JP4465166B2

JP4465166B2 - Jellyfish processing apparatus and jellyfish processing method

Info

Publication number: JP4465166B2
Application number: JP2003204090A
Authority: JP
Inventors: 豊喜川端; 洋祐岡; 敏治柳川; 毅長沼; 泰之小串; 竹内　　善幸; 進河野
Original assignee: Chugoku Electric Power Co Inc; Mitsubishi Heavy Industries Ltd
Current assignee: Chugoku Electric Power Co Inc; Mitsubishi Heavy Industries Ltd
Priority date: 2002-07-30
Filing date: 2003-07-30
Publication date: 2010-05-19
Anticipated expiration: 2023-07-30
Also published as: JP2004122118A

Description

【０００１】
【発明の属する技術分野】
本発明は、海域に大量発生したクラゲを、発生場所において又は陸上げされた状態で分解処理して、無公害な処理液として排出する処理装置および処理方法に関する。
【０００２】
【従来の技術】
夏季になると日本近海には大量のクラゲが発生する。最近では、海域の温暖化等により冬季でも多量のクラゲの生存が確認されている。臨海地域に立地し、冷却水として大量の海水を必要とする発電所等のプラント施設においては、発生したクラゲが潮流にのって押し寄せ、冷却水の取水口から取り込まれると、フィルタの目詰まり等多くの弊害をもたらす。そのため、発電所等では回転式除塵機等を使用してクラゲを捕獲・回収している。このように陸揚げされたクラゲは、そのまま陸地に埋め立て処分されるか、自然乾燥されるか、あるいは、機械的、化学的又は生物学的に処理されている。
【０００３】
陸揚げされたクラゲ処理には、以下のような問題点がある:
(１)死んだクラゲは魚が腐ったような臭気を発生して悪臭源となる。
(２)クラゲはその体に占める水分が９５〜９８%であるため焼却処理が可能であるとしてもエネルギー消費量が高く、しかもゼリー状で流動性に乏しいため、そのままでは通常の排水処理工程での処理も困難である。
(３)埋め立て処分する場合にも用地の確保が難しい。
【０００４】
かかる間題を解決すべく、陸揚げされたクラゲを嫌気性条件下で、嫌気性細菌により生物学的及び機械的に処理し、その後排水処理する簡易な処理方法・装置について記載されている（例えば、特許文献１参照）。また、陸揚げされたクラゲを加圧下で加熱し、その後瞬時に脱圧により膨化処理してクラゲ水を得、このクラゲ水に次亜塩素酸ナトリウムを添加して、排水処理する方法について、記載している（例えば、特許文献２参照）。しかしながら、特許文献１に記載の発明においては、そのクラゲ分解処理が嫌気性菌の自然発生又は下水処理後の活性汚泥に含まれる嫌気性細菌の添加によるので、嫌気性環境を作り出さなければならず、また、その分解処理には、３日間と長期間を要するので、迅速かつ効率のよい処理とは言い難い。特許文献２に記載の発明においては、加熱蒸気の供給設備、加圧槽、次亜塩素酸ナトリウム添加設備等の装置が必要であり、それらの装置群の建設・維持費のコストが高い。
【０００５】
【特許文献１】
特開平１１-１７９３２７号公報
【０００６】
【特許文献２】
特開平１１-２４４８３３号公報
【０００７】
【発明が解決しようとする課題】
したがって、本発明は、陸揚げクラゲの処理に関する上記の諸問題を解決すべく、また、上記従来技術のクラゲ処理方法・装置の不具合を解消すべく、迅速、かつ、効率のよいクラゲの生物学的処理方法を提供することを目的とする。
【０００８】
【課題を解決するための手段】
上記目的を達成するために、本発明は、クラゲと分解酵素とを混合するための酵素混合槽と、酵素混合槽で処理されたクラゲとクラゲからの溶出水の混合物中に含まれるＣＯＤを分解および/または除去するためのＣＯＤ分解塔と、酵素混合槽およびＣＯＤ分解塔において発生する気体の脱臭処理を行って排気するための脱臭塔とを備えてなるクラゲ処理装置を提供する、また、クラゲと分解酵素とを混合して、クラゲの体に含まれる水を溶出させるステップと、クラゲとクラゲの溶出水の混合物中に含まれるＣＯＤを分解および/または除去するステップと、酵素混合槽およびＣＯＤ分解塔において発生する気体を脱臭処理するステップとを含むクラゲ処理方法を提供する。
【０００９】
このクラゲ処理装置及び処理方法によれば、クラゲの処理において、ＣＯＤの排水処理基準を満たした排水を、最終産物として排出することができ、かつ、クラゲの処理中に発生する異臭を除去することができる。
【００１０】
ＣＯＤ分解塔は、紫外線処理装置、活性炭処理装置およびオゾン酸化処理装置からなる群から選択される一の処理装置、またはそれらの二以上の処理装置の組み合わせからからなってもよい。すなわち、紫外線処理装置、活性炭処理装置、またはオゾン酸化処理装置のうちのいずれか単独でＣＯＤ分解塔を構成してもよいし、紫外線処理装置、活性炭処理装置、またはオゾン酸化処理装置のうち、２以上を組み合わせてＣＯＤ分解塔を構成してもよい。これらのうち、特に好ましいのは、紫外線処理装置であり、もっとも好ましいのは、紫外線処理装置と活性炭処理装置の組み合わせである。たとえば、紫外線処理装置の後段に活性炭処理装置を設けてＣＯＤ分解塔を構成する。
【００１１】
また別の実施態様では、上記の実施態様に加えて、ＣＯＤ分解塔に供給される処理液から、非水溶性物質を分離するための膜分離装置を、酵素混合槽とＣＯＤ分解塔との間にさらに設ける。このクラゲ処理装置によれば、クラゲを酵素で処理した処理液を膜分離装置によりろ過することによって、酵素により分解できないクラゲの破片や夾雑物等の非水溶性物を取り除いて、ろ過されたろ液をＣＯＤ分解塔に流入できる。この膜分離装置による処理によって、ＣＯＤ分解塔に流入される処理水のＣＯＤ値を下げることができ、結果としてＣＯＤ分解時間の低減を図ることができる。この態様においては、膜分離装置により分離した非水溶性物質を、加熱分解または焼却処理するための処理槽をさらに備えるのが好ましい。
【００１２】
【発明の実施の形態】
以下、本発明を図面に基づき詳しく説明する。
図１は、本発明のクラゲ処理装置の一実施例を説明するための概略図である。図中１は、クラゲ処理装置であり、この処理装置は、クラゲ１３と分解酵素とを混合して酵素分解するための酵素混合槽２と、酵素混合槽２で処理されたクラゲを含む液体中のＣＯＤを分解するためのＣＯＤ分解塔３と、酵素混合槽２およびＣＯＤ分解塔３において発生する気体の脱臭処理を行って排気する脱臭塔４とを備えてなる。
【００１３】
酵素混合槽２では、クラゲとクラゲ分解酵素とを攪拌、混合して、酵素反応によりクラゲを分解する。クラゲ分解酵素としては、コラゲナーゼを例示できる。クラゲは、その体を構成するタンパク質(コラーゲン)が繊維状構造をとり、その網目に水を閉じ込めてゼリー状となっている。この網目構造を構成するコラーゲン繊維をコラゲナーゼによって切断し、クラゲ体内に閉じ込められた水を溶出させて(解放して)、またコラーゲン自身も溶解してクラゲの体から除かれ、クラゲが減容化される。クラゲの減容化に伴って、クラゲと溶出水の混合物は流動化する。本明細書中、クラゲの減容化とは、クラゲ分解酵素、特にコラゲナーゼを適用することにより、上記クラゲの体を構成するコラーゲン繊維を破壊して上記体に含有される水を除去し、またコラーゲン自身も溶解してクラゲの体から除かれ、これをもってクラゲの体積を減少させることをいう。
【００１４】
コラゲナーゼは、特に限定されず、任意の生物由来のコラゲナーゼを用いてもよいが、例として、通性嫌気性のビブリオ属(Vibrio sp.)に属する細菌由来および/またはバチルス属(Bacillus sp.)に属する細菌由来のものを使用することができる。バチルス属の細菌の具体的な例は、２００１年４月２５日に独立行政法人産業技術総合研究所に寄託された海洋細菌バチルス属(Bacillus sp.)(J２６Ｗ株)(受託番号FERM P-18313)である。クラゲ分解酵素の代わりに、クラゲ分解酵素分泌細菌、たとえば上述のビブリオ属(Vibrio sp.)に属する細菌および/またはバチルス属(Bacillus sp.)に属する細菌を直接酵素混合槽２に投入して、そこでクラゲ分解酵素を分泌させてクラゲの体を分解してもよい。
【００１５】
処理されるクラゲは、クラゲが発生した海域またはプラントの取水口付近など、クラゲを除去すべき海域または海水から、捕集機５などによりクラゲを捕集し、吸引ダスト６で陸上に引き上げた後、固液分離器７によりクラゲともに回収された海水とクラゲとを分離する。分離された海水は再び海中に戻される。
【００１６】
固液分離されたクラゲは、酵素混合槽２に投入され、酵素処理される。酵素混合槽に投入される前に、酵素処理時間の短縮を図るため、クラゲの体を予め破砕して酵素混合槽２に投入するための破砕機を酵素混合槽２の前段に設けてもよい。破砕は、固液分離と同時に固液分離装置内で行ってもよく、固液分離の前段または後段に別途破砕機を設けてもよい。
【００１７】
次に、酵素混合槽２における酵素処理時間、攪拌速度、処理温度について説明するが、これらの条件は、クラゲの量および酵素の量などに応じて適宜変更可能であり、特に限定されない。たとえば、酵素混合槽２における酵素処理時間は、生きたクラゲを用いた場合、約２０〜３０時間程度であるが、破砕したクラゲを用いると、３時間で９０％以上分解される。この程度の処理時間をかけてクラゲを酵素処理することにより、クラゲの体内のコラーゲンは分解され、体内の水分は溶出して、流動化する。酵素混合槽２における攪拌速度は、槽内のクラゲの量により変更可能であり、約１０〜６０rpmで攪拌するのが好ましいが、特に限定されない。また、攪拌によりクラゲと酵素が充分混合された後は静置しても良い。処理温度は、酵素が働く温度、すなわち、１５〜４５℃が好ましいが、通常は、加熱および冷却を特に行なわず、外気温で処理を行うことができる。ここでクラゲ分解物が腐敗する際に生じる悪臭の発生の抑制のために、珪素系の腐臭抑制処理剤を混合してもよい。
【００１８】
酵素処理により減容化されたクラゲは、ＣＯＤ分解塔３に投入される。コラゲナーゼ処理を行っただけでは、ＣＯＤが発電所などに適用される一般的な排水基準濃度(以下、排水基準という)である１５ｍｇ/Ｌを上回るため、流動化したクラゲと溶出水の混合物を元の海域に廃棄することができない。したがって、クラゲと溶出水の混合物をＣＯＤ分解塔３においてＣＯＤ分解処理を行い、排水規制を満足する処理水として排出することができる。
【００１９】
好ましくは、ＣＯＤ分解塔に供給されるクラゲと溶出水の混合物から、非水溶性物質を分離するための膜分離装置８を、酵素混合槽２とＣＯＤ分解塔３との間にさらに設ける。流動化したクラゲと溶出水の混合物を膜分離装置８によりろ過することによって、酵素により分解できないクラゲの破片や來雑物等の非水溶性物を除去して、ろ過されたろ液をＣＯＤ分解塔に流入できる。この膜分離装置８による処理によって、ＣＯＤ分解塔３に流入されるクラゲと溶出水の混合物のＣＯＤを膜処理前よりも下げることができ、結果としてＣＯＤ分解時間の低減を図ることができる。また、この膜分離装置８は、酵素混合槽２の一部として設けてもよい。この膜分離装置８としては、限外ろ過膜やマイクロフィルター等が使用され、約１０μm以下の物質を非水溶性物質と分離できるものが好ましい。
【００２０】
膜分離装置８により分離された非水溶性物質は、酵素混合槽２に戻してさらにコラゲナーゼ処理に供してもよいが、長期間処理を続けると、膜分離装置８の目詰まりを起こしやすいため、膜分離装置８に付着した非水溶性物質を加熱分解または焼却処理してもよい。すなわち、膜分離装置８から酵素混合槽に分離された非水溶性物資を戻すためのラィンを設けてもよく、酵素混合槽２と別に加熱または焼却処理用の処理槽(図示せず)を設けてもよい。
【００２１】
ＣＯＤ分解塔３では、具体的には、以下の処理のいずれか一またはそれらの二つ以上の処理を組み合わせた処理が行われる。
【００２２】
(１)活性炭吸着法
処理水中の有機物を活性炭により吸着して分離する。吸着後の活性炭の再生処理が必要である。
【００２３】
(２)オゾン酸化法
オゾンは、水に溶解して分解するときに生成するＯＨラジカルによる強い酸化力を示す。その結果、水中の物質の二重結合のような不飽和結合部の切断、芳香族化合物の酸化、硫化物やアミン類の酸化に有効である。また、後段に活性炭吸着処理装置を設けることにより、オゾン難分解性成分の吸着や残留オゾンの除去に効果がある。
【００２４】
(３)紫外線照射法
水中の有機物の光吸収性を利用して有機物を分解する。オゾンは、紫外線の光を吸収し、酸素原子と酸素分子に解離する。この解離した酸素原子が水と反応してＯＨラジカルを生成し、酸化反応が加速される。従って、紫外線照射法とオゾン酸化法との組み合わせにより、有機物の分解効果が大きくなる。
【００２５】
(４)膜処理法
限外ろ過膜やマイクロフィルター膜により、数μm以上のＣＯＤ成分が分離される。処理時間の経過に伴って分離性能が低下するため、膜の再生または交換が必要になる。新品の膜と交換するたびに廃棄物が生じるが、紫外線照射法およびオゾン酸化法に比べて、装置費が安価であるという利点がある。膜処理法単独では、ＣＯＤ濃度の排水基準値を満足しない場合には、活性炭吸着法との併用が望ましい。
【００２６】
(５)凝集剤+電解浮上法
凝集剤を添加して、クラゲと溶出水の混合物中の微細粒子、コロイド上物質を凝集させた後、浮上槽内に設置した電極問に直流電流をかけて、電気分解により水素と酸素の気泡を生じさせる。この気泡により、凝集した有機物を浮上させ固液分離により除去し、ＣＯＤの低減を図る。電解浮上の換わりに加圧浮上法により凝集物を浮上させてもよい。
【００２７】
上記の方法のうち、紫外線照射法を用いるのが好ましく、処理時間、処理効率の点から、紫外線照射によりある程度ＣＯＤを分解した後、活性炭吸着法により紫外線照射後も残存するＣＯＤを除去するのが好ましい。図１の例においては、ＣＯＤ分解塔３は、紫外線照射塔９とその後段に活性炭充填塔１０を備え、循環式に紫外線照射を行えるように供給槽１１を設け、酵素混合槽２で処理されたクラゲと溶出水の混合物をいったん供給槽１１に導入し、そこから紫外線照射塔９に供給し、紫外線照射塔９から流出した処理水を再び供給層１１に戻す。このように、供給槽１１と紫外線照射塔９との間をＣＯＤが充分減少するまで循環させ、ＣＯＤが充分減少した処理水を活性炭充填塔１０に導入する。紫外線照射と活性炭処理により、ＣＯＤが排水基準濃度(１５ｍｇ/Ｌ)以下となった処理水は、清浄排水として排水できる。図１では、ＣＯＤ分解塔に供給槽１１を設け、循環式にしたが、バッチ式に行ってもよい。
【００２８】
ＣＯＤ分解に紫外線照射を用いる場合には、Ｈ_２Ｏ_２(過酸化水素)を紫外線照射時に添加して行うのがよく、Ｈ_２Ｏ_２の添加は、照射中に複数回又は連続的に行うのが、ＣＯＤ分解効率の点で望ましい。図１の例のように、供給槽１１を設ける場合には、供給槽１１にＨ_２Ｏ_２を添加することができる。照射時間はＣＯＤの濃度により異なるが、１００ｍｇ／Ｌの場合、４Ｗの紫外線ランプを用いて、６〜１２時間程度照射することによってＣＯＤ排水基準濃度である１５ｍｇ/Ｌ以下とすることができる。また、処理時間、処理効率、設備の小型化のために、紫外線照射処理によってＣＯＤ濃度を約２５ｍｇ/Ｌ程度とし、紫外線処理後に他のＣＯＤ分解処理、たとえば活性炭吸着を行ってもよい。
【００２９】
ＣＯＤ分解に活性炭吸着法を用いる場合には、クラゲと溶出水の混合物を活性炭充填カラムに通すことができる。この方法では、ＳＶ=１〜０.５h^−１程度で処理を行うことによりＣＯＤを吸着除去できる。また、他の方法としては、クラゲと溶出水の混合物中に活性炭を投入して攪拌する方法が挙げられる。攪拌後、ろ過等の処理により活性炭を除去して、ＣＯＤが低減した処理水を得ることができる。
【００３０】
ＣＯＤ分解にオゾン酸化法を用いる場合には、オゾンガス流量を約１〜５Ｌ/０.１g−ＣＯＤ/分で、３〜８時間処理することによりＣＯＤを減少できる。オゾン酸化により、トリハロメタンを副生する可能性があるので、オゾン酸化の後に活性炭吸着法を行うことが好ましい。
【００３１】
ＣＯＤ分解に限外ろ過膜法を用いる場合には、分画分子量３０００以下のものを使用するのが好ましい。中空糸型限外ろ過膜を使用する場合、ＣＯＤ成分が中空糸膜に付着除去されているので、処理性能が低下すると再生または交換する必要がある。新品の膜との交換により廃棄物が生じるが、紫外線照射法やオゾン酸化法に比べ装置費が安価である。この限外ろ過膜法単独でＣＯＤ濃度の排水基準値を満たさない場合には、活性炭吸着法と併用して、排水基準値以下までＣＯＤを分解、除去する方法がある。また、分画分子量の異なるものを複数個設けて処理を行ってもよい。
【００３２】
ＣＯＤ分解に凝集剤添加法および電解浮上法を用いる場合には、無機凝集剤としてアルミニウム系(ポリ塩化アルミニウム、硫酸アルミニウム、塩基性塩化アルミニウム等)、鉄塩系(硫酸鉄、塩化鉄等)を用いることができ、高分子凝集剤として陰イオン性ポリマー(アルギン酸ナトリウム、ポリアクリルアミド部分加水分解塩等)、陽イオン性ポリマー(水溶性アニリン樹脂、ポリチオ尿素、ポリエチレンイミン、ポリビニルピリジン類等)、非イオン性ポリマー(ポリアクリルアミド、ポリオキシエチレン等)等を用いることができる。無機凝集剤と高分子凝集剤を併用するのが望ましいが、無機凝集剤単独または高分子凝集剤単独でも可能である。しかし、無機凝集剤単独使用では、生成した凝集物が細かく、沈降性が悪いため清澄な上澄みが得にくい場合があるため、このような場合には高分子凝集剤を添加して凝集物を粗大化し、沈降性をあげるのが好ましい。凝集剤添加後、電解浮上により凝集物を浮上させ、液分離により除去する。この方法では、浮上物をスクラバーでかき寄せ回収するため、一般に沈降法に比べて水分の低い汚泥となる点が有利である。
【００３３】
本発明のクラゲ分解装置では、酵素混合槽およびＣＯＤ分解槽からクラゲ分解物が腐敗することにより生じるアンモニア、硫黄化合物、トリメチルアミン等の悪臭物質の除去のために、酵素分解槽およびＣＯＤ分解塔から生じた気体を捕集し、脱臭処理を行う脱臭塔４を設けることができる。脱臭塔４には、活性炭を充填し、酵素混合槽およびＣＯＤ分解塔から生じた気体を捕集して、脱臭塔４に導入するためのラインと、脱臭処理後の気体を放出するためのブロワ１２の付いたラインが備えられている。悪臭物質を含む気体を脱臭塔の活性炭により吸着処理した後、大気中に放出できる。
【００３４】
以上のクラゲ処理装置を用いたクラゲ処理工程の一例を述べる。
クラゲの捕集機５により海中のクラゲを捕集し、吸引ダクト６を経て、ポンプを通過させた後、固液分離器７によりクラゲと海水とを分離する。その後、分離したクラゲを酵素混合槽２の中に投入し、分解酵素を当該酵素混合槽2内に供給してこれらを攪拌・混合する。混合物はスラリー状態で循環ポンプにより抜き出され、膜分離装置8により分解液と未分解物とを分離する。分離された未分解物のスラリーは、循環ラインにより酵素混合槽２に戻される。一方、膜分離装置８を透過した分解液は、供給槽１１に供給される。供給槽１１に供給された分解液は、循環ポンプにより抜き出され、紫外線照射塔９を経て供給槽１１の間を循環して、分解液中のＣＯＤを分解処理する。所定時間循環してＣＯＤ成分を分解した後、処理液は活性炭充填塔１０にて未分解のＣＯＤ成分が吸着・分離された後、清浄排水となって排出される。発生した分解ガスは、ブロワ１２により吸引され、脱臭塔４を経て排気される。
【００３５】
本発明のクラゲ処理装置では、大型の装置を必要としないために、陸地に静置することには限定されることなく、移動可能な船舶および自動車のような可搬式設備に搭載することができる。クラゲ処理装置は、クラゲが出現したときのみ、クラゲ処理装置を稼動させればよく、常に臨海地域のプラントに必要となるわけではない。そのため、本発明のクラゲ分解装置を可搬式設備に搭載すれば、クラゲ分解装置をクラゲが出現した場所に移動させて、そこでクラゲ処理を行い、処理が終わってクラゲ処理装置が不要となれば、クラゲ処理が必要なほかの場所に移動させることができる。
【００３６】
【実施例】
以下に実施例をあげて、本発明をさらに詳細に説明するが、これらにより本発明を制限することを意図するものではない。
【００３７】
［実施例１］
(１)紫外線照射法によるＣＯＤ処理試験
紫外線照射法によるＣＯＤの分解を試験した。供試液には、５４gのクラゲをクラゲ分解酵素により分解して得られたもので、初期ＣＯＤは、１３５ｍｇ/Ｌのものを用いた。ＵＶランプには、出力４Ｗ、ランプ長２４０mm、主波長２５４nmの低圧紫外線ランプを用いた。ＵＶランプを包むカラムの形状は、塩ビ円筒容器(内径３４mm、高さ２８５mm)中に石英管(外径２８mm)を通し、中央に紫外線ランプを配置し、その外側に供試液を流す二重管構造とした。このカラムにタンクからマグネットポンプで供試液を送り、カラムを通した後、タンクに戻す循環式により供試液を循環させた。循環流量は１.６Ｌ/分とし、温度は、３８℃で行った。サンプリングは２時間毎に１００mＬをタンクから採取して行った。結果を図２に示す。１０時間後残留ＣＯＤは、１１ｍｇ/Ｌとなり、水質基準濃度である１５ｍｇ/Ｌ以下になることを確認した。
【００３８】
また、Ｈ_２Ｏ_２無添加で紫外線処理した結果を図３に示す。本結果から、Ｈ_２Ｏ_２添加の効果の大きいことが確認できる。
【００３９】
(２)活性炭吸着法によるＣＯＤ処理試験
活性炭吸着法によるＣＯＤの除去を試験した。供試液には、初期ＣＯＤ約８０ｍｇ/Ｌ相当のものを用いた。試験は２５℃の室温で行い、５０gの活性炭(BOMBA 100CG8-32C 多木化学、一般的な水質処理用活性炭、石炭系) を添加直後、４時間後、８時間後、２４時間後にサンプリングして、ＣＯＤ濃度を測定した。活性炭へのＣＯＤ平衡吸着量測定時の残留ＣＯＤ濃度の経時変化を図４に表す。２４時間後の残留ＣＯＤ濃度は、ほぼ平衡に達しており、本点をもって平衡吸着速度とした。
【００４０】
(３)活性炭へのＣＯＤ吸着カラム試験
活性炭を充填したカラムによるＣＯＤの除去を試験した。供試液には、初期ＣＯＤ約８０ｍｇ/Ｌ相当のものを用いた。ＳＶ=１及び０.５について試験を行った。ここでＳＶ=(液流速/活性炭量)を示す。カラムから流出した試料についてＣＯＤ濃度の経時変化を図５に示す。図５から明らかなように、クラゲと溶出液の混合物中に含まれるＣＯＤは、活性炭への吸着が遅いため、活性炭吸着塔は、ＳＶ=０.５ｈ-１程度の低いＳＶ値が好ましく、紫外線照射またはオゾン酸化等の処理の後段の処理として活性炭処理を行うのが好ましいことがわかった。
【００４１】
(４)オゾン酸化法によるＣＯＤ処理試験
オゾン酸化法によるＣＯＤの除去を試験した。供試液には、初期ＣＯＤ約８０ｍｇ/Ｌ相当のものを用いた。オゾン発生装置として、株式会社増田研究所のAOC-30Wを使用し、オゾンガス流量３Ｌ/分として２１〜２３℃の室温で行った。オゾン酸化法によるＣＯＤ濃度の経時変化を図６に示す。
【００４２】
オゾン処理により、ＣＯＤ成分は低減することが確認された。しかしながら、オゾンは強い酸化作用があり、クラゲ中に含まれる有機物、塩素、臭素からトリハロメタンが処理反応時に生成する可能性がある。トリハロメタンは、ハロゲン系有機化合物であり、クロロホルム(CHCl₃)、ブロモジクロロメタン(CHBrCl₂)、ジブロモクロロメタン(CHBr_２Cl)、ブロモホルム(CHBr₃)の総称である。これらには、発がん性を有する可能性があるものもあり、日本では、トリハロメタンについて水道水の水質基準が定められているが、排水基準は定められていない。ＣＯＤをオゾンによる処理とその後の活性炭処理により行うことを想定し、JIS K０１２５:１９９５「用水・排水中の揮発性有機化合物試験方法」に準拠し、処理前後のトリハロメタンの濃度を測定した。結果を下記の表１に示す。
【００４３】
【表１】

【００４４】
表から明らかなように、オゾン処理後に活性炭吸着処理することによって、トリハロメタンは除去可能であることがわかった。
【００４５】
(５)限外ろ過膜法によるＣＯＤ処理試験
限外ろ過膜法によるＣＯＤの除去を試験した。クラゲ分解液中のＣＯＤ成分となる微細粒子、コロイド状物質を半透膜によって分離し、ＣＯＤを低減処理した。装置には、ＣＯＤによる膜面の堆積物形成を抑制しやすく、またモジュールあたりの膜面積を広く取りやすい中空糸膜を用いたクロスフローろ過方式を用いた。供試液には、８５０mＬの初期ＣＯＤ約８０ｍｇ/Ｌ相当のものを用い、限外ろ過膜として、ＳＥＰ-００１３(旭化成製、膜内径２mm、有効膜面積８０cm^２、公称孔径０.２５μm、分画分子量３０００、モジュール外径２０mm×１３０mm(ペンシル型))を用いた。通水は、チューブポンプで中空糸内側に流して、循環ろ過する方式を採用し、２１〜２３℃の室温で行った。ろ過速度は１.１〜１.３mＬ/分とした。１０時間循環させた後、処理液を測定した。結果を下記の表２に示す。
【００４６】
【表２】

【００４７】
１０時間の膜処理により、ＣＯＤ濃度８０ｍｇ/Ｌの原水は、１３ｍｇ/ＬまでＣＯＤが除去されて、水質基準濃度である１５ｍｇ/Ｌ以下の透明なろ過水が得られた。膜処理法では、ＣＯＤ成分が中空糸膜に付着して除去されているので、処理性能が低下したときには再生または新品と取り替えて使用する必要がある。また、処理後のＣＯＤ濃度が排水基準値に満たない場合には、活性炭吸着法など他法との併用により基準値を満たす処理水を得ることができる。
【００４８】
(６)凝集剤+電解浮上法によるＣＯＤ処理試験
凝集剤を添加した後、電解浮上を行ってＣＯＤの除去を試験した。供試液には、初期ＣＯＤ約９２ｍｇ/Ｌ相当のものを用いた。この供試液を５００ｍＬビーカーに入れ、無機凝集剤PAC(多木化学)を５００ｍｇ/Ｌまたは１０００ｍｇ/Ｌ添加し、スターラーで攪拌しながらpH試験紙でｐＨ８に中和した。続いて攪拌を緩めて、高分子凝集剤A-133(多木化学)を２ｍｇ/Ｌ添加し、静置して懸濁物を沈降させて、上清を採集し、ＣＯＤ濃度を測定した。また、無機凝集剤のみを５００ｍｇ/Ｌ添加して、同様にＣＯＤ濃度を測定した。結果を表３に示す。
【００４９】
【表３】

【００５０】
無機凝集剤１０００ｍｇ/Ｌ、高分子凝集剤２ｍｇ/Ｌを添加することにより、原水中のＣＯＤ濃度９２ｍｇ/Ｌが５７ｍｇ/Ｌまで低減した。また、また、処理後のＣＯＤ濃度が排水基準値に満たない場合には、活性炭吸着法など他法との併用により基準値を満たす処理水を得ることができる。
【００５１】
さらに、上記の結果のうち、凝集状況がよく、薬剤添加量が少ない、無機凝集剤５００ｍｇ/Ｌ、高分子凝集剤２ｍｇ/Ｌの組み合わせを採用して、２Ｌの容器に凝集処理した供試液をいれ、電極を設置した。電極は、６５×３０×２ｍｍの電極を３枚並べて、中央を陽極とした。電極面積は３９ｃｍ^２(中央の電極の表裏面の合計)、電流密度２.６Ａ／ｄｃｍ^２(気泡発生時の電流値１Ａ電流抑制、電圧３Ａ)として、電流を流した。
【００５２】
処理前後のＣＯＤ濃度を表４に示す。１時間後には、ＣＯＤ濃度が６１ｍｇ/Ｌとなったが、その後４時間後でもほとんどＣＯＤは減少しなかったため、短時間での処理で充分であると考えられる。
【００５３】
【表４】

【００５４】
［実施例２］
図１で示すクラゲ処理装置におけるクラゲ分解装置、紫外線照射塔、及び活性炭充填塔について、ベンチスケールでのクラゲ分解実験を行った。その実験内容及び結果を以下に述べる。
【００５５】
＜クラゲ分解装置＞
クラゲ分解装置は図７に示したような形状で、アクリル製であり、有効処理容積は５０Ｌである。
図７のクラゲ分解装置に、海水で５倍希釈した粗酵素液１５ｋｇを入れ、切断したクラゲ２０ｋｇを投入し、６０ｒｐｍで攪拌しながら室温で反応させ、時間経過後の残存固形分を調べたところ、図８に示すように、５時間以内に残存固形分が１０％以下となった。
【００５６】
＜ＣＯＤ低減装置＞
上記クラゲ分解装置をもちいて処理した後のクラゲ分解物に対し、JIS K010217の過マンガン酸カリウム法でＣＯＤを測定したところ、約５００ｍｇ／Ｌであった。このＣＯＤを低減化するため、紫外線処理装置及び活性炭処理装置を作製し、ＣＯＤ低減効果を調べた。
【００５７】
図９に紫外線酸化試験装置の概略図を示す。紫外線照射装置１００は、SUS316L製の円筒容器（内径４０ｍｍ）１０１の中に、石英管（外径３０ｍｍ）１０２を通し、中心に紫外線ランプ（出力８５Ｗ）を設置したもので、円筒容器１０１と石英管１０２の間に、アクリル製タンク（５０Ｌ容量；底面の直径３５０ｍｍ、高さ５５０ｍｍの円筒形）１０３からポンプ１０４で循環供給されるクラゲ分解液を通した。タンク１０３にクラゲ分解液３５ｋｇを投入し、開始時にＨ_２Ｏ_２を１７５ｇ（５０００ｍｇ／Ｌ相当）添加し、７．５時間後より連続的に５．８３ｇ／ｈ（１６７ｍｇ／Ｌ／ｈ相当）を添加する条件で紫外線照射を行い、経時的にＣＯＤ濃度（図１０Ａ）、及びＨ_２Ｏ_２濃度（図１０Ｂ）を測定した。この結果、紫外線照射のみで、ＣＯＤ濃度を規制値１５ｍｇ／Ｌ以下に減少させられることが確認できた。
【００５８】
一方、活性炭は比表面積が５００〜１５００ｍ^２／ｇと大きいため、微量の溶存有機物を吸着できる。そこで、確実にＣＯＤ濃度を低減させるため、図１に示した様に、紫外線照射塔９の後段に活性炭充填塔１０を設置した。活性炭充填塔１１０の概略図を図１１に示す。活性炭充填塔１１０は、塩ビ製の円筒１１１（底面の直径１２０ｍｍ、高さ４００ｍｍ）であり、３Ｌの活性炭を充填した。紫外線照射処理されたクラゲ分解液（ＣＯＤは約２５ｍｇ／Ｌ）を、ポンプ１１２で下方より連続供給した。活性炭充填塔１１０の上部に設けられた液出口において、経時的にＣＯＤ濃度、及びＨ_２Ｏ_２濃度を測定した（図１２）。結果として、少なくとも２１０時間にわたって、安定してＣＯＤ及びＨ_２Ｏ_２の濃度低減処理ができることが明らかになった。
【００５９】
＜脱臭テスト＞
以上のようなクラゲ処理の際に生じる臭気を、臭覚測定法によって、各処理段階で測定した。臭覚測定法は、人間の臭覚を利用して、臭いの強さを定量化しようとするものである。その場合、臭気全体で臭いの強さを評価するのであって、機器分析法のように、臭いの各原因物質ごとに濃度を測定する方法とは異なる。
【００６０】
図１３に示す各槽に、テフロンチューブでフレックスポンプ（ジールサイエンス社）をつなぎ、槽内の気体を試料採取用バッグ（テドラーバッグ、アズワン社）に採取した。
【００６１】
臭気の官能試験は、以下のように行った。まず、無臭の空気の入った袋と対象とする気体を希釈した気体の入った袋を準備した。３人のパネラー（臭いを判定する判定者）にその２つの袋を与え、違いが感じられるかどうか判定するというやり方で、希釈倍率を徐々に上げてゆき、パネラー全員が２つの袋の違いが感じられなくなった時点の希釈倍率を求めた。結果を表５に示す。
【００６２】
【表５】

【００６３】
この結果より、各処理段階での臭気濃度及び臭気指数を求めた。
まず、以下のようにして、各パネラーの閾値を常用対数として求めた。例えば、パネラーｉの場合、次式でパネラーの閾値Ｘｉを求める。
【００６４】
Ｘｉ＝（ｌｏｇＭ_１ｉ＋ｌｏｇＭ_０ｉ）／２
式中、Ｍ１ｉ：パネラーの回答が正解である最大である希釈倍率
Ｍ０ｉ：パネラーの回答が不正解である希釈倍率
求めた各パネラーの閾値の平均値Ｘより、次式で臭気濃度Ｙを求めた。
Ｙ＝１０^Ｘ
パネラーの閾値の平均値Ｘを１０倍した値Ｚを臭気指数とする。
Ｚ＝１０Ｘ（＝１０ｌｏｇＹ）
このようにして得られた、各処理段階での臭気濃度Ｙ及び臭気指数を表６に示す。
【００６５】
【表６】

【００６６】
悪臭は、感覚的で、長期に渡って大気や土壌を汚染しない公害であるとの見解から、全国一律の規制値は設けられていないが、総理府令定める範囲内で、都道府県知事及び指定都市、中核市、特例市の庁が規定地域及び規定基準を決めることとなっている。各地での敷地境界線における規制基準（１号規制）は臭気指数１０〜２１となっており、本発明にかかるクラゲ処理装置の各槽から漏れる気体における臭気指数１２〜２２は、ほぼ規制基準に適合している。
【００６７】
【発明の効果】
上記したところから明らかなように、本発明によれば、クラゲの処理において、ＣＯＤの排水処理基準を満たした排水を、最終産物として排出することができ、かつ、クラゲの処理中に発生する異臭を除去することができる。本発明によれば、水質汚濁防止法に基づく排水基準１６０ｍｇ/Ｌ(日間平均１２０ｍｇ/Ｌ)よりも厳しい、１０〜２０ｍｇ/Ｌ以下にすることも可能である。したがって、環境に影響を与えることなく、クラゲを処理することができる。また、酵素処理後に膜分離処理を行うことによって、ＣＯＤ分解塔に流入される処理水のＣＯＤ値を下げることができ、結果としてＣＯＤ分解時間の低減を図ることができる。さらに、本発明のクラゲ処理装置を可搬式設備に搭載すれば、クラゲ出現場所にクラゲ処理装置を移動させて処理すればよく、プラントにおいてクラゲ処理装置の設置面積を取らずにすむ点でも好ましい。
【図面の簡単な説明】
【図１】本発明のクラゲ処理装置の模式図を表す。
【図２】実施例１における、初期ＣＯＤが１３５ｍｇ/Ｌの供試液を紫外線照射法により処理したＣＯＤ処理試験の結果を表す。
【図３】実施例１におけるＨ_２Ｏ_２無添加の場合の紫外線照射法によるＣＯＤ処理試験の結果を表す。
【図４】実施例１における活性炭へのＣＯＤ平衡吸着測定時の残留ＣＯＤ濃度の経時変化を示す。
【図５】実施例１におけるＣＯＤ吸着カラム試験結果を表す。
【図６】実施例１におけるオゾン酸化処理時のＣＯＤ濃度の経時的変化を表す。
【図７】実施例２におけるクラゲ分解装置の概略図である。
【図８】実施例２におけるクラゲ分解時の、残存固形分の経時変化を示す図である。
【図９】実施例２における紫外線参加試験装置の概略図である。
【図１０】実施例２における紫外線照射時のＣＯＤ濃度（Ａ）及びＨ_２Ｏ_２濃度（Ｂ）の経時変化を示す図である。
【図１１】実施例２における活性炭充填塔の概略図である。
【図１２】実施例２における活性炭処理の際のＣＯＤ濃度及びＨ_２Ｏ_２濃度の経時変化を示す図である。
【図１３】実施例２における臭気を測定した場所を示す図である。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a processing apparatus and a processing method for decomposing jellyfish generated in a large amount in a sea area at a generation site or in a landed state and discharging the jellyfish as a pollution-free processing liquid.
[0002]
[Prior art]
In the summer, a lot of jellyfish occur in the sea near Japan. Recently, a large amount of jellyfish has been confirmed to survive even in winter due to warming of the sea area. In plant facilities such as power plants that are located in the coastal area and require a large amount of seawater as cooling water, if the generated jellyfish rush on the tide and are taken in from the cooling water intake, the filter is clogged. And so on. For this reason, jellyfish are captured and collected at power stations using rotary dust removers. The jellyfish landed in this way is either landfilled on land as it is, air-dried, or mechanically, chemically or biologically treated.
[0003]
Landed jellyfish processing has the following problems:
(1) Dead jellyfish generate a bad smell of fish and become a source of bad odor.
(2) Jellyfish has 95 to 98% of the water in its body, so even if it can be incinerated, energy consumption is high, and it is jelly-like and poor in fluidity. Is also difficult to process.
(3) It is difficult to secure land for landfill disposal.
[0004]
In order to solve such a problem, a simple treatment method / apparatus is described in which landed jellyfish are treated biologically and mechanically with anaerobic bacteria under anaerobic conditions, and then drained (for example, , See Patent Document 1). In addition, a method is described in which a jellyfish that has been landed is heated under pressure, and then instantly expanded by depressurization to obtain jellyfish water, and sodium chlorite is added to this jellyfish water to treat the wastewater. (For example, refer to Patent Document 2). However, in the invention described in Patent Document 1, the jellyfish decomposition treatment is due to the natural generation of anaerobic bacteria or the addition of anaerobic bacteria contained in activated sludge after sewage treatment, so an anaerobic environment must be created. In addition, since the decomposition process takes a long period of three days, it is difficult to say that the process is quick and efficient. In the invention described in Patent Document 2, devices such as a heating steam supply facility, a pressurizing tank, and a sodium hypochlorite addition facility are necessary, and the cost of construction and maintenance of these devices is high.
[0005]
[Patent Document 1]
Japanese Patent Laid-Open No. 11-179327
[0006]
[Patent Document 2]
Japanese Patent Laid-Open No. 11-244833
[0007]
[Problems to be solved by the invention]
Accordingly, the present invention is intended to solve the above-mentioned problems relating to the treatment of landed jellyfish, and to solve the problems of the above-mentioned prior art jellyfish treatment method and apparatus, and to provide a quick and efficient biological biological jellyfish. An object is to provide a processing method.
[0008]
[Means for Solving the Problems]
In order to achieve the above object, the present invention decomposes COD contained in an enzyme mixing tank for mixing a jellyfish and a degrading enzyme, and a mixture of jellyfish treated in the enzyme mixing tank and water eluted from the jellyfish. And / or a COD decomposition tower for removal, and a jellyfish treatment apparatus comprising a deodorization tower for exhausting by performing deodorization treatment of gas generated in the enzyme mixing tank and the COD decomposition tower. And leaching water contained in the jellyfish body, decomposing and / or removing COD contained in the mixture of jellyfish and jellyfish elution water, enzyme mixing tank and COD And a step of deodorizing the gas generated in the decomposition tower.
[0009]
According to this jellyfish treatment apparatus and treatment method, in the treatment of jellyfish, wastewater that satisfies the COD wastewater treatment standards can be discharged as a final product, and the off-flavor generated during the treatment of jellyfish can be removed. Can do.
[0010]
The COD decomposition tower may consist of one treatment device selected from the group consisting of an ultraviolet treatment device, an activated carbon treatment device, and an ozone oxidation treatment device, or a combination of two or more treatment devices. That is, the COD decomposition tower may be configured by any one of the ultraviolet treatment apparatus, the activated carbon treatment apparatus, and the ozone oxidation treatment apparatus, or 2 of the ultraviolet treatment apparatus, the activated carbon treatment apparatus, or the ozone oxidation treatment apparatus. A combination of the above may constitute a COD decomposition tower. Of these, an ultraviolet treatment device is particularly preferred, and a combination of the ultraviolet treatment device and the activated carbon treatment device is most preferred. For example, an activated carbon treatment apparatus is provided after the ultraviolet treatment apparatus to constitute a COD decomposition tower.
[0011]
In another embodiment, in addition to the above-described embodiment, a membrane separation device for separating a water-insoluble substance from the treatment liquid supplied to the COD decomposition tower is provided between the enzyme mixing tank and the COD decomposition tower. Further provided. According to this jellyfish processing apparatus, by filtering the treatment liquid obtained by treating jellyfish with an enzyme with a membrane separation apparatus, the water-insoluble matter such as jellyfish fragments and impurities that cannot be decomposed by the enzyme is removed, and the filtrate is filtered. Can flow into the COD cracking tower. By the treatment by the membrane separation apparatus, the COD value of the treated water flowing into the COD decomposition tower can be lowered, and as a result, the COD decomposition time can be reduced. In this aspect, it is preferable to further include a treatment tank for thermally decomposing or incinerating the water-insoluble substance separated by the membrane separator.
[0012]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, the present invention will be described in detail with reference to the drawings.
FIG. 1 is a schematic view for explaining an embodiment of the jellyfish processing apparatus of the present invention. In the figure, reference numeral 1 denotes a jellyfish processing apparatus. This processing apparatus mixes a jellyfish 13 with a degrading enzyme to perform enzymatic decomposition, and in a liquid containing jellyfish processed in the enzyme mixing tank 2. A COD decomposition tower 3 for decomposing the COD, and a deodorization tower 4 for performing a deodorization treatment of the gas generated in the enzyme mixing tank 2 and the COD decomposition tower 3 and exhausting it.
[0013]
In the enzyme mixing tank 2, the jellyfish and the jellyfish decomposing enzyme are stirred and mixed, and the jellyfish is decomposed by an enzymatic reaction. A collagenase can be illustrated as a jellyfish degrading enzyme. The jellyfish has a jelly-like structure in which the protein (collagen) that constitutes its body has a fibrous structure and water is trapped in its mesh. Collagen fibers that make up this network structure are cut by collagenase, the water trapped in the jellyfish body is eluted (released), and the collagen itself is dissolved and removed from the jellyfish body, reducing the volume of the jellyfish. Is done. As the volume of the jellyfish is reduced, the mixture of jellyfish and elution water becomes fluid. In the present specification, jellyfish volume reduction means that by applying a jellyfish degrading enzyme, particularly collagenase, collagen fibers constituting the body of the jellyfish are broken to remove water contained in the body, Collagen itself dissolves and is removed from the jellyfish body, which reduces the jellyfish volume.
[0014]
Collagenase is not particularly limited, and collagenase derived from any organism may be used.For example, bacteria derived from facultative anaerobic Vibrio sp. And / or Bacillus sp. The thing derived from the bacteria which belong to can be used. A specific example of a bacterium belonging to the genus Bacillus is the marine bacterium Bacillus sp. (J26W strain) deposited with the National Institute of Advanced Industrial Science and Technology on April 25, 2001 (accession number FERM P-18313). ). Instead of a jellyfish degrading enzyme, a jellyfish degrading enzyme-secreting bacterium, for example, a bacterium belonging to the above-mentioned genus Vibrio (Vibrio sp.) And / or a bacterium belonging to the genus Bacillus (Bacillus sp.) Is directly put into the enzyme mixing tank 2, Therefore, the jellyfish body may be decomposed by secreting a jellyfish degrading enzyme.
[0015]
The jellyfish to be treated are collected from the sea area where the jellyfish is generated or near the water intake of the plant, from the sea area or seawater where the jellyfish should be removed, using a collector 5 or the like, and lifted to the land with suction dust 6 The seawater and jellyfish recovered together with the jellyfish are separated by the solid-liquid separator 7. The separated seawater is returned to the sea again.
[0016]
The jellyfish that has been subjected to solid-liquid separation is put into the enzyme mixing tank 2 and subjected to enzyme treatment. A crusher for crushing the jellyfish body in advance and feeding it into the enzyme mixing tank 2 may be provided in the front stage of the enzyme mixing tank 2 in order to shorten the enzyme treatment time before being put into the enzyme mixing tank. . The crushing may be performed in the solid-liquid separation apparatus simultaneously with the solid-liquid separation, or a crusher may be separately provided before or after the solid-liquid separation.
[0017]
Next, the enzyme treatment time, stirring speed, and treatment temperature in the enzyme mixing tank 2 will be described, but these conditions can be appropriately changed according to the amount of jellyfish and the amount of enzyme, and are not particularly limited. For example, the enzyme treatment time in the enzyme mixing tank 2 is about 20 to 30 hours when a live jellyfish is used, but when a crushed jellyfish is used, it is decomposed by 90% or more in 3 hours. By treating the jellyfish with an enzyme over this amount of treatment time, the collagen in the jellyfish body is decomposed, and the water in the body is eluted and fluidized. The stirring speed in the enzyme mixing tank 2 can be changed depending on the amount of jellyfish in the tank, and it is preferable to stir at about 10 to 60 rpm, but is not particularly limited. Further, after the jellyfish and the enzyme are sufficiently mixed by stirring, they may be allowed to stand. The treatment temperature is preferably a temperature at which the enzyme works, that is, 15 to 45 ° C., but usually, the treatment can be performed at an outside temperature without particularly performing heating and cooling. Here, a silicon-based odor control agent may be mixed in order to suppress the generation of malodor that occurs when the jellyfish decomposition product decays.
[0018]
The jellyfish reduced in volume by the enzyme treatment is put into the COD decomposition tower 3. Just by performing collagenase treatment, COD exceeds 15 mg / L, which is a general drainage standard concentration (hereinafter referred to as drainage standard) applied to power plants, etc., so the mixture of fluidized jellyfish and elution water is the original. Can not be disposed of in the sea area. Therefore, the mixture of jellyfish and elution water can be subjected to COD decomposition treatment in the COD decomposition tower 3 and discharged as treated water that satisfies the drainage regulations.
[0019]
Preferably, a membrane separation device 8 for separating a water-insoluble substance from a mixture of jellyfish and elution water supplied to the COD decomposition tower is further provided between the enzyme mixing tank 2 and the COD decomposition tower 3. By filtering the fluidized jellyfish-elution water mixture with the membrane separation device 8, jellyfish fragments and impurities that cannot be decomposed by the enzyme are removed, and the filtered filtrate is subjected to the COD decomposition tower. Can flow into. By the treatment by the membrane separation device 8, the COD of the mixture of jellyfish and elution water flowing into the COD decomposition tower 3 can be lowered as compared with that before the membrane treatment, and as a result, the COD decomposition time can be reduced. The membrane separation device 8 may be provided as a part of the enzyme mixing tank 2. As the membrane separation device 8, an ultrafiltration membrane, a microfilter, or the like is used, and a device that can separate a substance of about 10 μm or less from a water-insoluble substance is preferable.
[0020]
The water-insoluble substance separated by the membrane separator 8 may be returned to the enzyme mixing tank 2 and further subjected to collagenase treatment. However, if the treatment is continued for a long period of time, the membrane separator 8 is likely to be clogged. The water-insoluble substance attached to the membrane separation device 8 may be subjected to thermal decomposition or incineration. That is, a line for returning the water-insoluble material separated from the membrane separation device 8 to the enzyme mixing tank may be provided, and a processing tank (not shown) for heating or incineration treatment is provided separately from the enzyme mixing tank 2. May be.
[0021]
In the COD decomposition tower 3, specifically, any one of the following treatments or a combination of two or more treatments is performed.
[0022]
(1) Activated carbon adsorption method
Organic substances in the treated water are adsorbed and separated by activated carbon. It is necessary to regenerate activated carbon after adsorption.
[0023]
(2) Ozone oxidation method
Ozone exhibits a strong oxidizing power due to OH radicals generated when dissolved in water and decomposed. As a result, it is effective for cleavage of unsaturated bonds such as double bonds of substances in water, oxidation of aromatic compounds, oxidation of sulfides and amines. In addition, providing an activated carbon adsorption treatment apparatus in the subsequent stage is effective in adsorbing ozone-degradable components and removing residual ozone.
[0024]
(3) UV irradiation method
Decompose organic matter by utilizing light absorption of organic matter in water. Ozone absorbs ultraviolet light and dissociates into oxygen atoms and oxygen molecules. The dissociated oxygen atoms react with water to generate OH radicals, and the oxidation reaction is accelerated. Therefore, the combination of the ultraviolet irradiation method and the ozone oxidation method increases the organic matter decomposition effect.
[0025]
(4) Membrane treatment method
A COD component of several μm or more is separated by an ultrafiltration membrane or a microfilter membrane. Since separation performance decreases with the lapse of processing time, it is necessary to regenerate or replace the membrane. Although waste is generated every time the membrane is replaced with a new membrane, there is an advantage that the apparatus cost is low compared with the ultraviolet irradiation method and the ozone oxidation method. If the membrane treatment method alone does not satisfy the COD concentration drainage standard value, the combined use with the activated carbon adsorption method is desirable.
[0026]
(5) Flocculant + electrolytic levitation method
After adding a flocculant to agglomerate fine particles and colloidal substances in the mixture of jellyfish and elution water, a direct current is applied to the electrode placed in the levitation tank, and hydrogen and oxygen bubbles are generated by electrolysis. Give rise to The bubbles cause the agglomerated organic matter to float and be removed by solid-liquid separation to reduce COD. Instead of electrolytic levitation, aggregates may be levitated by a pressure levitation method.
[0027]
Among the above methods, it is preferable to use the ultraviolet irradiation method. From the viewpoint of processing time and processing efficiency, after the COD is decomposed to some extent by ultraviolet irradiation, the remaining COD after ultraviolet irradiation is removed by the activated carbon adsorption method. preferable. In the example of FIG. 1, the COD decomposition tower 3 is provided with an ultraviolet irradiation tower 9 and an activated carbon packed tower 10 at a subsequent stage, a supply tank 11 is provided so as to perform ultraviolet irradiation in a circulating manner, and is processed in the enzyme mixing tank 2. The mixture of jellyfish and elution water is once introduced into the supply tank 11 and supplied from there to the ultraviolet irradiation tower 9, and the treated water flowing out from the ultraviolet irradiation tower 9 is returned to the supply layer 11 again. In this manner, the COD is circulated between the supply tank 11 and the ultraviolet irradiation tower 9 until the COD is sufficiently reduced, and the treated water having the sufficiently reduced COD is introduced into the activated carbon packed tower 10. The treated water whose COD has become below the drainage standard concentration (15 mg / L) by ultraviolet irradiation and activated carbon treatment can be drained as clean wastewater. In FIG. 1, the supply tank 11 is provided in the COD decomposition tower and is circulated, but it may be batch-processed.
[0028]
If UV irradiation is used for COD decomposition, H₂O₂(Hydrogen peroxide) should be added during UV irradiation.₂O₂The addition of is preferably performed a plurality of times or continuously during irradiation in terms of COD decomposition efficiency. When the supply tank 11 is provided as in the example of FIG.₂O₂Can be added. Although the irradiation time varies depending on the COD concentration, in the case of 100 mg / L, it can be reduced to 15 mg / L or less, which is the COD drainage standard concentration, by irradiating with a 4 W ultraviolet lamp for about 6 to 12 hours. Further, in order to reduce the processing time, the processing efficiency, and the equipment size, the COD concentration may be set to about 25 mg / L by the ultraviolet irradiation process, and another COD decomposition process such as activated carbon adsorption may be performed after the ultraviolet process.
[0029]
When the activated carbon adsorption method is used for COD decomposition, a mixture of jellyfish and elution water can be passed through an activated carbon packed column. In this method, SV = 1 to 0.5h^-1The COD can be adsorbed and removed by performing the treatment to the extent. Moreover, as another method, the method of throwing activated carbon into the mixture of a jellyfish and elution water, and stirring it is mentioned. After stirring, the activated carbon is removed by a treatment such as filtration to obtain treated water with reduced COD.
[0030]
When the ozone oxidation method is used for COD decomposition, COD can be reduced by treating the ozone gas flow rate at about 1 to 5 L / 0.1 g-COD / min for 3 to 8 hours. Since there is a possibility that trihalomethane is by-produced by ozone oxidation, it is preferable to perform an activated carbon adsorption method after ozone oxidation.
[0031]
When the ultrafiltration membrane method is used for COD decomposition, it is preferable to use one having a fractional molecular weight of 3000 or less. When a hollow fiber type ultrafiltration membrane is used, the COD component is attached to and removed from the hollow fiber membrane, so that it is necessary to regenerate or replace it when the processing performance deteriorates. Although waste is generated by exchanging with a new membrane, the apparatus cost is lower than that of the ultraviolet irradiation method or the ozone oxidation method. When the ultrafiltration membrane method alone does not satisfy the COD concentration drainage standard value, there is a method of decomposing and removing COD to the drainage standard value or less in combination with the activated carbon adsorption method. Moreover, you may process by providing several things from which a fraction molecular weight differs.
[0032]
When using coagulant addition method and electrolytic flotation method for COD decomposition, aluminum (polyaluminum chloride, aluminum sulfate, basic aluminum chloride, etc.) and iron salt system (iron sulfate, iron chloride, etc.) are used as inorganic flocculants. Anionic polymers (sodium alginate, polyacrylamide partially hydrolyzed salts, etc.), cationic polymers (water-soluble aniline resin, polythiourea, polyethylenimine, polyvinylpyridines, etc.), non-polymeric flocculants can be used. Ionic polymers (polyacrylamide, polyoxyethylene, etc.) can be used. Although it is desirable to use the inorganic flocculant and the polymer flocculant in combination, the inorganic flocculant alone or the polymer flocculant can be used alone. However, when the inorganic flocculant is used alone, the resulting aggregate is fine and poor sedimentation, so it may be difficult to obtain a clear supernatant. In such a case, a polymer flocculant is added to coarsen the aggregate. It is preferable to increase the sedimentation property. After adding the flocculant, the agglomerates are floated by electrolytic levitation and removed by liquid separation. In this method, the levitated material is scraped and collected by a scrubber, so that it is generally advantageous in that the sludge has a lower moisture content than the sedimentation method.
[0033]
In the jellyfish decomposition apparatus of the present invention, it is generated from the enzyme decomposition tank and the COD decomposition tower in order to remove malodorous substances such as ammonia, sulfur compounds, and trimethylamine, which are generated by the decay of the jellyfish decomposition products from the enzyme mixing tank and the COD decomposition tank. It is possible to provide a deodorization tower 4 that collects the collected gas and performs deodorization treatment. The deodorization tower 4 is filled with activated carbon, gas generated from the enzyme mixing tank and the COD decomposition tower is collected and introduced into the deodorization tower 4, and a blower for releasing the gas after the deodorization treatment. A line with 12 is provided. After the gas containing malodorous substance is adsorbed by the activated carbon of the deodorizing tower, it can be released into the atmosphere.
[0034]
An example of a jellyfish processing process using the above jellyfish processing apparatus will be described.
The jellyfish in the sea is collected by the jellyfish collector 5, passed through the pump through the suction duct 6, and then the jellyfish and seawater are separated by the solid-liquid separator 7. Thereafter, the separated jellyfish is put into the enzyme mixing tank 2 and the degrading enzyme is supplied into the enzyme mixing tank 2 to stir and mix them. The mixture is extracted in a slurry state by a circulation pump, and the decomposition solution and the undecomposed material are separated by the membrane separation device 8. The separated undecomposed product slurry is returned to the enzyme mixing tank 2 by a circulation line. On the other hand, the decomposition solution that has passed through the membrane separation device 8 is supplied to the supply tank 11. The decomposition liquid supplied to the supply tank 11 is extracted by a circulation pump, circulates between the supply tanks 11 through the ultraviolet irradiation tower 9, and decomposes COD in the decomposition liquid. After the COD component is decomposed by circulating for a predetermined time, the treatment liquid is discharged as clean wastewater after the undecomposed COD component is adsorbed and separated by the activated carbon packed tower 10. The generated cracked gas is sucked by the blower 12 and exhausted through the deodorizing tower 4.
[0035]
Since the jellyfish processing apparatus of the present invention does not require a large-sized apparatus, it is not limited to standing on land, and can be mounted on portable equipment such as movable ships and automobiles. . The jellyfish processing apparatus only needs to operate the jellyfish processing apparatus only when a jellyfish appears, and is not always necessary for a plant in a coastal area. Therefore, if the jellyfish decomposing apparatus of the present invention is installed in a portable facility, the jellyfish decomposing apparatus is moved to the place where the jellyfish appeared, and jellyfish processing is performed there. It can be moved to other locations that require jellyfish processing.
[0036]
【Example】
The present invention will be described in more detail with reference to the following examples. However, the present invention is not intended to be limited thereby.
[0037]
[Example 1]
(1) COD treatment test by ultraviolet irradiation method
The decomposition of COD by the ultraviolet irradiation method was tested. The test solution was obtained by degrading 54 g of jellyfish with a jellyfish degrading enzyme, and the initial COD was 135 mg / L. As the UV lamp, a low-pressure ultraviolet lamp having an output of 4 W, a lamp length of 240 mm, and a main wavelength of 254 nm was used. The shape of the column that wraps the UV lamp is a double tube in which a quartz tube (outer diameter 28 mm) is passed through a PVC cylindrical container (inner diameter 34 mm, height 285 mm), an ultraviolet lamp is placed in the center, and the test solution flows outside. The structure. The test solution was sent from this tank to the column with a magnet pump, passed through the column, and then circulated by a circulation type returning to the tank. The circulation flow rate was 1.6 L / min, and the temperature was 38 ° C. Sampling was performed by collecting 100 mL from the tank every 2 hours. The results are shown in FIG. After 10 hours, the residual COD was 11 mg / L, and it was confirmed that the residual COD was 15 mg / L or less, which is the water quality standard concentration.
[0038]
H₂O₂The result of ultraviolet treatment without addition is shown in FIG. From this result, H₂O₂It can be confirmed that the effect of the addition is large.
[0039]
(2) COD treatment test by activated carbon adsorption method
The removal of COD by the activated carbon adsorption method was tested. As the test solution, an initial COD of about 80 mg / L was used. The test is performed at room temperature of 25 ° C., and 50 g of activated carbon (BOMBA 100CG8-32C Taki Chemical, general activated carbon for water treatment, coal-based) is sampled immediately after addition, 4 hours, 8 hours and 24 hours later. The COD concentration was measured. FIG. 4 shows the change over time in the residual COD concentration when measuring the COD equilibrium adsorption amount on activated carbon. The residual COD concentration after 24 hours has almost reached equilibrium, and this point was taken as the equilibrium adsorption rate.
[0040]
(3) COD adsorption column test on activated carbon
The removal of COD by a column packed with activated carbon was tested. As the test solution, an initial COD of about 80 mg / L was used. Tests were conducted for SV = 1 and 0.5. Here, SV = (liquid flow rate / active carbon amount) is shown. FIG. 5 shows the change over time in the COD concentration of the sample flowing out from the column. As is apparent from FIG. 5, since COD contained in the mixture of jellyfish and eluate is slow to be adsorbed on activated carbon, the activated carbon adsorption tower preferably has a low SV value of about SV = 0.5h-1, It has been found that the activated carbon treatment is preferably performed as a subsequent treatment such as irradiation or ozone oxidation.
[0041]
(4) COD treatment test by ozone oxidation method
The removal of COD by the ozone oxidation method was tested. As the test solution, an initial COD of about 80 mg / L was used. As the ozone generator, AOC-30W manufactured by Masuda Laboratory Co., Ltd. was used, and the ozone gas flow rate was 3 L / min. FIG. 6 shows changes with time in the COD concentration by the ozone oxidation method.
[0042]
It was confirmed that the COD component is reduced by the ozone treatment. However, ozone has a strong oxidizing action, and trihalomethane may be generated during the treatment reaction from organic substances, chlorine and bromine contained in the jellyfish. Trihalomethane is a halogen-based organic compound that is chloroform (CHCl_Three), Bromodichloromethane (CHBrCl₂), Dibromochloromethane (CHBr₂Cl), bromoform (CHBr_Three) Is a general term. Some of these may have carcinogenicity. In Japan, water quality standards for trihalomethane are established, but no drainage standards are established. The concentration of trihalomethane before and after the treatment was measured in accordance with JIS K0125: 1995 “Testing method for volatile organic compounds in water and wastewater” assuming that COD is treated by ozone and subsequent activated carbon treatment. The results are shown in Table 1 below.
[0043]
[Table 1]

[0044]
As is clear from the table, it was found that trihalomethane can be removed by the activated carbon adsorption treatment after the ozone treatment.
[0045]
(5) COD treatment test by ultrafiltration membrane method
The removal of COD by the ultrafiltration membrane method was tested. Fine particles and colloidal substances that become COD components in the jellyfish decomposition solution were separated by a semipermeable membrane to reduce COD. The apparatus used was a cross-flow filtration method using a hollow fiber membrane that can easily suppress the formation of deposits on the membrane surface due to COD and that can easily increase the membrane area per module. For the test solution, an 850 mL initial COD equivalent of about 80 mg / L was used. As an ultrafiltration membrane, SEP-0013 (manufactured by Asahi Kasei, membrane inner diameter 2 mm, effective membrane area 80 cm)², Nominal pore size 0.25 μm, molecular weight cut-off 3000, module outer diameter 20 mm × 130 mm (pencil type)). Water flow was carried out at a room temperature of 21 to 23 ° C. using a method of circulating and filtering the inside of the hollow fiber with a tube pump. The filtration rate was 1.1 to 1.3 mL / min. After circulating for 10 hours, the treatment liquid was measured. The results are shown in Table 2 below.
[0046]
[Table 2]

[0047]
The membrane treatment for 10 hours removed COD from raw water having a COD concentration of 80 mg / L to 13 mg / L, and transparent filtered water having a water quality standard concentration of 15 mg / L or less was obtained. In the membrane treatment method, the COD component adheres to and is removed from the hollow fiber membrane. Therefore, when the treatment performance deteriorates, it is necessary to regenerate or replace it with a new one. Moreover, when the COD density | concentration after a process is less than a waste water reference value, the treated water which satisfy | fills a reference value can be obtained by combined use with other methods, such as an activated carbon adsorption method.
[0048]
(6) COD treatment test by flocculant + electrolytic levitation method
After adding the flocculant, electrolytic levitation was performed to test the removal of COD. As the test solution, one corresponding to an initial COD of about 92 mg / L was used. This test solution was placed in a 500 mL beaker, 500 mg / L or 1000 mg / L of inorganic flocculant PAC (Taki Chemical) was added, and neutralized to pH 8 with pH test paper while stirring with a stirrer. Subsequently, the stirring was loosened, 2 mg / L of polymer flocculant A-133 (Taki Chemical) was added, and the mixture was allowed to stand to settle the suspension. The supernatant was collected, and the COD concentration was measured. Moreover, only the inorganic flocculant was added at 500 mg / L, and the COD concentration was measured in the same manner. The results are shown in Table 3.
[0049]
[Table 3]

[0050]
By adding inorganic flocculant 1000 mg / L and polymer flocculant 2 mg / L, the COD concentration 92 mg / L in the raw water was reduced to 57 mg / L. Moreover, when the COD density | concentration after a process is less than a waste water reference value, the treated water which satisfy | fills a reference value can be obtained by combined use with other methods, such as an activated carbon adsorption method.
[0051]
Furthermore, among the above results, a test solution that was agglomerated in a 2 L container using a combination of an inorganic aggregating agent 500 mg / L and a polymer aggregating agent 2 mg / L with good aggregation conditions and a small amount of drug addition. The electrode was installed. As the electrode, three 65 × 30 × 2 mm electrodes were arranged, and the center was used as an anode. The electrode area is 39cm²(Total of the front and back surfaces of the center electrode), current density 2.6 A / dcm²A current was applied as (current value 1 A current suppression at the time of bubble generation, voltage 3 A).
[0052]
Table 4 shows the COD concentration before and after the treatment. After 1 hour, the COD concentration reached 61 mg / L, but the COD hardly decreased even after 4 hours thereafter, so it is considered that a short time treatment is sufficient.
[0053]
[Table 4]

[0054]
[Example 2]
A jellyfish decomposition experiment on a bench scale was performed on the jellyfish decomposition apparatus, the ultraviolet irradiation tower, and the activated carbon packed tower in the jellyfish processing apparatus shown in FIG. The contents and results of the experiment are described below.
[0055]
<Jellyfish decomposition device>
The jellyfish decomposing apparatus has a shape as shown in FIG. 7, is made of acrylic, and has an effective processing volume of 50L.
7 kg of crude enzyme solution diluted 5-fold with seawater was added to the jellyfish decomposition apparatus in FIG. 7, 20 kg of cut jellyfish was added, reacted at room temperature with stirring at 60 rpm, and the remaining solid content after the passage of time was examined. As shown in FIG. 8, the remaining solid content became 10% or less within 5 hours.
[0056]
<COD reduction device>
When COD was measured by the potassium permanganate method of JIS K010217 with respect to the jellyfish decomposition product treated using the jellyfish decomposition apparatus, it was about 500 mg / L. In order to reduce this COD, an ultraviolet treatment device and an activated carbon treatment device were produced, and the COD reduction effect was examined.
[0057]
FIG. 9 shows a schematic diagram of an ultraviolet oxidation test apparatus. The ultraviolet irradiation device 100 is a device in which a quartz tube (outer diameter 30 mm) 102 is passed through a SUS316L cylindrical container (inner diameter 40 mm) 101 and an ultraviolet lamp (output 85 W) is installed in the center. The jellyfish decomposition solution circulated by the pump 104 from the acrylic tank (50 L capacity; cylindrical shape with a bottom diameter of 350 mm and a height of 550 mm) 103 was passed between the tubes 102. 35 kg of jellyfish decomposition solution is put into the tank 103 and H is started at the start.₂O₂Was added under the condition that 5.83 g / h (equivalent to 167 mg / L / h) was continuously added after 7.5 hours, and the COD concentration (Fig. 10A) and H₂O₂The concentration (FIG. 10B) was measured. As a result, it was confirmed that the COD concentration could be reduced to a regulation value of 15 mg / L or less only by ultraviolet irradiation.
[0058]
On the other hand, activated carbon has a specific surface area of 500-1500 m.²Since it is as large as / g, a small amount of dissolved organic matter can be adsorbed. Therefore, in order to reliably reduce the COD concentration, as shown in FIG. A schematic diagram of the activated carbon packed column 110 is shown in FIG. The activated carbon packed tower 110 is a PVC cylinder 111 (bottom diameter 120 mm, height 400 mm), and filled with 3 L of activated carbon. An ultraviolet irradiation-treated jellyfish decomposition solution (COD is about 25 mg / L) was continuously supplied from below by a pump 112. At the liquid outlet provided in the upper part of the activated carbon packed tower 110, the COD concentration and H₂O₂The concentration was measured (Figure 12). As a result, stable COD and H over at least 210 hours₂O₂It became clear that the concentration reduction treatment can be performed.
[0059]
<Deodorization test>
The odor produced during the jellyfish treatment as described above was measured at each treatment stage by the olfactory measurement method. The olfactory measurement method attempts to quantify the intensity of odor by using human olfaction. In that case, the strength of the odor is evaluated by the whole odor, which is different from the method of measuring the concentration for each causative substance of the odor as in the instrumental analysis method.
[0060]
Each tank shown in FIG. 13 was connected to a flex pump (Ziel Science) with a Teflon tube, and the gas in the tank was collected in a sampling bag (Tedlar Bag, ASONE).
[0061]
The sensory test for odor was performed as follows. First, a bag containing odorless air and a bag containing gas obtained by diluting the target gas were prepared. Give the three panelists (judgment judges who judge the odors) the two bags, and determine if the difference is felt. Gradually increase the dilution factor, and all the panelists will see the difference between the two bags. The dilution factor at the time when it was no longer felt was determined. The results are shown in Table 5.
[0062]
[Table 5]

[0063]
From this result, the odor concentration and odor index at each treatment stage were determined.
First, the threshold value of each panel was obtained as a common logarithm as follows. For example, in the case of paneler i, the paneler threshold value Xi is obtained by the following equation.
[0064]
Xi = (logM_1i+ LogM_0i) / 2
In the formula, M1i: dilution factor at which the paneler's answer is the correct answer
M0i: Dilution factor for which panelist's answer is incorrect
From the average value X of the threshold values of the obtained panelists, the odor concentration Y was determined by the following formula.
Y = 10^X
A value Z obtained by multiplying the average value X of the paneler threshold by 10 is defined as an odor index.
Z = 10X (= 10logY)
Table 6 shows the odor concentration Y and the odor index obtained in this manner at each treatment stage.
[0065]
[Table 6]

[0066]
Odor is sensuous and is a pollution that does not pollute the air and soil for a long time.Therefore, there is no uniform regulation value nationwide. The central city and special city offices will determine the prescribed areas and standards. The regulation standard (No. 1 regulation) at the site boundary in each place is the odor index 10-21, and the odor index 12-22 in the gas leaking from each tank of the jellyfish processing apparatus according to the present invention is almost the regulation standard. It fits.
[0067]
【The invention's effect】
As is apparent from the above, according to the present invention, in the jellyfish treatment, wastewater that satisfies the COD wastewater treatment standards can be discharged as a final product, and an odor generated during the jellyfish treatment. Can be removed. According to this invention, it is also possible to make it 10-20 mg / L or less severer than the waste water standard 160 mg / L (daily average 120 mg / L) based on the water pollution prevention method. Therefore, jellyfish can be processed without affecting the environment. Further, by performing the membrane separation treatment after the enzyme treatment, the COD value of the treated water flowing into the COD decomposition tower can be lowered, and as a result, the COD decomposition time can be reduced. Furthermore, if the jellyfish processing apparatus of the present invention is mounted on a portable facility, the jellyfish processing apparatus may be moved to the jellyfish appearance location for processing, which is preferable in that it does not take up the installation area of the jellyfish processing apparatus in the plant.
[Brief description of the drawings]
FIG. 1 is a schematic view of a jellyfish processing apparatus of the present invention.
2 shows the results of a COD treatment test in which a test solution having an initial COD of 135 mg / L was treated by an ultraviolet irradiation method in Example 1. FIG.
FIG. 3 shows H in Example 1.₂O₂The result of the COD process test by the ultraviolet irradiation method in the case of no addition is represented.
4 shows a change with time in residual COD concentration during measurement of COD equilibrium adsorption on activated carbon in Example 1. FIG.
5 shows the COD adsorption column test results in Example 1. FIG.
6 shows a change with time in COD concentration during ozone oxidation in Example 1. FIG.
7 is a schematic view of a jellyfish decomposing apparatus in Embodiment 2. FIG.
8 is a graph showing the change over time in residual solid content during jellyfish decomposition in Example 2. FIG.
9 is a schematic view of an ultraviolet light participation test apparatus in Example 2. FIG.
10 shows COD concentration (A) and H at the time of ultraviolet irradiation in Example 2. FIG.₂O₂It is a figure which shows a time-dependent change of a density | concentration (B).
11 is a schematic view of an activated carbon packed tower in Example 2. FIG.
12 shows COD concentration and H during the activated carbon treatment in Example 2. FIG.₂O₂It is a figure which shows a time-dependent change of density | concentration.
13 is a diagram showing a place where odor is measured in Example 2. FIG.

Claims

Enzyme mixing tank for mixing jellyfish and collagenase , COD decomposition tower and enzyme mixing tank for decomposing and / or removing COD contained in a mixture of jellyfish and jellyfish treated in the enzyme mixing tank And a deodorization tower for performing deodorization treatment of gas generated in the COD decomposition tower and exhausting the jellyfish treatment apparatus.

The jellyfish processing apparatus according to claim 1, wherein the mixing of the jellyfish and the collagenase is performed by mixing a jellyfish and a collagenase-secreting bacterium and causing the collagenase-secreting bacterium to secrete the collagenase.

The jellyfish processing apparatus according to claim 1 or 2, wherein the collagenase is derived from Vibrio and / or Bacillus.

COD decomposition tower, ultraviolet treatment device, any one of claims 1 to 3 comprising a combination of activated carbon treatment apparatus and an ozone oxidation treatment apparatus one processing device selected from the group consisting of, or their two or more processing devices 1 The jellyfish processing apparatus of item .

The membrane separation apparatus for isolate | separating a water-insoluble substance from the process liquid supplied to a COD decomposition tower is further provided between the enzyme mixing tank and the COD decomposition tower . The jellyfish processing apparatus of any one of Claims .

The jellyfish processing apparatus of Claim 5 which further has a processing tank for carrying out the thermal decomposition or incineration processing of the water-insoluble substance isolate | separated with the membrane decomposition apparatus.

The jellyfish processing apparatus according to any one of claims 1 to 6 , further comprising a pulverizing apparatus for pulverizing the jellyfish in a preceding stage of the enzyme mixing tank.

Mixing jellyfish and collagenase to elute water contained in the jellyfish body; decomposing and / or removing COD contained in the mixture of jellyfish and jellyfish elution water; and enzyme mixing tank and COD And a step of deodorizing gas generated in the decomposition tower.

The jellyfish treatment method according to claim 8, wherein the mixing of the jellyfish and the collagenase is performed by mixing a jellyfish and a collagenase-secreting bacterium, and causing the collagenase-secreting bacterium to secrete the collagenase.

The jellyfish treatment method according to claim 8 or 9, wherein the collagenase is derived from Vibrio and / or Bacillus.

Degradation and / or removal of COD is ultraviolet treatment, any of claims 8 to 10 which is performed by a combination of activated carbon treatment and one treatment selected from the group consisting of ozone oxidation treatment, or their two or more processing 1 The jellyfish processing method of claim | item .

The jellyfish treatment method according to any one of claims 8 to 11, further comprising a step of separating a water-insoluble substance by membrane separation before decomposition and / or removal of COD.

The jellyfish treatment method according to claim 12 , further comprising a step of thermally decomposing or incinerating the water-insoluble substance separated by membrane separation.

The jellyfish processing method according to any one of claims 8 to 13, further comprising a step of crushing the jellyfish before mixing the collagenase and the jellyfish.