JP2021063699A - Device and method for monitoring belt press dewatering system, and device for controlling belt press dewatering system - Google Patents
Device and method for monitoring belt press dewatering system, and device for controlling belt press dewatering system Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000004744 fabric Substances 0.000 claims abstract description 48
- 239000007787 solid Substances 0.000 claims abstract description 29
- 239000010802 sludge Substances 0.000 claims abstract description 21
- 230000008859 change Effects 0.000 claims abstract description 6
- 230000002123 temporal effect Effects 0.000 claims abstract description 3
- 230000018044 dehydration Effects 0.000 claims description 20
- 238000006297 dehydration reaction Methods 0.000 claims description 20
- 238000012806 monitoring device Methods 0.000 claims description 17
- 238000004140 cleaning Methods 0.000 claims description 13
- 239000000701 coagulant Substances 0.000 claims description 8
- 238000005406 washing Methods 0.000 abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 15
- 238000005259 measurement Methods 0.000 description 20
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- 238000005345 coagulation Methods 0.000 description 18
- 230000015271 coagulation Effects 0.000 description 18
- 230000004520 agglutination Effects 0.000 description 13
- 230000002776 aggregation Effects 0.000 description 12
- 229920000642 polymer Polymers 0.000 description 12
- 238000002347 injection Methods 0.000 description 11
- 239000007924 injection Substances 0.000 description 11
- 208000005156 Dehydration Diseases 0.000 description 10
- 238000001514 detection method Methods 0.000 description 10
- 238000004220 aggregation Methods 0.000 description 9
- 239000002351 wastewater Substances 0.000 description 9
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- 230000035699 permeability Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- JKNCOURZONDCGV-UHFFFAOYSA-N 2-(dimethylamino)ethyl 2-methylprop-2-enoate Chemical compound CN(C)CCOC(=O)C(C)=C JKNCOURZONDCGV-UHFFFAOYSA-N 0.000 description 2
- DPBJAVGHACCNRL-UHFFFAOYSA-N 2-(dimethylamino)ethyl prop-2-enoate Chemical compound CN(C)CCOC(=O)C=C DPBJAVGHACCNRL-UHFFFAOYSA-N 0.000 description 2
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 229920006317 cationic polymer Polymers 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 229920001577 copolymer Polymers 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
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- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
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- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
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- 229920002873 Polyethylenimine Polymers 0.000 description 1
- 108010039918 Polylysine Proteins 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
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- 229910052782 aluminium Inorganic materials 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 238000005537 brownian motion Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
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- 230000007423 decrease Effects 0.000 description 1
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- 239000010419 fine particle Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229920001519 homopolymer Polymers 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000691 measurement method Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 229920000083 poly(allylamine) Polymers 0.000 description 1
- 229920000371 poly(diallyldimethylammonium chloride) polymer Polymers 0.000 description 1
- 229920000656 polylysine Polymers 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D33/00—Filters with filtering elements which move during the filtering operation
- B01D33/04—Filters with filtering elements which move during the filtering operation with filtering bands or the like supported on cylinders which are impervious for filtering
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D37/00—Processes of filtration
- B01D37/04—Controlling the filtration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/123—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using belt or band filters
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N21/00—Investigating or analysing materials by the use of optical means, i.e. using sub-millimetre waves, infrared, visible or ultraviolet light
- G01N21/17—Systems in which incident light is modified in accordance with the properties of the material investigated
- G01N21/47—Scattering, i.e. diffuse reflection
- G01N21/49—Scattering, i.e. diffuse reflection within a body or fluid
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Mechanical Engineering (AREA)
- Biochemistry (AREA)
- Hydrology & Water Resources (AREA)
- General Physics & Mathematics (AREA)
- Immunology (AREA)
- Pathology (AREA)
- Physics & Mathematics (AREA)
- Analytical Chemistry (AREA)
- General Health & Medical Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Treatment Of Sludge (AREA)
- Investigating Or Analysing Materials By Optical Means (AREA)
- Filtration Of Liquid (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
Description
汚泥をベルトプレスにより脱水処理するシステムの監視及び制御に関する。 It relates to the monitoring and control of a system for dehydrating sludge by a belt press.
ベルトプレス脱水機を用いた脱水処理において、安定した脱水処理を行うために脱水ケーキの剥離性を適切に評価することが求められている。無機凝集剤や高分子凝集剤の注入量を増加することで脱水ケーキの剥離性を改善する方法は有効であるが、どの程度の薬剤投入でどの程度の改善効果があるかを投入時点において数値で示すことは困難である。実際には薬剤投入後に脱水ケーキの剥離性をベルトプレス脱水機の濾布の汚れ具合を目視で判断していたが、この手法は人が現場にいる時にのみ可能な方法であるため連続的な監視は困難である。 In the dehydration treatment using a belt press dehydrator, it is required to appropriately evaluate the peelability of the dehydrated cake in order to perform a stable dehydration treatment. A method of improving the peelability of a dehydrated cake by increasing the injection amount of an inorganic flocculant or a polymer flocculant is effective. It is difficult to indicate with. Actually, the peelability of the dehydrated cake was visually judged by the degree of dirt on the filter cloth of the belt press dehydrator after the drug was added, but this method is continuous because it is possible only when a person is in the field. Monitoring is difficult.
特公昭６３−２９６３９号公報には、濾布の通気度を測定することで剥離性を評価することが記載されている。しかし、剥離性の評価は濾布の広い範囲にわたって評価する必要があるため、広範囲にわたって通気度を測定するためには大がかりな装置が必要となる。また、部分的に汚泥が十分に剥離している濾布では、その部分に集中して流体が通過するため、通気性で剥離性を正確に評価することは困難である。 Japanese Patent Application Laid-Open No. 63-29639 describes that the peelability is evaluated by measuring the air permeability of the filter cloth. However, since it is necessary to evaluate the peelability over a wide range of the filter cloth, a large-scale device is required to measure the air permeability over a wide range. Further, in a filter cloth in which sludge is sufficiently peeled off, it is difficult to accurately evaluate the peelability by air permeability because the fluid passes through the filter cloth in a concentrated manner.
特公平３−８００８０号公報には濾布洗浄排水中の懸濁物質濃度を測定することにより剥離性を評価することが記載されている。しかし、濾布洗浄排水中の懸濁物質は、塊として存在することがあるため、均一に液中に分散するとは限らない。そのため、濾布洗浄排水中の懸濁物質の濃度は、通常の光学式ＭＬＳＳ計では適切に測定することができない。 Japanese Patent Publication No. 3-800080 describes that the peelability is evaluated by measuring the concentration of suspended solids in the filter cloth washing wastewater. However, since the suspended solids in the filter cloth washing wastewater may exist as a lump, they are not always uniformly dispersed in the liquid. Therefore, the concentration of suspended solids in the filter cloth washing wastewater cannot be appropriately measured by a normal optical MLSS meter.
そこで、従来は、濾布洗浄排水中の懸濁物質濃度は、濾過分離重量測定法などにより分析されている。しかし、濾過分離重量測定方法などの方法は連続的に測定するためには装置が大がかりとなる。 Therefore, conventionally, the concentration of suspended solids in the filter cloth washing wastewater has been analyzed by a filtration separation weight measurement method or the like. However, a method such as a filtration separation weight measuring method requires a large-scale device for continuous measurement.
特許文献３には、レーザー光を水中に向けて照射し、水中のフロック等によって散乱される散乱光を受光して凝集状態を測定する凝集状態モニタリングセンサを用いて凝集剤添加を制御することが記載されている。
In
本発明は、上記のような問題に鑑み、ベルトプレス脱水機の汚泥剥離性を的確に監視できる監視システムおよび監視方法と、その監視した結果に基づいて、ベルトプレス脱水機を適切に制御することが可能なベルトプレス脱水機の制御装置を提供することを目的とする。 In view of the above problems, the present invention appropriately controls the belt press dehydrator based on a monitoring system and a monitoring method capable of accurately monitoring the sludge detachability of the belt press dehydrator and the monitoring result. It is an object of the present invention to provide a control device for a belt press dehydrator capable of performing the above.
本発明のベルトプレス脱水システムの監視装置は、ベルトプレス脱水機の濾布ベルト洗浄排水中の固形物の状態に対応した指標値の測定手段を有するベルトプレス脱水システムの監視装置であって、該測定手段は、濾布ベルト洗浄排水中にレーザ光を照射する照射部及び散乱光を受光する受光部を有し、散乱光強度信号の時間的な変化から前記指標値を求めるものである。 The monitoring device for the belt press dehydration system of the present invention is a monitoring device for the belt press dehydration system having a means for measuring an index value corresponding to the state of solid matter in the filter cloth belt cleaning drainage of the belt press dehydrator. The measuring means has an irradiation unit that irradiates the laser beam and a light receiving unit that receives the scattered light in the filter cloth belt cleaning drainage, and obtains the index value from the temporal change of the scattered light intensity signal.
本発明のベルトプレス脱水システムの監視方法は、本発明のベルトプレス脱水システムの監視装置を用い、前記指標値に基づいてベルトプレス脱水システムの監視を行うものである。 The method for monitoring the belt press dehydration system of the present invention uses the monitoring device for the belt press dehydration system of the present invention to monitor the belt press dehydration system based on the index value.
本発明のベルトプレス脱水機の制御装置は、本発明のベルトプレス脱水システムの監視装置を用い、前記指標値が所定値又は所定範囲内となるように被処理汚泥への凝集剤添加量を制御するものである。 The control device for the belt press dewatering machine of the present invention uses the monitoring device for the belt press dewatering system of the present invention to control the amount of coagulant added to the sludge to be treated so that the index value falls within a predetermined value or a predetermined range. Is what you do.
本発明の一態様では、前記散乱光強度信号の時間積分値に基づいて前記指標値を設定する。 In one aspect of the present invention, the index value is set based on the time integral value of the scattered light intensity signal.
本発明の一態様では、前記散乱光強度信号の所定時間毎のボトム値に基づいて前記指標値を設定する。 In one aspect of the present invention, the index value is set based on the bottom value of the scattered light intensity signal at predetermined time intervals.
本発明の一態様では、所定時間における前記散乱光強度信号のピークの数を検出し、各ピークの信号強度を所定時間で積算した値に基づいて前記指標値を設定する。 In one aspect of the present invention, the number of peaks of the scattered light intensity signal in a predetermined time is detected, and the index value is set based on the value obtained by integrating the signal intensity of each peak in a predetermined time.
発明者らは、特許文献３に記載の凝集状態モニタリングセンサにより、ベルトプレス濾布洗浄排水中の固形物の状態（固形物量や粒径分布の相対的な情報）を評価できることを見出した。
The inventors have found that the state of solid matter (relative information on the amount of solid matter and the particle size distribution) in the belt press filter cloth washing drainage can be evaluated by the agglomeration state monitoring sensor described in
濾布からの脱水ケーキの剥離性が悪化した場合、脱水ケーキが濾布上に張り付いて残る。この濾布上に残った脱水ケーキは洗浄水で洗い流され、濾布洗浄排水中に含まれることになる。従って、濾布洗浄排水中に含まれる固形物量が多いほど、剥離性が悪化していることになる。濾布洗浄排水中の固形物量の増加は、該凝集状態モニタリングセンサを用いて測定した場合、一定以上の散乱光強度を伴う信号波形の出現率上昇として検出できる。 When the detachability of the dehydrated cake from the filter cloth deteriorates, the dehydrated cake sticks to the filter cloth and remains. The dehydrated cake remaining on the filter cloth is washed away with washing water and is contained in the filter cloth washing drainage. Therefore, the larger the amount of solid matter contained in the filter cloth cleaning wastewater, the worse the peelability. The increase in the amount of solid matter in the filter cloth washing drainage can be detected as an increase in the appearance rate of the signal waveform accompanied by the scattered light intensity above a certain level when measured using the aggregation state monitoring sensor.
また、裏漏れ（凝集不良の汚泥液が素透し状に濾布を透過すること）やサイドリーク（濾布の両サイドから汚泥液が流れ出ること）現象が生じているときには、濾布洗浄排水中に固化前の泥状態の汚泥に由来する微小な粒子の量が増加する。これにより、該凝集状態モニタリングセンサの出力において、一定レベル以下の散乱光強度の信号波形の出現率が上昇したり、全体的な信号ベースレベルが上昇する。 In addition, when back leakage (sludge liquid with poor aggregation permeates the filter cloth in a transparent manner) or side leak (sludge liquid flows out from both sides of the filter cloth) occurs, the filter cloth cleaning drainage The amount of fine particles derived from the sludge in the mud state before solidification increases. As a result, in the output of the agglutination state monitoring sensor, the appearance rate of the signal waveform having a scattered light intensity of a certain level or less increases, or the overall signal base level increases.
本発明によれば、脱水ケーキの剥離性や裏漏れといった運転上の障害現象を数値化し、運転障害事象に対する運転時の目標値を設けることで凝集剤の注入量や濾布送り速度などの脱水機運転条件を連続的に制御できる。 According to the present invention, by quantifying operational obstacle phenomena such as dewatering cake peeling property and back leakage and setting a target value during operation for an operation obstacle event, dehydration such as an injection amount of a coagulant and a filter cloth feeding speed The machine operating conditions can be continuously controlled.
以下、図面を参照して実施の形態に係るベルトプレス脱水システムについて説明する。 Hereinafter, the belt press dehydration system according to the embodiment will be described with reference to the drawings.
図１の通り、このベルトプレス脱水システムでは、被処理汚泥である原汚泥は、流量計２を有する流入管１を介して第１凝集槽３に導入され、第１薬注装置４によって無機凝集剤が添加される。第１凝集槽３には撹拌機３ａが設置されている。
As shown in FIG. 1, in this belt press dewatering system, the raw sludge to be treated is introduced into the
第１凝集槽３内で凝集処理された液（第１凝集処理液）は、移流口（又は移流管）を介して第２凝集槽５に導入され、第２薬注装置６によって高分子凝集剤が添加される。第２凝集槽５には撹拌機５ａが設置されている。
The liquid (first coagulation-treated liquid) that has been coagulated in the
無機凝集剤としては塩化第二鉄、硫酸第二鉄、ポリ塩化第二鉄、ポリ硫酸第二鉄などの鉄系無機凝集剤や塩化アルミニウム、ポリ塩化アルミニウム、硫酸バンド、水酸化アルミニウム、酸化アルミニウムなどのアルミ系無機凝集剤が挙げられる。 Examples of the inorganic flocculant include ferric chloride, ferric sulfate, polyferric chloride, polyferric sulfate and other iron-based inorganic flocculants, aluminum chloride, polyaluminum chloride, sulfate band, aluminum hydroxide and aluminum oxide. Examples include aluminum-based inorganic flocculants such as.
高分子凝集剤としてはカチオン性又は両性の高分子凝集剤、とりわけカチオン性高分子凝集剤が好適である。カチオン性高分子凝集剤としては、ジメチルアミノエチルアクリレート或いはその四級化物、ジメチルアミノエチルメタクリレート或いはその四級化物などのカチオン性単量体の単独重合物やアクリルアミドとの共重合物、ポリビニルアミジン、ポリ（ジアリルジメチルアンモニウムクロリド）、ポリエチレンイミン、ポリアリルアミン、ポリビニルアミン、ポリ（２−ビニル−１−メチルピリニジウム）、ジアルキルアミン‐エピクロルヒドリン重縮合物、ポリリジン、キトサン、ジエチルアミノエチルデキストランなどが挙げられる。 As the polymer flocculant, a cationic or amphoteric polymer flocculant, particularly a cationic polymer flocculant is preferable. Examples of the cationic polymer flocculant include homopolymers of cationic monomers such as dimethylaminoethyl acrylate or quaternized products thereof, dimethylaminoethyl methacrylate or quaternized products thereof, copolymers with acrylamide, and polyvinylamidine. Examples thereof include poly (diallyldimethylammonium chloride), polyethyleneimine, polyallylamine, polyvinylamine, poly (2-vinyl-1-methylpyrinidium), dialkylamine-epichlorohydrin polycondensate, polylysine, chitosan, diethylaminoethyldextran and the like. ..
両性高分子凝集剤としては、ジメチルアミノエチルアクリレート或いはその四級化物やジメチルアミノエチルメタクリレート或いはその四級化物などのカチオン性単量体と、アクリルアミドなどのノニオン性単量体と、アクリル酸或いはその塩などとの共重合物を用いることができる。 Examples of the amphoteric polymer flocculant include cationic monomers such as dimethylaminoethyl acrylate or its quaternized product, dimethylaminoethyl methacrylate or its quaternized product, nonionic monomer such as acrylamide, and acrylic acid or its quaternized product. A copolymer with a salt or the like can be used.
第２凝集槽８内で凝集処理された汚泥は、移送管９を介してベルトプレス脱水機１０に送られる。
The sludge coagulated in the second coagulation tank 8 is sent to the
図１では、凝集槽３，５を設置しているが、無機凝集剤を配管１で添加し、凝集槽３を省略してもよい。
In FIG. 1, the
また、図１では、第２凝集槽５に高分子凝集剤を添加するものとしているが、第２凝集槽５の代わりに第２配管を設置し、該第２配管に高分子凝集剤を添加してもよい。
Further, in FIG. 1, the polymer coagulant is added to the
ベルトプレス脱水機１０は、無端回動する下側濾布ベルト及び上側濾布ベルトを備えている。凝集汚泥は、両者の間で挟圧され、脱水される。脱水ケーキは濾布から剥離され、取り出される。
The
濾布ベルトの洗浄排水の一部は配管１１を介して計測槽１２に送水される。計測槽１２には凝集状態モニタリングセンサ２０が設置されており、その検出信号が制御器８に入力される。制御器８はこの検出信号に基づいて第１及び第２薬注装置４，６を制御する。
A part of the cleaning drainage of the filter cloth belt is sent to the
凝集状態モニタリングセンサ２０は、好ましくは、特許文献３に記載のものが用いられる。図２はこの凝集状態モニタリングセンサのプローブ部分の構成を示している。このプローブは、直交する面２１ａ，２１ｂ及びそれらが交わる頂部２１ｃを有したブロック２１と、面２１ａに沿って設けられた、凝集処理液に向ってレーザ光を照射する発光部２２と、面２１ｂに沿って設けられた、受光光軸を該発光部２２の発光光軸と直交方向とした受光部２３とを有する。また、凝集状態モニタリングセンサ２０は、発光部２２の発光作動及び受光部２３の受光信号の解析を行うために、発光回路、検波回路及び計測回路（図示略）を備えている。計測回路は、タイミング回路、Ａ／Ｄ変換部、演算部等を有する。
As the agglutination
特許文献３と同様に、発光部２２から、頂部２１ｃ近傍の計測領域Ａに照射されたレーザー光が計測領域Ａ内の粒子によって散乱され、この散乱光が受光部２３で受光され、この受光強度の経時変化に基づいて凝集状態が計測される。なお、ブロック２１は不透明材料よりなる。
Similar to Patent
発光回路は、タイミング回路からの信号に応じて発光部に一定の変調周波数を持った電気信号を送り、レーザ発光を行わせる。発光部は、発光回路からの信号によって、レーザ光を発光する。受光部は、レーザ光が水中の懸濁物に当たって発生した散乱光を受けて、電気信号に変換する。検波回路は、受光部からの電気信号から変調成分を除去し、散乱光強度に応じた受光電圧を出力する。 The light emitting circuit sends an electric signal having a constant modulation frequency to the light emitting unit in response to the signal from the timing circuit to cause laser light emission. The light emitting unit emits laser light by a signal from the light emitting circuit. The light receiving unit receives the scattered light generated by the laser light hitting the suspension in water and converts it into an electric signal. The detection circuit removes the modulation component from the electric signal from the light receiving unit and outputs the light receiving voltage according to the scattered light intensity.
計測回路 は、発光回路に発光のための信号（特定の周波数変調波）を送信すると共に、検波回路からの信号をデジタル信号に変換し、論理演算して凝集に関する情報を出力する。 The measurement circuit transmits a signal for light emission (specific frequency modulated wave) to the light emitting circuit, converts the signal from the detection circuit into a digital signal, performs a logical operation, and outputs information on aggregation.
この凝集状態モニタリングセンサとしては、特許文献３のモニタリング装置、特にそれが特許された特許第６２８１５３４号公報に記載のモニタリング装置を好適に用いることができるが、これに限定されるものではない。
As the agglutination state monitoring sensor, the monitoring device of
なお、特許第６２８１５３４号の凝集モニタリング装置は、
「 凝集処理される被処理水の処理状態を監視する凝集モニタリング装置であって、
計測光を前記被処理水の計測領域に照射する計測光照射部と、
前記計測領域にある前記被処理水の粒子による散乱光を受光する散乱光受光部と、
前記散乱光受光部に得られる受光信号の振幅を計測する振幅計測手段を含み、計測された前記振幅の出現を監視および集計し、特定の振幅の発生率または発生頻度を算出して、前記被処理水中のフロックの粒径を表す前記被処理水の凝集に関わる指標を算出する計測値演算部と、
を備え、
前記振幅計測手段は、前記受光信号が上昇から下降に変化する第１の変曲点および下降から上昇に変化する第２の変曲点を検出し、前記第１の変曲点および第２の変曲点のレベル差から前記振幅を計測することを特徴とする凝集モニタリング装置。」
である。
The agglutination monitoring device of Japanese Patent No. 6281534 is available.
"A coagulation monitoring device that monitors the treatment status of the water to be coagulated.
A measurement light irradiation unit that irradiates the measurement area of the water to be treated with measurement light,
A scattered light receiving unit that receives scattered light by the particles of the water to be treated in the measurement area, and a scattered light receiving unit.
The subject includes an amplitude measuring means for measuring the amplitude of a received signal obtained by the scattered light receiving unit, monitors and aggregates the appearance of the measured amplitude, calculates the occurrence rate or occurrence frequency of a specific amplitude, and obtains the subject. A measurement value calculation unit that calculates an index related to the aggregation of the water to be treated, which represents the particle size of the flocs in the treated water.
With
The amplitude measuring means detects a first inflection point in which the received light signal changes from rising to falling and a second inflection point in which the received signal changes from falling to rising, and the first inflection point and the second inflection point. An agglomeration monitoring device characterized in that the amplitude is measured from the level difference of an inflection point. "
Is.
図３は、図２の計測領域Ａにおけるレーザー光Ｌの光軸と垂直な断面を示す模式図である。図３の通り、ある時点では、計測領域Ａに５個の粒子が存在している。この時点で計測領域Ａに照射されたレーザー光が、各粒子によって散乱され、散乱光Ｓが受光部１３に入射する。この時点から所定時間Δｔ（好ましくは０．１〜１０ｍＳｅｃの間から選定された時間。例えば、約１ｍＳｅｃ）が経過した時点では、計測領域Ａに存在する粒子数が変動する（理論上は、粒子数が変化しないこともあるが、粒子がブラウン運動し、また計測槽１２内に液が連続的に注入するので、通常は該粒子数は変動する。）。
FIG. 3 is a schematic view showing a cross section perpendicular to the optical axis of the laser beam L in the measurement region A of FIG. As shown in FIG. 3, at a certain point in time, five particles are present in the measurement region A. At this point, the laser light irradiated to the measurement region A is scattered by each particle, and the scattered light S is incident on the light receiving unit 13. When a predetermined time Δt (preferably a time selected from between 0.1 and 10 mSec, for example, about 1 mSec) elapses from this point, the number of particles existing in the measurement region A fluctuates (theoretically, the particles). Although the number may not change, the number of particles usually fluctuates because the particles move in Brownian motion and the liquid is continuously injected into the measuring
粒子数が変動すると、それに連動して散乱光強度が変動し、受光部２３の受光強度が変動する。
When the number of particles fluctuates, the scattered light intensity fluctuates in conjunction with it, and the light receiving intensity of the
粒子の粒径が大きいほど、１個の粒子が計測領域Ａに出入りしたときの該受光強度の変動幅が大きいものとなる。従って、この受光強度の変動幅から、計測領域Ａに出入りした粒子の粒径の大小を検出することができる。すなわち、任意の時刻ｔｋの受光強度と、Δｔ経過後の時刻ｔｋ＋１の受光強度との差は、該Δｔの間に計測領域Ａに出入りした粒子の表面積に比例した値となる。 The larger the particle size of the particles, the larger the fluctuation range of the light receiving intensity when one particle enters or exits the measurement region A. Therefore, it is possible to detect the size of the particle size of the particles entering and exiting the measurement region A from the fluctuation range of the light receiving intensity. That is, the difference between the light receiving intensity at an arbitrary time t k and the light receiving intensity at the time t k + 1 after the elapse of Δt is a value proportional to the surface area of the particles entering and exiting the measurement region A during the Δt.
図４は、凝集状態モニタリングセンサの散乱光強度を信号処理して得られる凝集状態モニタリングセンサ出力信号（受光信号強度）の経時変化の一例を示している。図４における出力信号は、受光部２３の受光強度（散乱光強度）に比例した値であり、単位は、例えばｍＶである。
FIG. 4 shows an example of a change over time in the output signal (light receiving signal intensity) of the aggregation state monitoring sensor obtained by signal processing the scattered light intensity of the aggregation state monitoring sensor. The output signal in FIG. 4 is a value proportional to the light receiving intensity (scattered light intensity) of the
この実施の形態では、センサの発光素子の消耗を抑制するために、発光素子を間欠的に作動させる。一例としては、図５のように、２００ｍＳｅｃ発光作動させた後、１８００ｍＳｅｃ停止するように、２秒に１回のペースで発光させる。なお、２００ｍＳｅｃ、１８００ｍＳｅｃ及び２秒は一例であり、これに限定されるものではない。 In this embodiment, the light emitting element is operated intermittently in order to suppress the consumption of the light emitting element of the sensor. As an example, as shown in FIG. 5, after the 200 mSec light emission is activated, the light is emitted at a pace of once every two seconds so as to stop the 1800 mSec. Note that 200 mSec, 1800 mSec and 2 seconds are examples, and the present invention is not limited to these.
この実施の形態では、凝集状態モニタリングセンサ２０の受光強度に基づいて濾布ベルト洗浄排水中の固形物量を評価し、この固形物量を濾布からの脱水ケーキの剥離性の指標として、無機凝集剤及び高分子凝集剤の添加制御を行う。
In this embodiment, the amount of solid matter in the filter cloth belt cleaning drainage is evaluated based on the light receiving intensity of the aggregation
凝集状態モニタリングセンサの受光信号強度から濾布ベルト洗浄排水中の固形物量を評価する方法の第１の態様は、図５のように、受光信号強度を時間で積分し、この積分値が大きいほど固形物量が多いと判定する方法である。図５では、時刻Ｔ（ｍＳｅｃ）〜Ｔ＋２００（ｍＳｅｃ）間、Ｔ＋２０００（ｍＳｅｃ）〜Ｔ＋２２００（ｍＳｅｃ）間、…のように２００ｍＳｅｃの発光期間の受光信号強度を積分している。即ち、図５でドットを付した部分の面積（Ｓ１，Ｓ２…）を経時的に測定している。 As shown in FIG. 5, the first aspect of the method of evaluating the amount of solid matter in the filter cloth belt cleaning drainage from the received signal intensity of the agglomeration state monitoring sensor is to integrate the received signal intensity with time, and the larger the integrated value, the larger the integrated value. This is a method for determining that the amount of solid matter is large. In FIG. 5, the received signal intensities during the light emission period of 200 mSec are integrated as in the time T (mSec) to T + 200 (mSec), T + 2000 (mSec) to T + 2200 (mSec), and so on. That is, over time measure the area (S 1, S 2 ...) of the portion denoted by the dots in FIG.
所定時間（例えば２００秒）間における各積分値Ｓ１，Ｓ２…の和又は平均値に基づいて濾布ベルト洗浄排水中の固形物量を評価する。 To evaluate the solid content in the filter cloth belt cleaning waste water, based on the integrated value S 1, S 2 ... sum or average value of between predetermined time (e.g. 200 seconds).
濾布ベルト洗浄排水中の固形物量を評価する方法の第２態様は、図６のように各発光期間時刻Ｔ（ｍＳｅｃ）〜Ｔ＋２００（ｍＳｅｃ）間、Ｔ＋２０００（ｍＳｅｃ）〜Ｔ＋２２００（ｍＳｅｃ）間、…の最小受光信号強度Ｉｍｉｎ（１），Ｉｍｉｎ（２），…を求める方法である。この方法では、所定時間（例えば１０分間。この１０分間に発光期間は３００個（１０×６０÷２＝３００）存在する。）における最小受光信号強度（以下、ボトム値ということがある。）Ｉｍｉｎ（１），Ｉｍｉｎ（２）…Ｉｍｉｎ（３００）の和又は平均値を求め、この値を濾布ベルト洗浄排水中の固形物量の指標値とする。 The second aspect of the method for evaluating the amount of solid matter in the filter cloth belt cleaning drainage is as shown in FIG. 6 during each light emission period time T (mSec) to T + 200 (mSec), T + 2000 (mSec) to T + 2200 (mSec), and so on. This is a method for obtaining the minimum received signal strengths Imin (1), Imin (2), .... In this method, the minimum received signal intensity (hereinafter, may be referred to as a bottom value) Imin at a predetermined time (for example, 10 minutes. There are 300 light emitting periods (10 × 60/2 = 300) in this 10 minutes). (1), Imin (2) ... Obtain the sum or average value of Imin (300), and use this value as an index value of the amount of solid matter in the filter cloth belt washing drainage.
上記第１の実施の態様、第２の実施の態様では、発光素子を間欠的に作動させる例で説明したが、発光素子は連続で作動させてもよい。この場合、発光素子が連続して発光している所定時間（例えば２００秒）を更に短い単位（例えば２００ｍＳｅｃ）に区切り、この単位時間での受光信号強度の積分値やボトム値を算出する。引き続き、この単位時間での受光信号強度の積分値やボトム値を、所定時間にわたって、更に積算あるいは平均（加算移動平均）する。そして、所定時間にわたって得られた積算値或いは平均値を濾布ベルト洗浄排水中の固形物量の指標値とする。 In the first embodiment and the second embodiment described above, the example of intermittently operating the light emitting element has been described, but the light emitting element may be continuously operated. In this case, a predetermined time (for example, 200 seconds) in which the light emitting element continuously emits light is divided into shorter units (for example, 200 mSec), and the integrated value and the bottom value of the received signal intensity in this unit time are calculated. Subsequently, the integrated value and the bottom value of the received signal intensity in this unit time are further integrated or averaged (additional moving average) over a predetermined time. Then, the integrated value or the average value obtained over a predetermined time is used as an index value of the amount of solid matter in the filter cloth belt washing drainage.
濾布ベルト洗浄排水中の固形物量を評価する方法の第３態様は、所定時間における受光信号強度のピークの数を検出し、各ピークの信号強度を積算する方法である、この積算値に基づいて固形物量を評価する。 The third aspect of the method of evaluating the amount of solid matter in the filter cloth belt washing drainage is a method of detecting the number of peaks of the received signal intensity at a predetermined time and integrating the signal intensity of each peak, based on this integrated value. And evaluate the amount of solids.
なお、上記所定時間は２００ｍＳｅｃ〜２０分、特に２００ｍＳｅｃ〜１０分の間から選ばれることが好ましく、上記の２００秒及び１０分は一例にすぎない。 The predetermined time is preferably selected from 200 mSec to 20 minutes, particularly 200 mSec to 10 minutes, and the above 200 seconds and 10 minutes are only examples.
濾布ベルト洗浄排水中の固形物量を評価する方法の第４態様を図７ａ，７ｂを参照して次に説明する。 A fourth aspect of the method for evaluating the amount of solid matter in the filter cloth belt cleaning drainage will be described below with reference to FIGS. 7a and 7b.
図７ａは、時刻ｔ１，ｔ２…ｔｚの各時刻において測定された受光信号強度をプロットしたグラフであり、各時刻の間隔Δｔ（すなわちｔｋ−ｔｋ−１）は前述の通り、好ましくは０．１〜１０ｍＳｅｃ、例えば１ｍＳｅｃである。
Figure 7a, the
図７ｂは、図７ａにおいて、極小点Ｐ１，Ｐ２…と、極大点Ｑ１，Ｑ２…とを記入し、極小点と極大点との差（以下、ピーク差ということがある。）ｈ１，ｈ２…を記入した説明図である。なお、ピーク差が所定値以下の微小な極小、極大は外乱との差異が不明であるため無視して処理する。例えば、ｈ１が所定値以下の場合、Ｐ１≧Ｐ２であればＰ１とＱ１は無視してデータ処理し、Ｐ１＜Ｐ２であればＱ１とＰ２は無視して、Ｐ１とＱ２との差をピーク差となるようデータ処理する。 In FIG. 7b, the minimum points P 1 , P 2 ... And the maximum points Q 1 , Q 2 ... Are entered in FIG. 7a, and the difference between the minimum points and the maximum points (hereinafter, may be referred to as a peak difference). It is explanatory drawing which filled in h 1 , h 2 .... It should be noted that the minute minimum and maximum peak difference of less than a predetermined value is ignored because the difference from the disturbance is unknown. For example, when h 1 is less than or equal to a predetermined value, if P 1 ≥ P 2 , P 1 and Q 1 are ignored and data processing is performed, and if P 1 <P 2 , Q 1 and P 2 are ignored. Data processing is performed so that the difference between P 1 and Q 2 becomes a peak difference.
上述の通り、任意の時刻ｔｋ−１の受光信号強度と時刻ｔｋの受光信号強度との差ｈｋは、時刻ｔｋ−１〜ｔｋ間に計測領域Ａに出入りした粒子の表面積に相関した値である。 As described above, the difference h k of the light-receiving signal intensity at an arbitrary time t k-1 of the light-receiving signal intensity and the time t k is between times t k-1 ~t k to the surface area of the out particles in the measurement region A It is a correlated value.
そこで、時刻ｔ１〜ｔｚのΔｔ・ｚ秒間（ｚは例えば２００とされ、Δｔ＝１ｍＳｅｃである場合Δｔ×ｚは０．２秒となる。）におけるすべてのピーク差ｈ１，ｈ２…ｈｎの和に基づいて濾布洗浄排水中の固形物量を評価する。 Therefore, all the peak differences h 1 , h 2 ... At the time t 1 to t z for Δt · z seconds (z is, for example, 200, and Δt × z is 0.2 seconds when Δt = 1 mSec). to evaluate the solid content in the filter cloth washing water discharge on the basis of the sum of the h n.
原汚泥への無機凝集剤の注入量を増加するに従って濾布洗浄排水中の固形物量が少なくなる。濾布洗浄排水中の固形物量と脱水ケーキの剥離性は相関し、脱水ケーキの剥離性が良いほど固形物量は少なくなる。上記第１〜第４のいずれかの方法で求められる固形物量指標値に目標値又は目標範囲を設定し、目標値（又は目標範囲上限値）より大きくなったときには目標値（又は目標範囲上限値以下）になるまで無機凝集剤の注入量を増加させる。また、目標値（又は目標範囲下限値）より小さくなったときには目標値（又は目標範囲下限値以上）になるまで無機凝集剤の注入量を減少させる（又は維持する）ことで、適正な薬注条件となるよう連続的な制御が可能となる。 As the amount of the inorganic flocculant injected into the raw sludge is increased, the amount of solid matter in the filter cloth washing wastewater decreases. The amount of solid matter in the filter cloth washing drainage correlates with the peelability of the dehydrated cake, and the better the peelability of the dehydrated cake, the smaller the amount of solid matter. A target value or a target range is set for the solid matter amount index value obtained by any of the first to fourth methods, and when the target value (or the upper limit of the target range) becomes larger than the target value (or the upper limit of the target range). Increase the injection amount of the inorganic flocculant until (below). In addition, when it becomes smaller than the target value (or the lower limit of the target range), the injection amount of the inorganic flocculant is reduced (or maintained) until it reaches the target value (or the lower limit of the target range or more), so that appropriate chemical injection is performed. Continuous control is possible so that the condition is met.
尚、検出する信号強度（上記第３の態様に関連）或いは強度差（上記第４の態様に関連）を２つ以上設けて、それぞれの検出数値に重みづけを行って指標化することも可能である。つまり、特定のレベル以上の信号強度或いは強度差を設け、前記レベルの倍強度までの信号強度或いは強度差の範囲での出現数をＡ、倍強度以上の信号強度或いは強度差の出現数をＢとする時、
Ｃ＝Ａ＋ｎＢ（ｎは信号強度差に基づき設定される係数である。）
で算出される剥離指標Ｃを求めて、Ｃが特定の値となるように無機凝集剤の注入量を制御する、または脱水機の濾布送り速度を調整する といった方法を採用してもよい。
It is also possible to provide two or more signal intensities to be detected (related to the third aspect) or intensity differences (related to the fourth aspect), and weight each detected value for indexing. Is. That is, a signal intensity or intensity difference of a specific level or higher is provided, the number of occurrences in the range of signal intensity or intensity difference up to the double intensity of the above level is A, and the number of occurrences of signal intensity or intensity difference of double intensity or higher is B. When
C = A + nB (n is a coefficient set based on the difference in signal strength)
The peeling index C calculated in 1 may be obtained, and a method such as controlling the injection amount of the inorganic flocculant so that C becomes a specific value or adjusting the filter cloth feeding speed of the dehydrator may be adopted.
また、裏漏れやサイドリーク等の、固化前の汚泥の混入が見られる場合においては、散乱光受光信号のベース電圧（特許第６２８１５３４号に述べる、フロック間の濁度）の上昇を伴う為、この値が一定値以上となった場合には、外部に警報を出力することで凝集槽での高分子凝集剤の増加を促す。または、前記一定値を下回るまで、直接高分子凝集剤の添加量を増加する などの制御を行ってもよい。 In addition, when sludge before solidification such as back leakage and side leakage is observed, the base voltage of the scattered light reception signal (the turbidity between flocs described in Patent No. 6281534) increases. When this value exceeds a certain value, an alarm is output to the outside to promote an increase in the polymer flocculant in the coagulation tank. Alternatively, control such as directly increasing the amount of the polymer flocculant added may be performed until the value falls below the certain value.
なお、濾布からのリーク（裏漏れ）は、汚泥が十分に凝集されていないために、汚泥（濁質）が濾布を通過する現象である。この場合、上記第２態様（図６）のボトム値は十分大きな値として検出されるが、凝集物はない或いは少ないため、所定値以上の信号強度（上記第３態様に関連）或いは強度差（上記第４態様に関連）を有するピークの出現率は低くなる。したがって、これらを解析することで、裏漏れと剥離性の悪化とを区別して判断することができる。 Leakage (back leakage) from the filter cloth is a phenomenon in which sludge (turbid substance) passes through the filter cloth because the sludge is not sufficiently aggregated. In this case, the bottom value of the second aspect (FIG. 6) is detected as a sufficiently large value, but since there is no or little agglomerates, the signal intensity (related to the third aspect) or the intensity difference (related to the third aspect) (related to the third aspect) or the intensity difference (related to the third aspect). The appearance rate of peaks having (related to the fourth aspect) is low. Therefore, by analyzing these, it is possible to distinguish between back leakage and deterioration of peelability.
また、サイドリーク状態では、サイドリークや裏漏れが無い状態で剥離性悪化が生じた場合に比較して、小さい粒径の懸濁物質が洗浄排水中に検出される。そのため、予め設定したレベル範囲のピークの出現率によりサイドリークが生じたことを判断することができる。 Further, in the side leak state, suspended solids having a smaller particle size are detected in the washing wastewater as compared with the case where the peelability is deteriorated in the state where there is no side leak or back leakage. Therefore, it can be determined that the side leak has occurred based on the appearance rate of the peak in the preset level range.
上記説明では、凝集状態モニタリングセンサの検出データに基づいて凝集剤添加量を制御しているが、汚泥供給量や濾布ベルトの走行速度を制御してもよく、これらを適宜組み合わせて制御してもよい。 In the above description, the amount of the coagulant added is controlled based on the detection data of the coagulation state monitoring sensor, but the sludge supply amount and the running speed of the filter cloth belt may be controlled, and these are appropriately combined and controlled. May be good.
［実施例１］
原汚泥として工場廃水の活性汚泥処理工程から排出された余剰汚泥を用い、ベルトプレス脱水機として栗田工業株式会社製ハイドプレス２２５０を用いた。無機凝集剤としてＰＡＣを用い、高分子凝集剤として栗田工業株式会社製クリフィックスＥＣ−４６６を用いた。濾布ベルト洗浄排水中の固形物状態の測定装置として、特許第６２８１５３４号に記載の凝集センサ（栗田工業株式会社製Ｓ．ｓｅｎｓｉｎｇ ＣＰ−Ｐ）を用いた。
[Example 1]
Excess sludge discharged from the activated sludge treatment process of factory wastewater was used as the raw sludge, and Hide Press 2250 manufactured by Kurita Water Industries, Ltd. was used as the belt press dehydrator. PAC was used as the inorganic flocculant, and Crifix EC-466 manufactured by Kurita Water Industries, Ltd. was used as the polymer flocculant. The aggregation sensor (S. sensing CP-P manufactured by Kurita Water Industries, Ltd.) described in Japanese Patent No. 6281534 was used as a measuring device for the state of solid matter in the filter cloth belt cleaning drainage.
図５に示した２００ｍＳｅｃ間の積分値の２００秒間の和を算出した。 The sum of the integrated values between the 200 mSecs shown in FIG. 5 for 200 seconds was calculated.
無機凝集剤添加量を１６４２，２４６２，又は４４５６ｍｇ／Ｌとし、高分子凝集剤添加量を２４４ｍｇ／Ｌとし、汚泥供給量９６Ｋｇ／ｈ，濾布速度７８ｍ／ｈとして脱水処理し、濾布からの脱水ケーキ剥離状況を観察した。結果を表１に示す。 The amount of the inorganic flocculant added was 1642, 2462, or 4456 mg / L, the amount of the polymer flocculant added was 244 mg / L, the sludge supply amount was 96 kg / h, and the filtration rate was 78 m / h. The state of dewatering cake peeling was observed. The results are shown in Table 1.
［実施例２］
実施例１において、図６に示した２００ｍＳｅｃのボトム値Ｉｍｉｎ（１）、Ｉｍｉｎ（２）…Ｉｍｉｎ（３００）を求め、それらの平均値を算出した。結果を表１に示す。
[Example 2]
In Example 1, the bottom values Imin (1), Imin (2) ... Imin (300) of 200 mSec shown in FIG. 6 were obtained, and their average values were calculated. The results are shown in Table 1.
表１の通り、無機凝集剤の注入量を増加させるほど濾布からの脱水ケーキ剥離性が良好になることが認められた。また、散乱光強度積分値や平均ボトム値が基準値以下（例えば前者の場合は４２Ｖ／２００秒以下、後者の場合は６３ｍＶ以下）となるように無機凝集剤を添加することにより、脱水ケーキ剥離性を良好に維持できることが認められた。 As shown in Table 1, it was found that the dewatering cake peelability from the filter cloth became better as the injection amount of the inorganic flocculant was increased. Further, by adding an inorganic flocculant so that the integrated value of scattered light intensity and the average bottom value are equal to or less than the reference value (for example, 42 V / 200 seconds or less in the former case and 63 mV or less in the latter case), the dehydrated cake is peeled off. It was confirmed that the sex could be maintained well.
３，５ 凝集槽
４，６ 薬注装置
８ 制御器
２０ 凝集状態モニタリングセンサ
3,5
Claims (7)
該測定手段は、濾布ベルト洗浄排水中にレーザ光を照射する照射部及び散乱光を受光する受光部を有し、散乱光強度信号の時間的な変化から前記指標値を求めるベルトプレス脱水システムの監視装置。 A monitoring device for a belt press dehydration system that has a means for measuring index values corresponding to the state of solid matter in the filter cloth belt cleaning drainage of the belt press dehydrator.
The measuring means has an irradiation unit that irradiates a laser beam in the filter cloth belt cleaning drainage and a light receiving unit that receives scattered light, and a belt press dehydration system that obtains the index value from a temporal change of a scattered light intensity signal. Monitoring device.
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| JPS63166500A (en) * | 1986-12-22 | 1988-07-09 | パサバント−ウエルケ・アクチエンゲゼルシヤフト | Method for conditioning and dehydrating sludge |
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| JPH1110199A (en) * | 1997-06-18 | 1999-01-19 | Meidensha Corp | Chemical injection method and apparatus for sludge dewatering process |
| JPH11104890A (en) * | 1997-10-02 | 1999-04-20 | Japan Organo Co Ltd | Belt press dehydrator |
| US6447687B1 (en) * | 1997-04-30 | 2002-09-10 | Ciba Specialty Chemcials Water Treatments Ltd. | Dewatering of sewage sludge |
| US20090255876A1 (en) * | 2008-04-11 | 2009-10-15 | Dunbar James M | Feedback control scheme for optimizing dewatering processes |
| JP2017026438A (en) * | 2015-07-22 | 2017-02-02 | 栗田工業株式会社 | Aggregation monitoring device, aggregation monitoring method and aggregation system |
| JP2018096768A (en) * | 2016-12-12 | 2018-06-21 | 栗田工業株式会社 | Method for aggregation monitoring, aggregation monitoring device, aggregation monitoring probe, and aggregation system |
| WO2019187698A1 (en) * | 2018-03-29 | 2019-10-03 | 栗田工業株式会社 | Method for controlling addition of flocculant, control device, and water treatment system |
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2019
- 2019-10-11 JP JP2019187889A patent/JP6897742B2/en active Active
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- 2020-09-10 WO PCT/JP2020/034237 patent/WO2021070545A1/en active Application Filing
- 2020-09-14 TW TW109131456A patent/TW202115379A/en unknown
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPS63166500A (en) * | 1986-12-22 | 1988-07-09 | パサバント−ウエルケ・アクチエンゲゼルシヤフト | Method for conditioning and dehydrating sludge |
| JPH06182399A (en) * | 1992-12-18 | 1994-07-05 | Kazunobu Hishitani | Dehydrator of sludge |
| US6447687B1 (en) * | 1997-04-30 | 2002-09-10 | Ciba Specialty Chemcials Water Treatments Ltd. | Dewatering of sewage sludge |
| JPH1110199A (en) * | 1997-06-18 | 1999-01-19 | Meidensha Corp | Chemical injection method and apparatus for sludge dewatering process |
| JPH11104890A (en) * | 1997-10-02 | 1999-04-20 | Japan Organo Co Ltd | Belt press dehydrator |
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| JP2018096768A (en) * | 2016-12-12 | 2018-06-21 | 栗田工業株式会社 | Method for aggregation monitoring, aggregation monitoring device, aggregation monitoring probe, and aggregation system |
| WO2019187698A1 (en) * | 2018-03-29 | 2019-10-03 | 栗田工業株式会社 | Method for controlling addition of flocculant, control device, and water treatment system |
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| WO2021070545A1 (en) | 2021-04-15 |
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