JP2012096210A - Treatment method and treatment apparatus of organic sludge - Google Patents
Treatment method and treatment apparatus of organic sludge Download PDFInfo
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- JP2012096210A JP2012096210A JP2010248619A JP2010248619A JP2012096210A JP 2012096210 A JP2012096210 A JP 2012096210A JP 2010248619 A JP2010248619 A JP 2010248619A JP 2010248619 A JP2010248619 A JP 2010248619A JP 2012096210 A JP2012096210 A JP 2012096210A
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- 239000010802 sludge Substances 0.000 title claims abstract description 244
- 238000000034 method Methods 0.000 title claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 238000000926 separation method Methods 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000010790 dilution Methods 0.000 claims abstract description 27
- 239000012895 dilution Substances 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 18
- 238000007865 diluting Methods 0.000 claims abstract description 16
- 239000000701 coagulant Substances 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 abstract 3
- 239000000243 solution Substances 0.000 abstract 1
- 238000002360 preparation method Methods 0.000 description 39
- 230000000052 comparative effect Effects 0.000 description 15
- 229920000642 polymer Polymers 0.000 description 13
- 150000001409 amidines Chemical class 0.000 description 11
- 230000002776 aggregation Effects 0.000 description 10
- 239000008394 flocculating agent Substances 0.000 description 10
- 238000004220 aggregation Methods 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 239000006228 supernatant Substances 0.000 description 5
- 230000004931 aggregating effect Effects 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 208000005156 Dehydration Diseases 0.000 description 3
- 125000005396 acrylic acid ester group Chemical group 0.000 description 3
- 238000005054 agglomeration Methods 0.000 description 3
- 229920006317 cationic polymer Polymers 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 3
- 230000004151 fermentation Effects 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- -1 acrylate ester Chemical class 0.000 description 2
- 229920006222 acrylic ester polymer Polymers 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 210000003608 fece Anatomy 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000010871 livestock manure Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000009264 composting Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000010794 food waste Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 125000005397 methacrylic acid ester group Chemical group 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 229920000058 polyacrylate Polymers 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
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Abstract
Description
本発明は、有機性汚泥の処理方法及び処理装置に関するものである。 The present invention relates to a method and apparatus for treating organic sludge.
従来、下水、屎尿、厨芥などの有機性物質を処理する工程で排出される有機性汚泥に対して凝集剤を添加、混合後に固液分離する工程において、特に一部のメタン発酵汚泥、腐敗汚泥、初沈汚泥等において非常に多くの凝集剤添加を要する場合があった。それは処理対象となる有機性汚泥中の溶解成分濃度やコロイダル成分等の一部が凝集剤と反応し凝集剤が消費されるために、汚泥中懸濁物質と反応する凝集剤の割合が小さくなることによりもたらされると推定される。有機性汚泥の固液分離の前処理に使用される一般的な凝集剤としてカチオン系高分子凝集剤がある。しかしながら、溶解成分濃度が比較的高い汚泥を対象とする場合は適応可能なカチオン系高分子凝集剤は種類が非常に限られたものとなるという問題があった。
更に、例えば、アミジン系凝集剤等は当該汚泥に対しても比較的適応性が高い場合が多いが、一般的にアミジン系凝集剤は高価である上にその添加率が高くなるとコストが膨大になるという問題があった。
Conventionally, in the process of adding a flocculant to the organic sludge discharged in the process of treating organic substances such as sewage, manure, and soot, and in the process of solid-liquid separation after mixing, especially some methane fermentation sludge and septic sludge In some cases, it was necessary to add a large amount of flocculant to the initial sludge. Because part of the dissolved component concentration and colloidal component in the organic sludge to be treated reacts with the flocculant and the flocculant is consumed, the proportion of the flocculant that reacts with the suspended substance in the sludge is reduced. It is estimated that There is a cationic polymer flocculant as a general flocculant used for pretreatment of solid-liquid separation of organic sludge. However, in the case where sludge with a relatively high concentration of dissolved components is targeted, there is a problem that the types of applicable cationic polymer flocculants are very limited.
Furthermore, for example, amidine-based flocculants and the like are often highly adaptable to the sludge. In general, amidine-based flocculants are expensive, and the addition rate increases and the cost becomes enormous. There was a problem of becoming.
一方、特許文献１には、凝集剤を添加して凝集した汚泥固形物を固液分離して得られた濃縮汚泥に、水を加えて希釈し、分散したのち、ふたたび凝集剤を添加して汚泥固形物を凝集させ、脱水機で脱水処理し、塩類濃度の低い脱水汚泥とし、農地や緑地に還元して再資源化することができる有機性汚泥の処理方法を提案している。 On the other hand, in Patent Document 1, water is added to the concentrated sludge obtained by solid-liquid separation of the sludge solids that have been aggregated by adding a flocculant, and after dispersion, the flocculant is added again. We have proposed a method for treating organic sludge that can agglomerate sludge solids, dehydrate it with a dehydrator to make dehydrated sludge with a low salt concentration, and recycle it into farmland and green spaces.
特許文献２には、廃水処理設備から発生する汚泥濃度が１〜５％の汚泥に凝集剤を添加して１次凝集処理を行い、次に１次凝集処理後の汚泥をその汚泥濃度が６〜８％となるように高濃度濃縮処理し、次いで濃縮処理後の汚泥に凝集剤を添加して２次凝集処理を行い、さらに２次凝集処理を行った高濃度汚泥に脱水処理を施すことにより、脱水処理の効率を向上させ、低含水率の脱水ケーキを安定して得る方法を提案している。
しかしながら、上記両文献には、凝集剤の使用量を低減する意図、及びそのために最初に凝集剤を添加する汚泥濃度１〜５％の有機性汚泥を希釈するという手段は記載がない。
In
However, neither of the above documents describes the intention of reducing the amount of the flocculant used and the means for diluting the sludge having a sludge concentration of 1 to 5% for which the flocculant is first added.
本出願人は、ポリ鉄、ＰＡＣ等の無機系凝集助剤や粉状高分子凝集剤、エマルジョンタイプの液状凝集剤、及びそれらの併用法等での固液分離処理等も試みたが、薬品使用コストやケーキ処分コスト等のトータルコストの最小化を目指した結果、図２に示す処理フローを採用した。
図２に示すフローは、有機性汚泥１を凝集汚泥調製槽２２へ移送し、添加される凝集剤４と反応させて、凝集汚泥５が調製される。該凝集汚泥５は、凝集汚泥分離濃縮装置２３に移送され、濃縮凝集汚泥７と分離水６とに固液分離される。濃縮凝集汚泥７は、脱水ケーキ調製装置２５に移送され、脱水ケーキ１１と分離水１０とに固液分離される。
これは、比較的高価であるアミジン系ポリマーを上記凝集剤４として単独で使用する凝集方法を採用し固液分離する方法が最も低コストであることが分かり運転を行っていたという経緯からである。
しかし、それでも上述のようにコスト削減が不十分であった。
本発明はかかる問題点に鑑みてなされたもので、その目的は、凝集剤の使用量を低減でき、かつ脱水ケーキ含水率を維持できる有機性汚泥の処理方法及びその処理装置を提供することにある。
The present applicant also tried solid-liquid separation treatment using inorganic agglomeration aids such as polyiron and PAC, powdery polymer flocculants, emulsion-type liquid flocculants, and their combined methods. As a result of aiming to minimize the total cost such as use cost and cake disposal cost, the processing flow shown in FIG. 2 was adopted.
In the flow shown in FIG. 2, the organic sludge 1 is transferred to the agglomerated
This is due to the fact that the method of solid-liquid separation using the flocculation method using a relatively expensive amidine-based polymer alone as the
However, the cost reduction was still insufficient as described above.
The present invention has been made in view of such problems, and an object of the present invention is to provide an organic sludge treatment method and a treatment apparatus capable of reducing the amount of the flocculant used and maintaining the moisture content of the dehydrated cake. is there.
本発明は、以下のとおりである。
１）有機性汚泥に対して希釈水を用いて希釈し、希釈汚泥を調製する工程、該希釈汚泥に対して固液分離を行わないで凝集剤を添加、混合し、凝集汚泥を調製する工程、該凝集汚泥を分離濃縮する工程、分離濃縮された濃縮凝集汚泥に対して凝集剤を添加、混合し、再濃縮凝集汚泥を調製する工程、該再濃縮凝集汚泥を脱水して脱水ケーキを調製する工程を含む、有機性汚泥の処理方法。
２）有機性汚泥に対して希釈水を用いて希釈し、希釈汚泥を調製する装置、該希釈汚泥に対して固液分離を行わないで凝集剤を添加、混合し、凝集汚泥を調製する槽、該凝集汚泥を分離濃縮する装置、分離濃縮された濃縮凝集汚泥に対して凝集剤を添加、混合し、再濃縮凝集汚泥を調製する槽、該再濃縮凝集汚泥を脱水して脱水ケーキを調製する装置を含む、有機性汚泥の処理装置。
本発明は、特に有機性汚泥に対して希釈水を用いて希釈し、希釈汚泥を調製することが従来では見られない重要な技術思想である。
The present invention is as follows.
1) Diluting organic sludge with dilution water to prepare diluted sludge, adding flocculant to the diluted sludge without solid-liquid separation, mixing to prepare agglomerated sludge A step of separating and concentrating the agglomerated sludge, a step of adding a flocculant to the separated concentrated agglomerated sludge, mixing and preparing a re-concentrated agglomerated sludge, and dehydrating the re-concentrated agglomerated sludge to prepare a dehydrated cake The process of processing organic sludge including the process to do.
2) An apparatus for preparing diluted sludge by diluting organic sludge with dilution water, and a tank for preparing agglomerated sludge by adding and mixing a flocculant without performing solid-liquid separation on the diluted sludge. , A device for separating and concentrating the agglomerated sludge, a tank for adding a flocculant to the separated concentrated agglomerated sludge, mixing and preparing a reconcentrated agglomerated sludge, and dehydrating the reconcentrated agglomerated sludge to prepare a dehydrated cake Organic sludge treatment equipment, including equipment to perform.
In the present invention, it is an important technical idea that has not been conventionally found to dilute organic sludge with diluted water to prepare diluted sludge.
本発明は、凝集剤の使用量を低減でき、かつ脱水ケーキ含水率を維持できるとともにＳＳ回収率も高く維持することができる。 The present invention can reduce the amount of the flocculant used, maintain the water content of the dehydrated cake, and maintain a high SS recovery rate.
以下、本発明を説明する。
本発明において、有機性汚泥とは、下水、屎尿、厨芥などの有機性物質を処理する工程で排出される汚泥を意味する。特に、本発明は、溶解成分やコロイダル成分等の含まれるＭアルカリ度が高い有機性汚泥の処理に好適である。該Ｍアルカリ度は、２５００ｍｇ／ｌ以上が好ましく、４５００ｍｇ／ｌ以上が更に好ましい。このような有機性汚泥としては、メタン発酵汚泥、腐敗汚泥、初沈汚泥等が挙げられる。
本発明において、「有機性汚泥に対して希釈水を用いて希釈し、希釈汚泥を調製する工程」を以下、「希釈工程」と、「有機性汚泥に対して希釈水を用いて希釈し、希釈汚泥を調製する装置」を以下、「希釈装置」ともいう。以下、「希釈工程」、「希釈装置」について説明する。
本発明は、処理が施される有機性汚泥の電気伝導度が１２００ｍＳ／ｍ以下、かつＭアルカリ度が４０００ｍｇ／ｌ以下となるように希釈工程又は希釈装置において、希釈水により希釈され、希釈汚泥とすることが好ましい。希釈装置としては、汚泥性状に応じて希釈のための槽、配管内混合装置のいずれを選択しても良い。希釈水は、通常の飲用水等の他、溶解成分等の濃度が比較的小さい等のある程度の条件を満たす水であれば処理プラント内のどのプロセス水を使用しても良い。希釈汚泥の電気伝導度は、１２００ｍＳ／ｍ以下が好ましく、７５０ｍＳ／ｍ以下が更に好ましい。希釈汚泥のＭアルカリ度は、４０００ｍｇ／ｌ以下が好ましく、２５００ｍｇ／ｌ以下が更に好ましい。また、希釈汚泥の温度は、３５℃以上が好ましく、５０〜７５℃が更に好ましい。上記温度は、希釈水として、上記温度のものを使用して容易に得ることができるが、特にその手段は制限がなく、ヒーター等を備えた希釈装置を用いてもよい。また、希釈装置は攪拌機等を備えていてもよい。上記各々の範囲は、本発明の課題を達成するために寄与することができる。
The present invention will be described below.
In this invention, organic sludge means the sludge discharged | emitted in the process of processing organic substances, such as sewage, manure, and soot. In particular, the present invention is suitable for the treatment of organic sludge having a high M alkalinity containing dissolved components and colloidal components. The M alkalinity is preferably 2500 mg / l or more, and more preferably 4500 mg / l or more. Examples of such organic sludge include methane fermentation sludge, septic sludge, and initial settling sludge.
In the present invention, "the step of diluting the organic sludge with dilution water and preparing the diluted sludge" is hereinafter referred to as the "dilution step" and "diluting the organic sludge with the dilution water, Hereinafter, the “apparatus for preparing diluted sludge” is also referred to as “dilution apparatus”. The “dilution step” and “dilution apparatus” will be described below.
In the present invention, the organic sludge to be treated is diluted with dilution water in a diluting step or diluting apparatus so that the electric conductivity of the treated sludge is 1200 mS / m or less and the M alkalinity is 4000 mg / l or less. It is preferable that As a dilution device, either a tank for dilution or a mixing device in a pipe may be selected according to the sludge properties. As the dilution water, any process water in the treatment plant may be used as long as it satisfies a certain condition such as the concentration of dissolved components is relatively small, in addition to normal drinking water. The electric conductivity of the diluted sludge is preferably 1200 mS / m or less, and more preferably 750 mS / m or less. The M alkalinity of the diluted sludge is preferably 4000 mg / l or less, and more preferably 2500 mg / l or less. The temperature of the diluted sludge is preferably 35 ° C. or higher, and more preferably 50 to 75 ° C. Although the said temperature can be easily obtained using the thing of the said temperature as dilution water, the means in particular does not have a restriction | limiting, You may use the dilution apparatus provided with the heater etc. Moreover, the dilution apparatus may be equipped with a stirrer or the like. Each of the above ranges can contribute to achieving the object of the present invention.
次に、本発明において、「希釈汚泥に対して固液分離を行わないで凝集剤を添加、混合し、凝集汚泥を調製する工程」を以下、「凝集汚泥調製工程」と、「希釈汚泥に対して固液分離を行わないで凝集剤を添加、混合し、凝集汚泥を調製する槽」を以下、「凝集汚泥調製槽」ともいう。以下、「凝集汚泥調製工程」、「凝集汚泥調製槽」について説明する。
本発明において、凝集汚泥調製工程は、希釈汚泥に対して固液分離を行わないで、すなわち、希釈汚泥に、直接、凝集剤を添加、混合し、凝集汚泥を調製する工程である。凝集汚泥調製槽は、上記凝集汚泥調製工程において、凝集汚泥を調製するための槽であり、適宜、希釈汚泥導入手段、凝集剤添加手段、攪拌手段、加温手段、凝集汚泥の引き抜き手段等を備える。凝集汚泥は、沈降分離性が高いことが好ましい。凝集汚泥は、そのフロックの直径、すなわちフロック径が数ミリ程度であることが、沈降分離性が高く好ましい。このような凝集汚泥を得るための凝集剤としては、特に限定されるべきものではないが、高分子凝集剤等が用いられる。また、ポリ硫酸第二鉄またはＰＡＣ等の無機系凝集助剤と高分子凝集剤の併用も凝集分離水の清澄度を高めるために有効な場合がある。高分子凝集剤としては、高価なアミジン系凝集剤も使用できるが、比較的安価なカチオンポリマー系凝集剤、例えば、アクリル酸エステル系、メタアクリル酸エステル系、アニオン度よりもカチオン度の高い両性系等を用いることができる。アクリル酸エステル系としては、分子量が３５０〜６００万のものが上記沈降分離性の高いものを得る上で好ましい。
Next, in the present invention, “the step of adding and mixing the flocculant without performing solid-liquid separation on the diluted sludge and preparing the agglomerated sludge” is hereinafter referred to as “the agglomerated sludge preparation step” and “the diluted sludge. On the other hand, a tank in which a flocculant is added and mixed without solid-liquid separation to prepare a coagulated sludge is also referred to as a “coagulated sludge preparation tank”. Hereinafter, the “aggregated sludge preparation step” and the “aggregated sludge preparation tank” will be described.
In the present invention, the coagulated sludge preparation step is a step of preparing coagulated sludge without performing solid-liquid separation on the diluted sludge, that is, adding and mixing the coagulant directly to the diluted sludge. The agglomerated sludge preparation tank is a tank for preparing agglomerated sludge in the above-described agglomerated sludge preparation step, and appropriately includes diluted sludge introduction means, aggregating agent addition means, agitation means, heating means, agglomerated sludge extraction means, and the like. Prepare. The agglomerated sludge preferably has a high sedimentation separation property. The aggregated sludge preferably has a floc diameter, that is, a floc diameter of about several millimeters because of high sedimentation separation. The flocculant for obtaining such flocculent sludge is not particularly limited, but a polymer flocculant or the like is used. Further, the combined use of an inorganic flocculating aid such as polyferric sulfate or PAC and a polymer flocculating agent may be effective for increasing the clarification of the flocculated separation water. As the polymer flocculant, an expensive amidine flocculant can be used, but a relatively inexpensive cationic polymer flocculant, for example, acrylate ester-based, methacrylic acid ester-based, amphoteric with higher cationicity than anionic degree A system or the like can be used. As the acrylic ester, those having a molecular weight of 3.5 to 6,000,000 are preferable for obtaining the above-described high sedimentation separation property.
次に、本発明において、「凝集汚泥を分離濃縮する工程」を以下、「凝集汚泥分離濃縮工程」と、「凝集汚泥を分離濃縮する装置」を以下、「凝集汚泥分離濃縮装置」ともいう。以下、「凝集汚泥分離濃縮工程」、「凝集汚泥分離濃縮装置」について説明する。
本発明において、凝集汚泥分離濃縮工程は、凝集汚泥調製工程で調製した凝集汚泥を分離濃縮された濃縮凝集汚泥と分離水に固液分離する工程である。凝集汚泥分離濃縮装置は、上記凝集汚泥分離濃縮工程において、凝集汚泥を濃縮凝集汚泥と分離水に固液分離する装置である。凝集汚泥分離濃縮装置は、特に限定されず、重力濃縮法が適用される単なる槽、遠心濃縮法が適用される遠心分離機、浮上濃縮法が適用される分離機、スクリーンを用いた分離機等が挙げられる。中でも、スクリーンを備えた固液分離装置が好ましく、例えば、一定間隔で平行に並ぶ複数のスクリーンと隣り合う該スクリーンの間で回転する複数の円盤により隣り合う該スクリーン間の隙間の凝集汚泥を物理的に排除するとともに濃縮凝集汚泥と分離水とに分別することが可能な固液分離装置が挙げられる。ここで、スクリーンのスリット幅は原理的に前記凝集汚泥調製工程で記載したフロック径未満であり、０.１〜２．５ｍｍが好ましい。本発明において、濃縮凝集汚泥の容積は、濃縮倍率が２．５〜８倍程度が好ましい。ここで、濃縮倍率とは、凝集汚泥の容積を濃縮凝集汚泥の容積で除した値を意味する。
Next, in the present invention, the “step for separating and concentrating the coagulated sludge” is hereinafter referred to as “the coagulated sludge separation and concentration step”, and the “device for separating and concentrating the coagulated sludge” is hereinafter also referred to as “coagulated sludge separation and concentration device”. Hereinafter, the “aggregated sludge separation and concentration step” and the “aggregated sludge separation and concentration device” will be described.
In the present invention, the agglomerated sludge separation and concentration step is a step of solid-liquid separation of the agglomerated sludge prepared in the agglomerated sludge preparation step into separated and concentrated agglomerated sludge and separated water. The agglomerated sludge separation / concentration apparatus is an apparatus for solid-liquid separation of the agglomerated sludge into the agglomerated sludge and separated water in the agglomerated sludge separation / concentration step. The coagulation sludge separation and concentration device is not particularly limited, and is simply a tank to which the gravity concentration method is applied, a centrifugal separator to which the centrifugal concentration method is applied, a separator to which the floating concentration method is applied, a separator using a screen, etc. Is mentioned. Among them, a solid-liquid separation device provided with a screen is preferable. For example, agglomerated sludge in a gap between adjacent screens is physically separated by a plurality of disks rotating in parallel with a plurality of screens arranged in parallel at regular intervals. And a solid-liquid separation device that can be separated into concentrated agglomerated sludge and separated water. Here, the slit width of the screen is in principle less than the floc diameter described in the agglomerated sludge preparation step, and is preferably 0.1 to 2.5 mm. In the present invention, the volume of the concentrated agglomerated sludge is preferably about 2.5 to 8 times the concentration ratio. Here, the concentration ratio means a value obtained by dividing the volume of the aggregated sludge by the volume of the concentrated aggregated sludge.
次に、本発明において、「分離濃縮された濃縮凝集汚泥に対して凝集剤を添加、混合し、再濃縮凝集汚泥を調製する工程」を以下、「再濃縮凝集汚泥調製工程」と、「分離濃縮された濃縮凝集汚泥に対して凝集剤を添加、混合し、再濃縮凝集汚泥を調製する槽」を以下、「再濃縮凝集汚泥調製槽」ともいう。以下、「再濃縮凝集汚泥調製工程」、「再濃縮凝集汚泥調製槽」について説明する。
本発明において、再濃縮凝集汚泥調製工程は、濃縮凝集汚泥に凝集剤を添加、混合し、脱水可能なフロックを含む再濃縮凝集汚泥を形成する工程である。再濃縮凝集汚泥調製槽は、上記再濃縮凝集汚泥調製工程において、再濃縮凝集汚泥を調製するための槽であり、適宜、濃縮凝集汚泥導入手段、凝集剤添加手段、攪拌手段、再濃縮凝集汚泥の引き抜き手段等を備える。再濃縮凝集汚泥は、脱水性が高いことが好ましい。再濃縮凝集汚泥は、後段の脱水工程におけるせん断力を受けた後もその粒状のフロック形状がわずかに残る程度の強度を持つフロックであることが好ましい。このような再濃縮凝集汚泥を得るための凝集剤としては、特に限定されるべきものではないが、高分子凝集剤が好ましい。高分子凝集剤としては、上記凝集汚泥調製工程に使用するものが挙げられ、同工程の凝集剤と同一でも異なっていてもよい。
Next, in the present invention, “the step of adding a flocculant to the separated concentrated flocculent sludge and mixing and preparing the reconcentrated flocculent sludge” is hereinafter referred to as “the reconcentrated flocculent sludge preparing step” and “the separation. A tank in which a flocculant is added to and mixed with the concentrated concentrated agglomerated sludge to prepare a reconcentrated agglomerated sludge is hereinafter also referred to as a “reconcentrated agglomerated sludge preparation tank”. Hereinafter, the “reconcentrated coagulated sludge preparation step” and the “reconcentrated coagulated sludge preparation tank” will be described.
In the present invention, the reconcentrated agglomerated sludge preparation step is a step of adding a flocculant to the concentrated agglomerated sludge and mixing it to form a reconcentrated agglomerated sludge containing dewaterable floc. The reconcentrated agglomerated sludge preparation tank is a tank for preparing the reconcentrated agglomerated sludge in the reconcentrated agglomerated sludge preparation step, and appropriately contains the concentrated agglomerated sludge introduction means, the aggregating agent addition means, the agitation means, and the reconcentrated agglomerated sludge. The drawing means is provided. The reconcentrated agglomerated sludge preferably has high dewaterability. The re-concentrated agglomerated sludge is preferably a floc having such a strength that the granular floc shape remains slightly even after receiving the shearing force in the subsequent dewatering step. The flocculant for obtaining such reconcentrated flocculent sludge is not particularly limited, but a polymer flocculant is preferable. Examples of the polymer flocculant include those used in the above-mentioned flocculent sludge preparation step, and may be the same as or different from the flocculant in the same step.
次に、本発明において、「再濃縮凝集汚泥を分離するとともに脱水して脱水ケーキを調製する工程」を以下、「脱水ケーキ調製工程」と、「再濃縮凝集汚泥を分離するとともに脱水して脱水ケーキを調製する装置」を以下、「脱水ケーキ調製装置」ともいう。以下、「脱水ケーキ調製工程」、「脱水ケーキ調製装置」について説明する。
本発明において、脱水ケーキ調製工程は、再濃縮凝集汚泥調製工程で調製した再濃縮凝集汚泥を脱水ケーキと分離水に固液分離する工程である。脱水ケーキ調製装置は、上記脱水ケーキ調製工程において、再濃縮凝集汚泥を脱水ケーキと分離水に固液分離する装置である。脱水ケーキ調製装置は、特に限定されず、通常、凝集汚泥分離濃縮装置と原理的に同じものを用いることができるが、凝集汚泥分離濃縮装置よりも脱水ケーキを分離するための再濃縮凝集汚泥への応力は高くすることが一般的であり、公知手段を用いることができる。脱水ケーキ調製装置は、再濃縮凝集汚泥へ応力を付与する手段と分離水を透過し、再濃縮凝集汚泥を保持するろ過手段から構成されることが好ましい。再濃縮凝集汚泥へ応力を付与する手段としては、プレス、遠心等が挙げられる。ろ過手段としては、開孔径が０．１〜２．５ｍｍのスクリ−ン等が挙げられる。本発明において、脱水ケーキの容積は、濃縮倍率が４〜１０倍程度が好ましい。ここで、濃縮倍率とは、再濃縮凝集汚泥の容積を脱水ケーキの容積で除した値を意味する。脱水ケーキ調製工程で分離された分離水は、ＳＳ濃度、Ｍアルカリ度、及び電気伝導度が小さく希釈水として用いることができる。脱水ケーキ調製工程で得られる脱水ケーキは、低含塩かつ低含水率であり、再資源化が可能であり、コンポスト、炭化などの二次加工等にも好適である。
Next, in the present invention, “the step of separating and dewatering the reconcentrated agglomerated sludge to prepare a dehydrated cake” is hereinafter referred to as “the dehydrated cake preparing step” and “the reconcentrated agglomerated sludge is separated and dehydrated for dehydration. Hereinafter, the “apparatus for preparing cake” is also referred to as “dehydrated cake preparation apparatus”. Hereinafter, the “dehydrated cake preparation process” and the “dehydrated cake preparation device” will be described.
In the present invention, the dehydrated cake preparation step is a step of solid-liquid separation of the reconcentrated agglomerated sludge prepared in the reconcentrated agglomerated sludge preparation step into a dehydrated cake and separated water. The dehydrated cake preparation device is a device that solid-liquid separates the reconcentrated agglomerated sludge into dehydrated cake and separated water in the dehydrated cake preparation step. The dewatered cake preparation device is not particularly limited, and normally, the same device as the coagulated sludge separation and concentration device can be used in principle, but the reconcentrated coagulated sludge for separating the dewatered cake is separated from the coagulated sludge separation and concentration device. In general, the stress is increased, and publicly known means can be used. The dewatered cake preparation device is preferably composed of a means for applying stress to the re-concentrated coagulated sludge and a filtering means that permeates the separated water and holds the re-concentrated coagulated sludge. Examples of means for applying stress to the re-concentrated agglomerated sludge include pressing and centrifuging. Examples of the filtering means include a screen having an opening diameter of 0.1 to 2.5 mm. In the present invention, the volume of the dehydrated cake is preferably about 4 to 10 times the concentration factor. Here, the concentration ratio means a value obtained by dividing the volume of the reconcentrated agglomerated sludge by the volume of the dewatered cake. The separated water separated in the dehydrated cake preparation step has a low SS concentration, M alkalinity, and electrical conductivity, and can be used as dilution water. The dehydrated cake obtained in the dehydrated cake preparation step has a low salt content and a low water content, can be recycled, and is suitable for secondary processing such as composting and carbonization.
次に、本発明の一例を、図１を参照して更に説明する。
有機性汚泥１に対して希釈水２を用いて希釈装置２１にて希釈し、希釈汚泥３を調製する。この希釈汚泥３は、該希釈汚泥３に対して固液分離を行わないで凝集汚泥調製槽２２へ移送され、添加される凝集剤４と反応させて、凝集汚泥５が調製される。該凝集汚泥５は、凝集汚泥分離濃縮装置２３に移送され、濃縮凝集汚泥７と分離水６とに固液分離される。濃縮凝集汚泥７は、再濃縮凝集汚泥調製槽２４に移送され、添加される凝集剤８と反応して、再濃縮凝集汚泥９が調製される。該再濃縮凝集汚泥９は、脱水ケーキ調製装置２５に移送され、脱水ケーキ１１と分離水１０とに固液分離される。
上記処理フローは、自動制御であってよいし、バッチ処理であってもよいし、その組み合わせであってもよい。また、各種汚泥の温度制御も自動化してもよい。
Next, an example of the present invention will be further described with reference to FIG.
The diluted
The processing flow may be automatic control, batch processing, or a combination thereof. In addition, temperature control of various sludges may be automated.
以下、本発明の実施例を説明する。以下に、本発明を実際に組み込んだ実験プラントによる運転結果の一例について詳細に説明する。本実証実験は約１ヶ月行った。なお、本発明はこの実施例により何等制限されるものではない。
本発明の処理フローは、図１の態様に従った。Ａ処理施設において食品系廃棄物を主体とする有機物をメタン発酵処理する工程で発生した有機性汚泥を最終的にスクリュープレス型脱水機等で固液分離するフローである。表１に処理される有機性汚泥１の約１ヶ月の性状を示す。汚泥の加温は１００％Ａ処理施設で発生する余剰バイオガスを活用した熱を利用した。なお、各例において用いた凝集剤のアミジン系又はアクリル酸エステル系はそれぞれ同じものである。
Examples of the present invention will be described below. Below, an example of the operation result by the experimental plant which actually incorporated this invention is demonstrated in detail. This demonstration experiment was conducted for about one month. In addition, this invention is not restrict | limited at all by this Example.
The processing flow of the present invention followed the embodiment of FIG. This is a flow in which organic sludge generated in the process of subjecting organic matter mainly composed of food waste to methane fermentation treatment in the processing facility A is finally solid-liquid separated with a screw press type dehydrator or the like. Table 1 shows the properties of the treated organic sludge 1 for about one month. The sludge was heated using heat generated from surplus biogas generated at the 100% A treatment facility. In addition, the amidine type | system | group or acrylic acid ester type | system | group of the coagulant | flocculant used in each example is the same respectively.
実施例１
有機性汚泥を希釈水にて３倍に希釈し、２８℃の希釈汚泥とし、この希釈汚泥にアミジン系凝集剤を反応させて、凝集汚泥を調製した。該凝集汚泥を、凝集汚泥分離濃縮装置に移送し、濃縮凝集汚泥と分離水とに固液分離した。濃縮凝集汚泥を、再濃縮凝集汚泥調製槽に移送し、上記と同じアミジン系凝集剤と反応させて、再濃縮凝集汚泥を調製した。該再濃縮凝集汚泥を、脱水ケーキ調製装置に移送し、脱水ケーキと分離水とに固液分離した。
Example 1
The organic sludge was diluted 3 times with dilution water to obtain a 28 ° C. diluted sludge, and the diluted sludge was reacted with an amidine flocculant to prepare agglomerated sludge. The agglomerated sludge was transferred to an agglomerated sludge separation / concentration device, and solid-liquid separated into concentrated agglomerated sludge and separated water. The concentrated flocculated sludge was transferred to a reconcentrated flocculated sludge preparation tank and reacted with the same amidine flocculant as described above to prepare a reconcentrated flocculated sludge. The re-concentrated agglomerated sludge was transferred to a dehydrated cake preparation apparatus, and solid-liquid separated into dehydrated cake and separated water.
実施例２
実施例１において、凝集汚泥及び濃縮凝集汚泥への凝集剤として、アクリル酸エステル系ポリマーを用いた以外は、同じ処理を行った。
実施例３
実施例２において、希釈汚泥の温度を５５℃とした以外は、同じ処理を行った。
Example 2
In Example 1, the same treatment was performed except that an acrylic ester polymer was used as a flocculant for the flocculent sludge and the concentrated flocculent sludge.
Example 3
In Example 2, the same treatment was performed except that the temperature of the diluted sludge was 55 ° C.
比較例１
図２のフローで、凝集汚泥調製槽２２の有機性汚泥の温度を２８℃とし、凝集剤として、アミジン系ポリマーを用いて凝集汚泥５を調製した。該凝集汚泥５を、凝集汚泥分離濃縮装置２３に移送し、濃縮凝集汚泥７と分離水６とに固液分離した。濃縮凝集汚泥７を、脱水ケーキ調製装置２５に移送し、脱水ケーキ１１と分離水１０とに固液分離した。
比較例２
比較例１において、凝集剤として、実施例２と同じアクリル酸エステル系ポリマーを用いた以外は、同じ処理を行った。
比較例３
比較例１において、凝集汚泥調製前に、有機性汚泥を３倍に希釈後１時間静置後に上澄み水を全体の２／３分離して沈降した汚泥（３倍希釈前のボリューム）を用いる洗浄工程を採用した以外は、同じ処理を行った。
Comparative Example 1
In the flow of FIG. 2, the temperature of the organic sludge in the coagulated
Comparative Example 2
In Comparative Example 1, the same treatment was performed except that the same acrylate polymer as in Example 2 was used as the flocculant.
Comparative Example 3
In Comparative Example 1, before the agglomerated sludge was prepared, the organic sludge was diluted 3 times and then allowed to stand for 1 hour, and then the supernatant water was separated and settled by separating 2/3 of the whole supernatant water (volume before 3 times dilution). The same process was performed except that the process was adopted.
上記実施例１〜３、比較例１〜３の結果を表１とともに表２に示す。表２の希釈倍率は、希釈後の希釈汚泥容積を希釈前の有機性汚泥の容積で除した値である。また、凝集状態は、以下により評価した。
○：凝集状態及び固液分離性がともに良好。
△：凝集状態は良好だが固液分離性は悪い。
×：凝集状態及び固液分離性がともに悪いまたは凝集せず。
The results of Examples 1 to 3 and Comparative Examples 1 to 3 are shown in Table 2 together with Table 1. The dilution factor in Table 2 is a value obtained by dividing the diluted sludge volume after dilution by the volume of organic sludge before dilution. Moreover, the aggregation state was evaluated by the following.
○: Both the aggregated state and the solid-liquid separation property are good.
(Triangle | delta): Although an aggregation state is favorable, solid-liquid separability is bad.
X: Both the aggregation state and the solid-liquid separation property are poor or do not aggregate.
表１に示すように、この有機性汚泥は、固形物（ＴＳ）濃度がほぼ３０ｇ／ｌ以上と比較的高い上に塩類や金属イオン等の溶解性成分（ＴＳ−ＳＳ）濃度も１０ｇ／ｌ以上と非常に高い。
実施法１〜３及び比較例１〜３の結果について解説する。比較例２では本願発明法の構成要件の一つである希釈工程は行わず比較的安価で一般的に使用されるアクリル酸エステル系ポリマーの凝集剤を使用したが、凝集剤総添加率（ＴＳに対する添加率）を１．５〜４．０％の範囲で変化させても脱水可能な凝集フロックが得られなかった。比較例１では比較的高価なアミジン系ポリマーの凝集剤を凝集剤総添加率２．８％で使用して約８０％のケーキ含水率を得た。比較例３では汚泥を洗浄後凝集及び脱水した。すなわち汚泥に対して水道水を２倍量添加混合し、１時間静置後上澄水を全体の２／３系外に排出した後に、アミジン系ポリマー凝集剤を凝集剤総添加率１．９％添加して脱水した結果約８０％のケーキ含水率を得た。しかしながら、比較例３では洗浄工程で分離する上澄水中に含まれるＳＳが多いことから、ＳＳ回収率は比較例２の９１．２％より２６％低い６５％となり該分離上澄水の水処理負荷増大等を考慮すると採用不可能な方式であった。実施例１では本発明法に準じて汚泥を３倍希釈後アミジン系ポリマー凝集剤を凝集剤総添加率２．０％添加することでケーキ含水率約８０％のケーキを得ることができ、比較例２と比較して約３割の凝集剤削減効果があった。実施例２では本発明法に準じて汚泥を３倍希釈後、アクリル酸エステル系ポリマー凝集剤を凝集剤総添加率１．６％添加することで脱水ケーキ含水率約８０％のケーキを得ることができ、比較例２と比較して約５割の凝集剤削減効果があった。実施例３では本発明法に準じて汚泥と希釈水を５５℃に加温した状態で３倍希釈後、アクリル酸エステル系ポリマー凝集剤を凝集剤総添加率１．４％添加することでケーキ含水率約８０％のケーキを得ることができ、比較例２と比較して約６割の凝集剤削減効果があった。実施例１〜３では汚泥に凝集剤を添加する前に「洗浄」することなく「希釈」方式を選択していることからのＳＳ回収率はいずれも９２％以上であり比較例３よりも大幅に回収率が高かった。
以上説明したように、本発明法による有機性汚泥の処理方法及び処理装置を採用することにより、脱水ケーキ含水率、及びＳＳ回収率を大きく損なうことなく薬品コストを従来法の半分以下にする処理が可能となることが理解できる。
As shown in Table 1, this organic sludge has a relatively high solid (TS) concentration of approximately 30 g / l or more, and also has a concentration of soluble components (TS-SS) such as salts and metal ions of 10 g / l. Above and very high.
The results of Examples 1 to 3 and Comparative Examples 1 to 3 will be described. In Comparative Example 2, the diluting step which is one of the constituent elements of the method of the present invention is not performed, and a flocculating agent of an acrylic ester polymer that is generally used at a relatively low cost is used. The aggregation floc that can be dewatered was not obtained even when the addition ratio was changed in the range of 1.5 to 4.0%. In Comparative Example 1, a relatively expensive amidine polymer flocculant was used at a total flocculant addition rate of 2.8% to obtain a cake water content of about 80%. In Comparative Example 3, the sludge was washed and then coagulated and dehydrated. That is, double the amount of tap water is added to and mixed with sludge, and after standing for 1 hour, the supernatant water is discharged out of the entire 2/3 system, and then the amidine-based polymer flocculant is added 1.9%. As a result of adding and dehydrating, a cake water content of about 80% was obtained. However, in Comparative Example 3, since the SS contained in the supernatant water separated in the washing step is large, the SS recovery rate is 65%, which is 26% lower than 91.2% in Comparative Example 2, and the water treatment load of the separated supernatant water Considering the increase, etc., it was a method that could not be adopted. In Example 1, according to the method of the present invention, a cake having a moisture content of about 80% can be obtained by diluting sludge three times and adding an amidine polymer flocculant to a total flocculant addition rate of 2.0%. Compared to Example 2, there was about 30% of the flocculant reduction effect. In Example 2, according to the method of the present invention, after sludge is diluted three times, a cake having a moisture content of about 80% dehydrated cake is obtained by adding 1.6% of the total amount of flocculating agent of acrylic acid ester polymer flocculant. As compared with Comparative Example 2, the flocculant was reduced by about 50%. In Example 3, in accordance with the method of the present invention, the sludge and the diluted water were heated to 55 ° C. and diluted 3 times, and then the acrylic acid ester polymer flocculant was added at a total flocculant addition rate of 1.4%. A cake having a water content of about 80% could be obtained, and there was an effect of reducing the flocculant by about 60% compared to Comparative Example 2. In Examples 1 to 3, the SS recovery rate is 92% or more from the fact that the “dilution” method is selected without “washing” before adding the flocculant to the sludge, which is significantly larger than Comparative Example 3. The recovery rate was high.
As described above, by adopting the organic sludge treatment method and treatment apparatus according to the present invention, the chemical cost is reduced to less than half that of the conventional method without greatly deteriorating the moisture content of the dehydrated cake and the SS recovery rate. Can be understood.
１…有機性汚泥、２…希釈水、３…希釈汚泥、４…凝集剤、５…凝集汚泥、６…分離水、７…濃縮凝集汚泥、８…凝集剤、９…再濃縮凝集汚泥、１０…分離水、１１…脱水ケーキ、２１…希釈装置、２２…凝集汚泥調製槽、２３…凝集汚泥分離濃縮装置、２４…再濃縮凝集汚泥調製槽、２５…脱水ケーキ調製装置。 DESCRIPTION OF SYMBOLS 1 ... Organic sludge, 2 ... Diluted water, 3 ... Diluted sludge, 4 ... Flocculant, 5 ... Flocculated sludge, 6 ... Separation water, 7 ... Concentrated sludge, 8 ... Flocculant, 9 ... Re-concentrated flocculent sludge, 10 DESCRIPTION OF SYMBOLS: Separation water, 11 ... Dehydrated cake, 21 ... Dilution apparatus, 22 ... Aggregated sludge preparation tank, 23 ... Aggregated sludge separation and concentration apparatus, 24 ... Re-concentration aggregation sludge preparation tank, 25 ... Dehydrated cake preparation apparatus.
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| JP2013144298A (en) * | 2013-05-01 | 2013-07-25 | Swing Corp | Method and device for treating organic sludge |
| JP2017136514A (en) * | 2016-02-01 | 2017-08-10 | 水ｉｎｇ株式会社 | Polymer coagulant and dewatering method and dewatering device of sludge using polymer coagulant |
| KR102643959B1 (en) * | 2023-09-01 | 2024-03-08 | 디와이산업개발 주식회사 | Method for dehydrating organic sludge |
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| JP2017136514A (en) * | 2016-02-01 | 2017-08-10 | 水ｉｎｇ株式会社 | Polymer coagulant and dewatering method and dewatering device of sludge using polymer coagulant |
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