
【表１】 [Table 1]
【００１１】従来方法による撹拌脱気の場合、脱気汚泥
の比重が１．０００以上を上回ることはなく、最大で
０．９８０まで増加する。本発明方法による減圧脱気の
場合、常に１．０００以上を維持し、最大で１．０２５
まで増加した。これによる体積減量を計算すると、従来
方法ではフロスの体積が６６．３〜８８．８％となり、
本発明方法では６２．４〜７９．８％になる。減圧脱気
装置１３の排ガスを測定した結果、二酸化炭素が６〜１
０％含有され、フロス内に気泡として含まれる二酸化炭
素及び溶解している二酸化炭素が系外に排出されてい
る。ヘンリーの法則に基づいて、減圧脱気処理によって
汚泥に溶存するＣＯ2が系外に排出されることで、微生
物活動に伴って発生するＣＯ2が溶存し、飽和、発泡す
るまでの猶予時間が伸びることで、後段の汚泥貯槽１４
及び汚泥消化槽１５における発泡は減少する。溶存する
ＣＯ2量は、脱気前にフロス１Ｌに対して０．８４〜
０．９４Ｌ溶解していたＣＯ2量が、本方法では、脱気
汚泥１Ｌに対して０．０７〜０．０８Ｌまで低減され、
この時の大気放散量をフロス処理量７．４ｍ3／ｈから
計算すると、５．６〜６．４ｍ3／ｈに達する。従来法
では０．４〜１．２ｍ3／ｈに留まった。汚泥消化槽１
４において発生する消化ガスのＣＯ2とＣＨ4の濃度を測
定した結果、従来法では、ＣＯ2濃度が３３〜３５％
で、ＣＨ4濃度は６１〜６５％であったが、本方法を用
いると、ＣＯ2濃度が２７〜２９％で、ＣＨ4濃度は６７
〜７１％となった。In the case of stirring degassing by the conventional method, the specific gravity of the degassed sludge does not exceed 1.000 or more, and increases up to 0.980 at the maximum. In the case of vacuum degassing by the method of the present invention, 1.000 or more is constantly maintained and 1.025 at maximum.
Increased to. Calculating the volume loss due to this, the volume of floss becomes 66.3 to 88.8% by the conventional method,
In the method of the present invention, it is 62.4 to 79.8%. As a result of measuring the exhaust gas of the vacuum degassing device 13, carbon dioxide was 6 to 1
Carbon dioxide contained in 0% and contained as bubbles in the floss and dissolved carbon dioxide are discharged out of the system. Based on Henry's law, CO 2 dissolved in sludge is discharged out of the system by vacuum degassing, so that CO 2 generated due to microbial activity is dissolved, and a grace time until saturation and foaming occurs. By extending, the sludge storage tank 14 at the latter stage
And foaming in the sludge digestion tank 15 is reduced. The amount of dissolved CO 2 is 0.84 to 1 L of floss before deaeration.
In this method, 0.94 L of dissolved CO 2 was reduced to 0.07 to 0.08 L per 1 L of degassed sludge,
Calculating the atmospheric emission amount at this time from flossing amount 7.4 m 3 / h, reaching 5.6~6.4m 3 / h. In the conventional method, it remained at 0.4 to 1.2 m 3 / h. Sludge digestion tank 1
As a result of measuring the concentrations of CO 2 and CH 4 of the digestion gas generated in No. 4 , in the conventional method, the CO 2 concentration was 33 to 35%.
In, CH 4 concentration was the 61 to 65 percent, using the present method, CO 2 concentration is 27 to 29% CH 4 concentration 67
It became ~ 71%.
【００１２】[0012]
【発明の効果】以上に詳細に説明したように、本発明に
よれば、フロスを減圧脱気処理することで、その比重を
安定的に１．０００以上に維持し、脱気によって可能な
最大限の体積減量を得られる。また、フロス中に気泡と
して存在する二酸化炭素のみならず、ヘンリーの法則に
より汚泥に溶存する二酸化炭素までが系外に排出され、
元々溶存する二酸化炭素を１／１０まで低減することが
できるため、微生物活動に伴って発生するＣＯ2が溶存
し、飽和、発泡するまでの猶予時間が伸びることで、後
段の汚泥貯槽や汚泥消化槽における発泡は減少する。ま
た、余剰汚泥を加圧浮上濃縮し、そのフロスを減圧脱気
処理することで、溶存するＣＯ2を系外に排出し、その
脱気汚泥を嫌気性消化することで、消化ガス中のＣＯ2
が減少することにより、目的のＣＨ4の純度が増す。As described above in detail, according to the present invention, by degassing the floss, the specific gravity of the floss can be stably maintained at 1.000 or more, and the maximum amount possible by degassing. You can get a limit volume reduction. Also, not only carbon dioxide existing as bubbles in the floss but also carbon dioxide dissolved in sludge according to Henry's law is discharged out of the system,
Since the amount of carbon dioxide originally dissolved can be reduced to 1/10, CO 2 generated due to microbial activity is dissolved, and the grace time until saturation and foaming is extended, which results in the sludge storage tank and sludge digestion in the latter stage. Foaming in the bath is reduced. Further, excess sludge is pressure-floated and concentrated, and the froth is subjected to degassing under reduced pressure to discharge dissolved CO 2 out of the system, and the degassed sludge is anaerobically digested to remove CO 2 in digestion gas. 2
Is reduced, the purity of the target CH 4 is increased.
【図１】本発明のフロスの脱気方法を示すフロー構成
図。FIG. 1 is a flow configuration diagram showing a degassing method for floss according to the present invention.
【図２】本発明の余剰汚泥の嫌気性消化方法を示すフロ
ー構成図。FIG. 2 is a flow configuration diagram showing an anaerobic digestion method of excess sludge of the present invention.
【図３】実施例１に用いたフロー構成図で、（ａ）本発
明のフロー、（ｂ）従来法のフロー。FIG. 3 is a flow configuration diagram used in Example 1, (a) the flow of the present invention, (b) the flow of a conventional method.
１：汚泥、２：加圧浮上濃縮槽、３：フロス、４：汚泥
ポンプ、５：減圧脱気装置、６：分配機モータ、７：真
空ポンプ、８：汚泥排出ポンプ、９：排ガス、１０：脱
気汚泥、１１：余剰汚泥、１２：加圧浮上濃縮槽、１
３：減圧脱気装置、１４：汚泥貯槽、１５：汚泥消化
槽、１６：撹拌脱気槽1: Sludge, 2: Pressure floating flotation tank, 3: Floss, 4: Sludge pump, 5: Vacuum degassing device, 6: Distributor motor, 7: Vacuum pump, 8: Sludge discharge pump, 9: Exhaust gas, 10 : Deaeration sludge, 11: Excess sludge, 12: Pressurized flotation concentration tank, 1
3: Decompression deaerator, 14: Sludge storage tank, 15: Sludge digestion tank, 16: Agitation degassing tank
───────────────────────────────────────────────────── フロントページの続き (72)発明者 入内嶋 義治 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 (72)発明者 吉澤 毅 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 (72)発明者 萩野 隆生 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 Ｆターム(参考） 4D011 AA06 AA16 AB02 AC04 AD06 4D059 AA05 BA12 BA21 BA48 BE41 BK15 ─────────────────────────────────────────────────── ─── Continued front page (72) Inventor Yoshiharu Iriuchi 11-1 Haneda Asahi-cho, Ota-ku, Tokyo Co., Ltd. Inside the EBARA CORPORATION (72) Inventor Takeshi Yoshizawa 11-1 Haneda Asahi-cho, Ota-ku, Tokyo Co., Ltd. Inside the EBARA CORPORATION (72) Inventor Takao Hagino 11-1 Haneda Asahi-cho, Ota-ku, Tokyo Co., Ltd. Inside the EBARA CORPORATION F-term (reference) 4D011 AA06 AA16 AB02 AC04 AD06 4D059 AA05 BA12 BA21 BA48 BE41 BK15
Claims (5)
を減圧脱気することを特徴とするフロスの脱気方法。1. A degassing method for floss, which comprises degassing the floss discharged from a pressurized flotation concentrator.
Ｐａ〜−９３．３ｋＰａの範囲に減圧して行い、フロス
に溶存している二酸化炭素を０．５ｇ／Ｌ以下まで低減
することを特徴とする請求項１に記載のフロスの脱気方
法。2. The reduced pressure degassing has a vacuum degree of −33.3 k.
The degassing method for floss according to claim 1, wherein the carbon dioxide dissolved in the floss is reduced to 0.5 g / L or less by reducing the pressure to a range of Pa to -93.3 kPa.
剰汚泥を嫌気性消化する方法において、前記余剰汚泥を
加圧浮上濃縮せしめ、得られたフロスを減圧脱気処理し
て、フロスに含有される気泡及びの溶存気体成分を系外
に排出し、その脱気汚泥を嫌気性消化処理することを特
徴とする嫌気性消化方法。3. A method of anaerobically digesting excess sludge generated in a water treatment facility using activated sludge, wherein the excess sludge is pressure-floated and concentrated, and the resulting floss is degassed under reduced pressure to be contained in the floss. A method for anaerobic digestion, which comprises discharging air bubbles and dissolved gas components thereof out of the system and subjecting the deaerated sludge to anaerobic digestion.
剰汚泥を濃縮する加圧浮上濃縮装置と、該濃縮されたフ
ロスを脱気処理する減圧脱気装置からなることを特徴と
するフロスの脱気装置。4. Defrosting of floss, comprising a pressure flotation concentrator for concentrating excess sludge generated in a water treatment facility using activated sludge and a decompression deaerator for deaerating the concentrated floss. Qi device.
剰汚泥を濃縮する加圧浮上濃縮装置と、該濃縮されたフ
ロスを脱気処理する減圧脱気装置と、該脱気汚泥を嫌気
性消化処理する汚泥消化槽とからなることを特徴とする
嫌気性消化装置。5. A pressure floating flotation concentrator for concentrating surplus sludge generated in a water treatment facility using activated sludge, a decompression deaerator for deaeration of the concentrated floss, and an anaerobic digestion of the deaerated sludge. An anaerobic digester characterized by comprising a sludge digestion tank for treatment.
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| JP2002153464A JP2003340498A (en) | 2002-05-28 | 2002-05-28 | Deaeration method for pressure flotation concentrated froth and anaerobic digestion method using the same, and apparatus for these |
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|---|---|---|---|
| JP2002153464A JP2003340498A (en) | 2002-05-28 | 2002-05-28 | Deaeration method for pressure flotation concentrated froth and anaerobic digestion method using the same, and apparatus for these |
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Family
ID=29770497
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Cited By (5)
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| JP2007098273A (en) * | 2005-10-04 | 2007-04-19 | Sumitomo Heavy Ind Ltd | Method and apparatus for producing organic acid |
| JP2008188504A (en) * | 2007-02-01 | 2008-08-21 | Sumitomo Heavy Industries Environment Co Ltd | Anaerobic treatment system and anaerobic treatment method |
| WO2012020577A1 (en) * | 2010-08-12 | 2012-02-16 | 株式会社テクノプラン | Sludge thickening method and sludge thickening system |
| JP2012045512A (en) * | 2010-08-30 | 2012-03-08 | Techno Plan:Kk | Sludge treatment method, and sludge treatment system |
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2002
- 2002-05-28 JP JP2002153464A patent/JP2003340498A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007098273A (en) * | 2005-10-04 | 2007-04-19 | Sumitomo Heavy Ind Ltd | Method and apparatus for producing organic acid |
| JP2008188504A (en) * | 2007-02-01 | 2008-08-21 | Sumitomo Heavy Industries Environment Co Ltd | Anaerobic treatment system and anaerobic treatment method |
| JP4680945B2 (en) * | 2007-02-01 | 2011-05-11 | 住友重機械エンバイロメント株式会社 | Anaerobic treatment system and anaerobic treatment method |
| WO2012020577A1 (en) * | 2010-08-12 | 2012-02-16 | 株式会社テクノプラン | Sludge thickening method and sludge thickening system |
| JP2012040452A (en) * | 2010-08-12 | 2012-03-01 | Techno Plan:Kk | Method and system of sludge concentration |
| CN102762505A (en) * | 2010-08-12 | 2012-10-31 | 株式会社泰科企划 | Sludge thickening method and sludge thickening system |
| CN102762505B (en) * | 2010-08-12 | 2014-03-12 | 株式会社泰科企划 | Sludge thickening method and sludge thickening system |
| JP2012045512A (en) * | 2010-08-30 | 2012-03-08 | Techno Plan:Kk | Sludge treatment method, and sludge treatment system |
| WO2012029334A1 (en) * | 2010-08-30 | 2012-03-08 | 株式会社テクノプラン | Sludge treatment method and sludge treatment system |
| CN102781852A (en) * | 2010-08-30 | 2012-11-14 | 株式会社泰科企划 | Sludge treatment method and sludge treatment system |
| CN115321678A (en) * | 2022-08-04 | 2022-11-11 | 常州大学 | Kitchen garbage digestion foam removal control device |
| CN115321678B (en) * | 2022-08-04 | 2023-11-17 | 常州大学 | Kitchen waste digestion foam removal control device |
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