JP3796863B2 - Method and apparatus for decomposing polychlorinated biphenyl compounds - Google Patents

Description

ける重力の加速度については９８０ｃｍ／ｓｅｃ^２であるから、Ｇ＝１．１１８×１０^７／５９８０≒１１，２００である。従って重力の加速度より約１１，２００倍の膨大な加速度による強力な超音波を発振させ、被処理液に対して強力な超音波により激しく振動をさせて、多量のキャビテーションを発生されることにより、超音波本来における作用及び超音波によるキャビテーションの発効によって、溶媒及びポリ塩化ビフェニル類化合物との間において相対速度が生じて、この両者との間に対して摩擦力が作用して、この摩擦力によりポリ塩化ビフェニル類化合物の結合分子鎖における主鎖及び側鎖が盛んに切断をされ、更にベンゼン環においても開裂されることによって、ポリ塩化ビフェニル類化合物を分解処理させ、再度超音波分解処理槽内に被処理液を低流速によって導入させることにより、被処理液を低流速により循環させて超音波分解処理をさせ、ポリ塩化ビフェニル類化合物は次第に分解処理されるのであり、

ポリ塩化ビフェニル類化合物に対して超音波による照射をさせることにより、ポリ塩化ビフェニル類化合物の分解処理に対する分解率の測定についてはＧＣ−ＥＣＤ（電子捕獲型検出器付ガスクロマトグラフ）により分析を行なった結果であり、被処理液を低流速により循環処理させて、超音波による照射をさせ、被処理液に含有しているポリ塩化ビフェニル類化合物の個々における各部分に対して分解処理をさせて、ポリ塩化ビフェニル類化合物の総体的な分解処理に対する超音波の照射による分解反応処理時間においては２５〜３０分間の超音波における照射時間が必要であることを実験によって判明したのであり、超音波による照射反応処理において３０分間以上の分解処理をさせても同程度以上による分解率は発揮できないのである。従って被処理液に含有しているポリ塩化ビフェニル類化合物の個々における各部分については超音波に接触される照射反応時間に対して超音波をできる限り長い期間有効的に接触させ照射させる必要があるので、それに適応させるために低流速により循環処理をさせ、ポリ塩化ビフェニル類化合物の総体的な分解処理において超音波による照射反応が必要であることを実験によって判明したのである。次にポリ塩化ビフェニル類化合物の結合分子鎖において側鎖結合による塩素分子については側鎖を超音波分解処理における摩擦力及び超音波分解処理により惹起されたキャビテーションによって切断され、側鎖に結合していた塩素分子は遊離されるのであり、遊離状態にされたすべての塩素分子についてはポリ塩化ビフェニル類化合物を超音波により分解処理させる以前において、被処理液に注入添加させていたナトリウムアルコラート（ナトリウムエチラート→ナトリウムエトキシド及びナトリウムメチラート→ナトリウムメトキシド）または金属ナトリウムによるナトリウム分子と遊離状態にされたすべての塩素分子とが結合されることにより、塩化ナトリウムが生成されるのである。更にポリ塩化ビフェニル類化合物の結合分子鎖における主鎖結合についても主鎖を超音波分解処理による摩擦力及び超音波分解処理により惹起されたキャビテーションによって切断され、ベンゼン環は遊離されるのであり、遊離状態にされたすべてのベンゼン環についても強力な超音波を効率的に最も有効な照射処理させることにより、強力な超音波による摩擦力の作用及び強力な超音波により惹起されたキャビテーションの作用によって、遊離状態にされたベンゼン環については強力な超音波の酸化作用によりベンゼンからフェノール（ヒドロキシベンゼン）を経過して、更にヒドロキノンよりキノン（ベンゾキノン）へと酸化をされ、次に酸化作用が促進されてベンゼン環は切断され開裂をされるのであり、最終的に直鎖の不飽和ジカルボン酸であるムコン酸（ＨＯＯＣＣＨ＝ＣＨＣＨ＝ＣＨＣＯＯＨ）が生成されるのである。従って遊離状態にされたすべてのベンゼン環については強力な超音波による摩擦力の作用及び強力な超音波により惹起されたキャビテーションの作用によって、酸化作用を惹起されることになり、瞬時においてベンゼン環は切断され開裂をされて、最終的にムコン酸（２．４−ヘキサジエンニ酸）が生成されるのである。次に超音波分解処理における超音波分解処理装置について、ポリ塩化ビフェニル類化合物に対する抽出処理を完結させた抽出処理液において、超音波分解処理用の移送ポンプ（１５）によりチタン製の超音波分解処理槽（１６）内に導入させ、更にナトリウムアルコラート（ナトリウムエチラート→ナトリウムエトキシド及びナトリウムメチラート→ナトリウムメトキシド）または金属ナトリウムにおける超音波分解処理用の薬品貯留タンク（１７）よりナトリウムアルコラートまたは金属ナトリウムを超音波分解処理用の薬品用流量制御装置連動定量ポンプ（１８）によって、超音波分解処理槽内における被処理液に対して定量を注入添加させるのである。次に超音波分解処理装置に対してシステム外における超音波分解処理用の真空ポンプ（１９）により、超音波分解処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更に超音波分解処理用のデジタル真空一定装置（２０）によって、高真空の状態を持続させるのである。次に超音波分解処理槽の外側にて超音波分解処理用の水冷ジャケット（２１）を接触装着させておき、超音波分解処理装置に対してシステム外における超音波分解処理用の水冷却装置（２２）によって水を冷却処理させ、冷却水を超音波分解処理用の冷却水循環ポンプ（２３）により水冷ジャケット内に導入させて、超音波分解処理槽内の被処理液を冷却処理させ、０〜４°Ｃにおける低温の状態を超音波分解処理用の温度調節器（９１）によって温度調整させることにより、低温の状態を持続させるのである。更に被処理液を冷却処理させた後における処理水については水冷ジャケットより排出させ、超音波分解処理用の水貯留タンク（２４）に処理水を貯留させて、再度冷却装置に導入させて冷却水を循環させるのである。次に超音波分解処理槽内における被処理液に対して高真空・冷却処理による低温の状態を持続させる処理条件下によって、被処理液を超音波分解処理槽内より超音波分解処理用の被処理液循環ポンプ（２５）により、被処理液を循環処理させて、被処理液に含有しているポリ塩化ビフェニル類化合物における個々の各部分に対して超音波による照射反応処理をさせ分解処理させるが、それに適応させるために被処理液の循環処理させる流速を低流速における処理条件下によって、ポリ塩化ビフェニル類化合物を分解処理させるのである。次に超音波による照射処理について低流速における処理条件下により循環処理させている被処理液を超音波分解処理部（２６）内に導入させ、超音波分解処理部内においてはポリ塩化ビフェニル類化合物を含有している被処理液における進行流に対して直角の状態において、超音波分解処理用の超音波発振装置（２７）を接触装着させておき、超音波分解処理用の超音波発生装置（２８）及び超音波分解処理用の超音波電力計（２９）により超音波の発振出力を調整させて、超音波発振装置より実効出力１，２００Ｗ、周波数（振動数）１９．５ＫＨｚ、振幅６０〜８０μ、超音波の強度５０Ｗ／ｃｍ^２による強力な超音波を発振させ、被処理液を高真空・冷却処理による低温の状態における処理条件下により、強力な超音波による激しく振動をさせて、超音波による摩擦力の作用及び強力な超音波によって惹起されたキャビテーションの作用によって、ポリ塩化ビフェニル類化合物を超音波による照射反応処理させて分解処理させ、被処理液を再度超音波分解処理槽内に低流速により導入させて循環処理させるのであり、被処理液を超音波による照射処理させ低流速によって循環処理させることにより、被処理液に含有しているポリ塩化ビフェニル類化合物を強力な超音波による照射処理によって次第に分解処理されるのである。次に被処理液に含有しているポリ塩化ビフェニル類化合物を超音波による照射処理させて分解処理させ、超音波による分解処理を完結させた処理液においては超音波分解処理槽の下部に装着させている超音波分解処理用の処理液排出電磁弁（３０）を作動させ開放状態にさせることにより、超音波の照射処理による分解処理が完結させた処理液を超音波分解処理装置におけるシステム外に摘出処理させるのであり、更にポリ塩化ビフェニル類化合物を完璧に分解処理させるために超音波分解処理装置におけるシステム外に摘出処理させた処理液を紫外線分解処理させるのである。次にポリ塩化ビフェニル類化合物に対して完璧に分解処理をさせるための紫外線分解処理について、ポリ塩化ビフェニル類化合物において超音波による照射処理させて分解処理を完結させ、超音波分解処理装置のシステム外に摘出処理させたポリ塩化ビフェニル類化合物に対して超音波により分解処理させた未分解の部分をも含有している処理液において、ポリ塩化ビフェニル類化合物を完璧に分解処理させるために紫外線分解処理用の移送ポンプによって、チタン製の紫外線分解処理槽内に導入させ、紫外線分解処理槽内に導入させた被処理液に対してポリ塩化ビフェニル類化合物を紫外線による照射反応処理させることにより、完璧に分解処理をさせるための化学的な反応において必要なナトリウムアルコラート（ナトリウムエチラート→ナトリウムエトキシド及びナトリウムメチラート→ナトリウムメトキシド）または金属ナトリウムの全量に対する残部による１／３の分量におけるナトリウムアルコラートまたは金属ナトリウムを被処理液に注入添加させ、更にポリ塩化ビフェニル類化合物における未分解の部分を紫外線により照射反応処理させ分解処理させる場合において、紫外線による照射反応処理に対する反応速度を増大させるために、光電導性を保有している二酸化チタンを被処理液に対して１〜４％の容量比における割合により定量を導入添加させ、次に紫外線分解処理槽内において紫外線の透過性を良好にさせ、かつ紫外線による効率についても増大をさせるために、紫外線分解処理装置のシステム外における真空ポンプによって、紫外線分解処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更にデジタル真空一定装置により高真空の状態において持続をさせるのである。次に紫外線分解処理槽内における被処理液に対して冷却処理による低温の状態にさせるために、紫外線分解処理槽による外側において水冷ジャケットを接触装着させておき、紫外線分解処理装置のシステム外における水冷却装置によって水を冷却処理させ、冷却処理された冷却水を冷却水循環ポンプにより水冷ジャケット内に導入させて、紫外線分解処理槽内における被処理液を水冷ジャケット内の冷却水により冷却処理させ、被処理液に対して温度調節器により温度調整をさせて、冷却処理された被処理液において０〜４°Ｃによる低温の状態を持続させるのであり、被処理液を冷却処理させた後における処理水については水冷ジャケットより排出させ、更に処理水を水貯留タンク内に導入させ貯留させて、再度冷却装置に導入させ冷却水を循環させるのである。次に高真空・冷却処理による低温の状態における処理条件下により、紫外線分解処理槽の下部に超音波発振装置を接触装着させておき、超音波発生装置及び超音波電力計により超音波の発振出力を調整させ、超音波発振装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μによる強力な超音波を被処理液に対して発振させ、被処理液を強力な超音波により振動させて、強力な超音波の振動により激しいミクロ的な攪拌作用を付加されることによって化学的な反応を促進させるのである。次に紫外線を発生させる石英ガラス性のランプハウスユニットにおいて、二重管ジャケット冷却法によりランプハウスユニットの最内部に紫外線を発生させる高圧水銀ランプまたは高圧キセノンランプを挿入させ、両端を石英ガラスにより固定装着させて、ランプの周辺における最内部の空間に石英ガラス製の空冷ジャケット及びその外側に石英ガラス製の純水による水冷ジャケットを溶着させ装備させておき、紫外線分解処理装置のシステム外における空気ポンプによって外部の空気を空冷ジャケット内に圧送導入させ、ランプによる発熱を気流により強制的に冷却処理させて、ランプを冷却処理させた後の空気についてはシステム外に排出させるのであり、また紫外線分解処理装置のシステム外における純水冷却装置により純水を冷却処理させ、イオン交換器を通過させて、高純度における純水の状態にさせた冷却純水を純水による水冷ジャケット内に圧送導入させ、冷却純水によりランプによる発熱及びランプによる熱線とを強制的に冷却処理させて、冷却処理させた後の純水においては純水による水冷ジャケットより排出させ、更に純水を純水貯留タンク内に導入させ貯留させて、再度純水冷却装置に導入させて冷却純水を循環させるのであり、高圧水銀ランプまたは高圧キセノンランプによる発熱及びランプにより放射された熱線とを気流及び冷却純水によって強制的に冷却処理させることにより、紫外線による温度上昇を抑制されるのでランプハウスユニットより熱線の少ない紫外線を放射させることができるのである。次にランプハウスユニットを紫外線分解処理槽内における被処理液の液面よりも上部または被処理液中の位置に固定装着させ、紫外線分解処理槽の内壁・外壁及びランプハウスユニットとの間において、紫外線分解処理槽内を高真空の状態に耐え得て、外気に対する吸引性がない気密状態を持続させるためにシリコンゴムなどのゴム類及びプラスチック樹脂類によるシール材により密着させ完全なシール状態にさせる必要があり、紫外線分解処理槽内における被処理液に対して高圧水銀ランプまたは高圧キセノンランプによって放射された紫外線を照射処理させるのであるが、ポリ塩化ビフェニル類化合物に対して紫外線による分解処理をさせる場合において、高圧水銀ランプまたは高圧キセノンランプによる必要な出力についてはポリ塩化ビフェニル類化合物において塩素の含有率によって異なり、その１容量％に対して１００Ｗにおける基準の割合によって、それに比例をした出力が必要であることが実験によって判明したのであり、ポリ塩化ビフェニル類化合物の分解処理において着手前の時点における塩素の含有率に対する数値に適応させ比例をさせる方式が簡便である。更にポリ塩化ビフェニル類化合物の紫外線による分解処理をさせる場合において、高圧水銀ランプまたは高圧キセノンランプに対する有効な波長光については２５０〜３７０ｎｍの紫外線領域による波長光が有効に作用をするのであり、特に極大吸収波長の付近においてポリ塩化ビフェニル類化合物に対する分解処理を惹起されることが実験によって判明したのである。次にポリ塩化ビフェニル類化合物の未分解による部分を含有している被処理液に対して紫外線を照射処理させることにより、被処理液に対して、導入添加をさせた二酸化チタンにおいては吸収できる光の波長域が広範囲であるために、紫外線による照射処理において活性点の紫外線光により、二酸化チタンの保有している光電導性による触媒作用によって、ポリ塩化ビフェニル類化合物に対して紫外線による分解処理については分解速度を加速させることになり、光化学反応における反応過程の加速性を増大させるのである。更に紫外線分解処理槽内におけるポリ塩化ビフェニル類化合物の未分解による部分を含有している被処理液に対して高真空の状態・冷却処理による低温の状態及び超音波の振動によるミクロ的な攪拌処理の状態における処理条件下により、ポリ塩化ビフェニル類化合物の未分解による部分に対して紫外線を照射処理させることによって光化学反応が惹起され、基底状態におけるポリ塩化ビフェニル類化合物の未分解による分子においては被処理液に対する紫外線の照射処理によって生じる紫外線光の作用により、基底状態におけるポリ塩化ビフェニル類化合物の未分解による分子に関与する電子において、紫外線光における高エネルギーの電磁波によって生じる光子エネルギーを吸収されることにより、電子がポリ塩化ビフェニル類化合物の未分解による分子内において、より高いエネルギー準位に遷移される際に、ポリ塩化ビフェニル類化合物の未分解による分子においては電子的な光励起状態になるのであり、電子的な光励起状態になったポリ塩化ビフェニル類化合物の未分解による分子においては分子内に励起エネルギーを得ることによって、ポリ塩化ビフェニル類化合物の未分解による分子においては活性化の状態になるのであり、活性化されたポリ塩化ビフェニル類化合物の未分解による分子が他のポリ塩化ビフェニル類化合物の未分解による分子に作用して、紫外線光により励起エネルギーを得ることによって、活性化されたポリ塩化ビフェニル類化合物の未分解による分子より他のポリ塩化ビフェニル類化合物の未分解による分子に対して励起エネルギーを授与させる反応により、自動連鎖反応を次々に進行されるのである。更に紫外線光より励起エネルギーを得ることによって励起状態になり活性化されたポリ塩化ビフェニル類化合物の未分解による分子が他のポリ塩化ビフェニル類化合物の未分解による分子に作用して、励起エネルギーを他のポリ塩化ビフェニル類化合物の未分解による分子に授与させる反応により、ポリ塩化ビフェニル類化合物の未分解による分子においては励起エネルギーを放出させ失活状態になり、再度基底状態に復帰するのである。次にポリ塩化ビフェニル類化合物の未分解による分子について結合分子鎖における側鎖結合により結合している塩素分子においては基底状態におけるポリ塩化ビフェニル類化合物の未分解による分子に対して紫外線を照射処理させることにより、ポリ塩化ビフェニル類化合物の分子においては紫外線を吸収して、励起エネルギーを得ることによって、励起状態になると同時にポリ塩化ビフェニル類化合物における側鎖結合により結合している塩素分子においては解離状態になって遊離されるのである。更に遊離状態になったすべての塩素分子については光化学反応による紫外線分解処理させる場合に着手前の時点において、被処理液に対して注入添加させていたナトリウムアルコラートまたは金属ナトリウムによるナトリウム分子とが結合されて塩化ナトリウムが生成されるのである。

ポリ塩化ビフェニル類化合物に対して超音波分解処理を完結させた後において、未分解の塩素分子に対する紫外線分解処理をさせた際の測定についてはＧＣ−ＥＣＤ（電子捕獲型検出器付ガスクロマトグラフ）により分析を行なった結果である。従ってポリ塩化ビフェニル類化合物に対して超音波分解処理後における未分解の部分について、光化学反応の紫外線による分解反応処理時間においては２７〜３０分間の紫外線による照射処理が必要であることを実験により判明したのであり、ポリ塩化ビフェニル類化合物に対して紫外線による照射処理によって完璧に分解処理を完結されるのである。分解処理後ポリ塩化ビフェニル類化合物に対する分解産物として塩化ナトリウム、ムコン酸及び少量のビフェニルが生成されるのである。次にポリ塩化ビフェニル類化合物に対して超音波分解処理を完結させた後により、完璧な分解処理をさせるための紫外線分解処理装置について、ポリ塩化ビフェニル類化合物に対して超音波による分解処理させ完結させた処理液を超音波分解処理装置のシステム外に摘出処理させ、更に未分解による部分を含有している処理液において、完璧に分解処理させるために超音波分解処理装置より摘出処理させた処理液を紫外線分解処理用の移送ポンプ（３１）によって、チタン製による紫外線分解処理槽（３２）内に導入をさせ、被処理液に含有しているポリ塩化ビフェニル類化合物における未分解の部分に対して紫外線による照射処理によって、完璧に分解処理をさせるための化学的な反応において必要なナトリウムアルコラート（ナトリウムエチラート→ナトリウムエトキシド及びナトリウムメチラート→ナトリウムメトキシド）または金属ナトリウムに対する紫外線分解処理用の第１薬品貯留タンク（３３）より、ナトリウムアルコラートまたは金属ナトリウムを紫外線分解処理用の第１薬品用流量制御装置連動定量ポンプ（３４）によって、ナトリウムアルコラートまたは金属ナトリウムによる定量を紫外線分解処理槽内における被処理液に対して注入添加させ、更に紫外線に対する光電導性を保有している二酸化チタンによる触媒作用によって、ポリ塩化ビフェニル類化合物における未分解の部分に対して紫外線による照射処理させ分解処理させる場合において分解速度を加速増大させるために、光電導性の特性を保有している二酸化チタンに対する紫外線分解処理用の第２薬品貯留タンク（３５）より、二酸化チタンを紫外線分解処理用の第２薬品添加量制御装置連動スクリュー定量供給装置（３６）によって、二酸化チタンの定量を紫外線分解処理槽内における被処理液に対して導入添加させ、次に紫外線分解処理装置のシステム外における紫外線分解処理用の真空ポンプ（３７）によって、紫外線分解処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更に紫外線分解処理用のデジタル真空一定装置（３８）により、紫外線分解処理槽内において高真空の状態を持続させるのである。次に紫外線分解処理槽における外側に対して紫外線分解処理用の水冷ジャケット（３９）を接触装着させておき、紫外線分解処理装置のシステム外における紫外線分解処理用の水冷却装置（４０）によって水を冷却処理させ、更に冷却処理された冷却水を紫外線分解処理用の冷却水循環ポンプ（４１）により水冷ジャケット内に導入させて、冷却水によって紫外線分解処理槽内における被処理液を冷却処理させ、０〜４°Ｃによる低温の状態を紫外線分解処理用の温度調節器（９２）によって温度調節させることにより、低温の状態を持続させるのである。次に被処理液を冷却処理させた後における処理水については水冷ジャケットより排出させ、処理水を紫外線分解処理用の水貯留タンク（４２）に貯留させて、再度水冷却装置に導入させることによって冷却水を循環させるのである。更に紫外線分解処理槽内における被処理液に対して高真空・冷却処理による低温の状態を持続させる処理条件下により、紫外線分解処理槽の下部において紫外線分解処理用の超音波発振装置（４３）を接触装着させておき、紫外線分解処理用の超音波発生装置（４４）及び紫外線分解処理用の超音波電力計（４５）とによって、超音波の発振出力を調整させることにより、超音波発生装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μによる超音波を被処理液に対して発振させ、紫外線分解処理槽内における被処理液に対して超音波による振動を付加させることにより、超音波により激しいミクロ的な攪拌作用を付与される状態になるので、紫外線分解処理に対する反応面積において著しく増大され、またポリ塩化ビフェニル類化合物の未分解による分子自体も振動されるので界面においては理想的な活性状態になり、紫外線分解処理による光化学反応を促進される状態になるのである。次に石英ガラス製によるランプハウスユニット（４６）を紫外線分解処理槽内における被処理液の液面より上部または被処理液中の位置において固定装着させ、紫外線分解処理槽における内壁・外壁及びランプハウスユニットとの間において、シリコンゴムなどのゴム類及びプラスチック樹脂類によるシール材により、紫外線分解処理槽内において高真空による気密状態を持続させるので高真空の状態に耐え得ることができ、また外気に対する吸引性がない気密状態を持続させるために、紫外線分解処理槽における内壁・外壁及びランプハウスユニットとの間において、シール材により密着させ完璧なシール状態にさせる必要がある。次にランプハウスユニットの機構については二重管ジャケット冷却法により、ランプハウスユニットにおける最内部にポリ塩化ビフェニル類化合物の未分解による部分の分解処理に対して完璧な分解処理をさせるために、必要な出力及び波長における条件について適応させた紫外線を発生させる高圧水銀ランプまたは高圧キセノンランプ（４７）を挿入させて、ランプの両端を石英ガラスにより固定装着させ、ランプに接触されている周辺における最内部の空間部分において石英ガラス製によるランプ冷却処理用の空冷ジャケット（４８）を溶着装備させておき、紫外線分解処理装置のシステム外におけるランプ冷却処理用の空気ポンプ（４９）により、外気を空冷ジャケット内に圧送導入させ、空冷ジャケット内において外気で生じる気流によってランプによる発熱を強制的に冷却処理させるのであり、ランプを冷却処理させた後における気流についてはランプハウスユニットよりシステム外に排気させるのである。更に空冷ジャケットの外側に冷却純水によってランプを冷却処理させるために、石英ガラス製によるランプ冷却処理用の水冷ジャケット（５０）を接触溶着させておき、紫外線分解処理装置のシステム外におけるランプ冷却処理用の純水冷却装置（５１）によって、純水を冷却処理させ、次に冷却処理させた冷却純水をランプ冷却処理用のイオン交換器（５２）内に導入させて、冷却純水を循環させる間において純水中に生じる金属イオンなどに対してイオン交換器により除去処理させるのであり、冷却純水をイオン交換器に対して通過排出させることにより、金属イオンなどを除去処理されて高純度による純水の状態にされた冷却純水を水冷ジャケット内に圧送導入させ、水冷ジャケット内に導入をされた冷却純水によって、ランプによる発熱及びランプより放射された熱線とを強制的に冷却処理させるのである。更に冷却処理をさせた後における処理純水については水冷ジャケットよりランプハウスユニットのシステム外に排出させ、次に排出された処理純水を紫外線分解処理装置によるランプハウスユニットのシステム外におけるランプ冷却処理用の純水貯留タンク（５３）内に導入させ貯留させて、再度純水冷却装置に導入させることにより冷却純水を循環させるのである。従ってランプハウスユニットのシステム内部において外気による気流の通気処理及び冷却純水の循環処理によって、ランプによる発熱及びランプより放射された熱線とを強制的に冷却処理させるので紫外線の発生による温度上昇が抑制されるため、ランプハウスユニットより熱線の少ない紫外線を放射されるのである。更に紫外線分解処理槽内におけるポリ塩化ビフェニル類化合物の未分解による部分を含有している被処理液に対して高真空状態・冷却処理による低温の状態及び超音波により激しいミクロ的な攪拌処理における状態とを持続させている処理条件下により、高圧水銀ランプまたは高圧キセノンランプより紫外線を放射させ、ランプハウスユニットを透過させて、熱線の少ない強力な紫外線をポリ塩化ビフェニル類化合物の未分解による部分に対して照射処理させ、光化学反応による紫外線分解処理をさせて、ポリ塩化ビフェニル類化合物の未分解による部分について完全に分解処理をさせることにより、ポリ塩化ビフェニル類化合物に対して完璧に分解処理をさせるのである。次にポリ塩化ビフェニル類化合物に対して紫外線分解処理により完璧に分解処理させて完結をさせた処理液において、紫外線分解処理槽の下部に装着されている紫外線分解処理用の処理液排出電磁弁（５４）を作動させ開放状態にさせることにより、光化学反応による紫外線分解処理を経過させて、ポリ塩化ビフェニル類化合物に対して完璧に分解処理が完結された処理液を紫外線分解処理装置よりシステム外に摘出処理させ、更に処理液を溶媒及びポリ塩化ビフェニル類化合物の分解残留物とを分別させる真空蒸留処理のために、摘出処理された処理液を真空蒸留処理用の移送ポンプにより、真空蒸留処理槽内に導入させるのである。次にポリ塩化ビフェニル類化合物を完璧に分解処理させた処理液より溶媒及び分解残留物とを分別処理させるための真空蒸留処理について、ポリ塩化ビフェニル類化合物に対して完璧に分解処理が完結された処理液を紫外線分解処理装置のシステム外に摘出処理させ、真空蒸留処理用の移送ポンプにより真空蒸留処理槽内に導入させて、溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを含有している被処理液が導入された真空蒸留処理槽内について、真空蒸留処理装置のシステム外における真空蒸留処理用の真空ポンプにより真空蒸留処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更に真空蒸留処理用のデジタル真空一定装置によって高真空の状態を持続させるのである。次に真空蒸留処理槽の下部において真空蒸留処理用の加熱装置を接触装着させておき、加熱装置により真空蒸留処理槽内の被処理液を高真空の状態における処理条件化により、真空蒸留処理用の第１温度調節器によって温度を調整させ、被処理液に含有している溶媒において沸点以上の温度条件下によって間接的な加熱処理をさせることにより、溶媒については気化されて溶媒蒸気の状態になり真空蒸留処理装置内を上昇して、真空蒸留処理装置内の上部において冷却用蛇管を配備されている冷却部における溶媒蒸気凝縮部内に導入させ、溶媒蒸気凝縮部に装備されている真空蒸留処理用の第２温度調節器により、温度を調整させ、溶媒の沸点以下による温度において溶媒蒸気を冷却処理させることにより、溶媒蒸気の状態に対して凝縮処理させ液化をされて溶媒の状態が再現され、溶媒を回収処理させるのであり、真空蒸留処理槽内に導入された溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを含有している被処理液を真空蒸留処理させ、溶媒を完璧に回収処理させた後において、溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを各々別処理できるのである。更に真空蒸留処理槽内に残留されたポリ塩化ビフェニル類化合物による分解残留物を真空蒸留処理装置のシステム外に摘出処理させるのである。更にポリ塩化ビフェニル類化合物による分解残留物において油分を含有している場合にはポリ塩化ビフェニル類化合物による分解残留物を真空蒸留処理装置のシステム外に摘出処理させた後において、油分を除去処理させるため、分離処理槽内に導入させるのである。次にポリ塩化ビフェニル類化合物を完璧に分解処理させた処理液より溶媒及び分解残留物とを分別処理させるための真空蒸留処理装置について、ポリ塩化ビフェニル類化合物に対して完璧に分解処理を完結させた処理液において、紫外線分解処理装置のシステム外に摘出処理させ、更に摘出処理させた処理液に対して真空蒸留処理用の移送ポンプ（５５）により、真空蒸留処理槽（５６）内に導入させて、溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを含有している被処理液を導入させた真空蒸留処理槽内について真空蒸留処理装置のシステム外における真空蒸留処理用の真空ポンプ（５７）によって、真空蒸留処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更に真空蒸留処理槽内を真空蒸留処理用のデジタル真空一定装置（５８）により、高真空の状態を持続させるのである。次に真空蒸留処理槽の下部に真空蒸留処理用の加熱装置（５９）を接触装着させておき、真空蒸留処理槽内の被処理液に対して加熱装置により高真空の状態における処理条件下によって間接的な加熱処理をさせ、加熱装置に対して装備されている真空蒸留処理用の第１温度調節器（６０）によって、温度を調整させ、高真空の状態における処理条件下に対応させて、被処理液に含有している溶媒に対する沸点温度以上の設定温度条件下による加熱処理の状態を持続させ、被処理液に含有している溶媒は沸点温度以上の加熱処理により気化され、溶媒蒸気の状態によって真空蒸留処理装置内を上昇して、真空蒸留処理装置の上部による真空蒸留処理用の溶媒蒸気凝縮部（６１）内に導入させて、溶媒蒸気凝縮部内においては周囲に真空蒸留処理用の冷却用蛇管（６２）を配備されている真空蒸留処理用の冷却部（６３）を装備させておき、真空蒸留処理装置のシステム外における真空蒸留処理用の水冷却装置（６４）により、水を冷却処理させ、更に冷却処理された冷却水を真空蒸留処理用の冷却水循環ポンプ（６５）によって、真空蒸留処理装置内の上部における冷却部に対して配備されている冷却用蛇管内に導入させ、真空蒸留処理装置内の上部における溶媒蒸気凝縮部内に導入をされた溶媒蒸気に対して冷却処理させて、溶媒蒸気凝縮部において装備されている真空蒸留処理用の第２温度調節器（６７）によって、温度を調整させ、被処理液に含有している溶媒における沸点温度以下の設定温度条件下によって冷却処理の状態を持続させるのである。更に溶媒蒸気を冷却処理させた後における処理水については冷却用蛇管より排出させて、真空蒸留処理装置のシステム外における真空蒸留処理用の水貯留タンク（６６）内に処理水を導入させて貯留させ、再度水冷却装置に導入させて冷却水を循環させるのである。次に真空蒸留処理装置内による溶媒蒸気凝縮部内に導入された溶媒蒸気を溶媒における沸点温度以下の温度条件下に対する冷却処理により凝縮処理させて液化させ、溶媒蒸気凝縮部内の冷却部における冷却用蛇管の下部に装備されている真空蒸留処理用の凝縮液滴下受納回収器（６８）によって、凝縮液としての溶媒を回収処理させて収納させ、凝縮液滴下受納回収器内に回収処理された溶媒を真空蒸留処理用の第１電磁弁（６９）により、自動的な開閉の作動によって開放状態にさせ、真空蒸留処理装置のシステム外における真空蒸留処理用の回収溶媒貯留タンク（７０）に導入させ貯留させて、回収溶媒の貯留量が定量に到達された時点において、回収溶媒貯留タンク内の回収溶媒を真空蒸留処理用の第２電磁弁（７１）によって、自動的な開閉の作動により開放状態にさせ、真空蒸留処理装置のシステム外に摘出処理させるのであり、真空蒸留処理装置により被処理液を完璧に真空蒸留処理させ完結させて溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを分別処理させるのである。次に真空蒸留処理に関した装置を停止させ、真空蒸留処理槽内に残留しているポリ塩化ビフェニル類化合物による分解残留物を冷却処理させて、真空蒸留処理装置のシステム外に摘出処理させ、更に分解残留物において油分を含有している場合には分離処理槽内に導入させるのである。次にポリ塩化ビフェニル類化合物による分解残留物に含有している油分を除去処理させるための分解処理について、ポリ塩化ビフェニル類化合物を完璧に分解処理させた後の処理液に対して真空蒸留処理させ、被処理液に含有している溶媒をすべて回収処理させた後において、真空蒸留処理槽内に残留されているポリ塩化ビフェニル類化合物による分解残留物を真空蒸留処理装置のシステム外に摘出処理させ、更にポリ塩化ビフェニル類化合物による分解残留物において油分を含有している場合に油分の除去処理させるため分離処理槽内に導入させるのである。次に分離処理槽内に導入させたポリ塩化ビフェニル類化合物による分解残留物に対してノルマルヘキサンを１：２の容量比における割合により、定量を分解残留物に注入添加させ、ノルマルヘキサンがポリ塩化ビフェニル類化合物による分解残留物に対して浸透性・脱油性及び油分の抽出効率について増進させる良好な処理条件にさせ、分解残留物に含有している油分を抽出処理させるために、分離処理装置のシステム外における真空ポンプによって、分離処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態を持続させ、更にデジタル真空一定装置により分離処理槽内が高真空の状態を持続させるのである。次に分離処理槽の外側に水冷ジャケットを接触装着させておき、分離処理装置のシステム外における水冷却装置によって水を冷却処理させ、更に冷却処理させた冷却水を分離処理装置のシステム外における冷却水循環ポンプにより水冷ジャケット内に導入させて、分離処理槽内における被処理液を水冷ジャケット内の冷却水により冷却処理させ、分離処理装置において装備されている温度調節器によって、温度を調節させ、冷却処理された被処理液において０〜４°Ｃによる低温の状態を持続させるのであり、被処理液に対して冷却処理させた後における処理水については水冷ジャケットより排出させて、更に分離処理装置のシステム外における水貯留タンク内に処理水を導入させて貯留させ、再度水冷却装置に導入させ冷却水を循環させるのである。次に高真空・冷却処理による低温の状態における処理条件下により、分離処理槽の下部に超音波発振装置を接触装着させておき、超音波発生装置及び超音波電力計とによって、超音波の発振出力を調整させ、超音波発振装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μによる強力な超音波を被処理液に対して発振させ、ポリ塩化ビフェニル類化合物による油分混在の分解残留物及びノルマルヘキサンとを含有している被処理液に対して超音波により振動させて、強力な超音波の振動による激しいミクロ的な攪拌作用を付加させることにより、分解残留物に含有している油分の抽出処理反応を促進させるのであり、被処理液に対する各種の処理条件下において、ノルマルヘキサンにより充分にポリ塩化ビフェニル類化合物による油分混在の分解残留物より油分を抽出処理させ、抽出処理時間については１５〜２０分間によって完璧に分解残留物に含有していた油分の抽出処理を完結させ、抽出処理が完結した後において、抽出処理に関与したすべての装置を停止させ、更に溶媒における溶解度、沸点及び比重差を利用して分離処理させるために、油分及びノルマルヘキサンに対して難溶解性によるフルフラールを選定使用するのであり、ポリ塩化ビフェニル類化合物による分解残留物に対してフルフラールを１：１の容量比における割合により、定量を被処理液に注入添加させて、再度すべての装置を作動させ、被処理液に対して各種の処理条件下において、フルフラールにより充分に溶媒分離処理をさせ、溶媒分離処理時間については１０〜１５分間により完璧に分解残留物に含有していた油分に対する溶媒分離処理を完結させ、次に溶媒分離処理が完結させた後において、分離処理に関与したすべての装置を停止させ、分離処理装置を静置させることにより、被処理液においては比重差によって２層部分に分離処理されて、上層部分においては油分及びノルマルヘキサンとの混合液であり、また下層部分にはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液とに分離処理されるのである。更に分離処理槽よりシステム外に装備されているガラス管測定装置または導電率液面測定装置による境界面検出装置によって２層部分に対する境界面の位置を検出測定させ、次に２層部分における境界面の位置を検出測定処理させた後において、分離処理槽内より処理液を分離処理装置のシステム外に摘出処理させる場合において、真空蒸留処理用の移送ポンプによって流出量に対する摘出処理の分量を制御させるか、または超音波レベル計により液面レベルの降下位置を制御させることで摘出処理させ、分離処理槽内における処理液を摘出処理させる分量について調整及び制御させるのである。更に分離処理槽の下部に装着されている処理液排出電磁弁を作動させ開放状態にさせることによって、最初に分離処理槽内の下層部分におけるフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液に対して分解処理装置のシテステム外に摘出処理させ、次に分離処理された各々に対する溶媒及び残留物とを個々において分別処理させるために、摘出処理された処理液を真空蒸留処理させるのであるが、予め真空蒸留処理槽を２槽に分割装備させておき、真空蒸留処理用の移送ポンプによって、真空蒸留処理槽における片方の槽内に分離処理装置より摘出処理されたフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液を導入させ、完全に導入処理を完結させた時点において、分離処理槽の下部における処理液排出電磁弁を自動的に作動させて閉塞状態にさせ、同時に真空蒸留処理用の移送ポンプを連動させて自動的に停止されるのである。次に分離処理槽内において残留されている油分及びノルマルヘキサンとの混合液に対して分離処理装置のシステム外に摘出処理をさせるために、再度処理液排出電磁弁を自動的に作動させて開放状態にさせ、同時に真空蒸留処理用の移送ポンプを連動させ再度自動的に作動させて、分離処理槽内における油分及びノルマルヘキサンとの混合液を分離処理装置のシステム外に摘出処理させ、更に真空蒸留処理用の移送ポンプにより、油分及びノルマルヘキサンとの混合液を真空蒸留処理槽における他方の槽内に導入させるのである。次にポリ塩化ビフェニル類化合物による分解残留物に含有している油分を除去処理させるための分離処理装置について、ポリ塩化ビフェニル類化合物を完璧に分解処理させた後の処理液に対して真空蒸留処理装置により真空蒸留処理させ、被処理液に含有している溶媒を真空蒸留処理装置によってすべて回収処理させた後において、真空蒸留処理槽内に残留されているポリ塩化ビフェニル類化合物による分解残留物を真空蒸留処理装置のシステム外に摘出処理させ、更に摘出処理されたポリ塩化ビフェニル類化合物による分解残留物についた油分が含有している場合には油分を除去処理させるために、ポリ塩化ビフェニル類化合物による分解残留物を分離処理槽（７２）内に導入させるのである。次に分離処理装置のシステム外における分離処理用の第１薬品貯留タンク（７３）よりノルマルヘキサンを分離処理用の第１薬品用流量制御装置連動定量ポンプ（７４）によって、ポリ塩化ビフェニル類化合物による分解残留物に対してノルマルヘキサンを１：２の容量比における割合によって、定量を分離処理槽内に導入させたポリ塩化ビフェニル類化合物による分解残留物に注入添加させ、更に分離処理槽において分離処理用の上部板（７５）により、分離処理槽の上部に対してセットさせ、分離処理槽の上部を閉塞させることによって、分離処理槽内を密閉状態にさせておき、分離処理装置のシステム外における分離処理用の真空ポンプ（７６）によって、分離処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更に分離処理用のデジタル真空一定装置（７７）により、分離処理槽内において高真空の状態を持続させるのである。次に分離処理槽の外側に分離処理用の水冷ジャケット（７８）を接触装着させておき、分離処理装置のシステム外における分離処理用の水冷却装置（７９）により水を冷却処理させ、冷却処理された冷却水を分離処理装置のシステム外における分離処理用の冷却水循環ポンプ（８０）により水冷ジャケット内に導入させて、分離処理槽内における被処理液を水冷ジャケット内の冷却水により冷却処理させ、分離処理装置において装備されている分離処理用の温度調節器（８９）によって、温度を調整させ、冷却処理された被処理液において０〜４°Ｃによる低温の状態を持続させるのであり、被処理液に対して冷却処理された後における処理水については水冷ジャケットより排出されて、更に分離処理装置のシステム外における分離処理用の水貯留タンク（８１）内に処理水を導入させて貯留させ、再度水冷却装置に導入させて冷却水を循環させるのである。次に高真空・冷却処理による低温の状態における処理条件下により、分離処理槽の下部に対して分離処理用の超音波発振装置（８２）を接触装着させておき、分離処理用の超音波発生装置（８３）及び分離処理用の超音波電力計（８４）とにより超音波の発振出力を調整させ、超音波発振装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μによる強力な超音波を被処理液に対して発振させ、ポリ塩化ビフェニル類化合物による油分混在の分解残留物及びノルマルヘキサンとを含有している被処理液に対して超音波により振動させ、強力な超音波の振動による激しいミクロ的な攪拌作用を付加させることによって、分解残留物に含有している油分に対して溶媒による抽出処理反応を促進されるのであり、被処理液に対する各種の処理条件下において、ノルマルヘキサンにより充分にポリ塩化ビフェニル類化合物による油分混在の分解残留物より油分を抽出処理させ、抽出処理時間については１５〜２０分間によって完璧に分解残留物に含有していた油分の抽出処理を完結させ、ノルマルヘキサンによって分解残留物に含有している油分の抽出処理を完結させた後において、抽出処理に関与したすべての装置を停止させ、更に溶媒における溶解度・沸点及び比重の差異を利用して分離処理させるために、油分及びノルマルヘキサンに対して難溶解性によるフルフラールを選定使用するのである。次に分離処理装置のシステム外における分離処理用の第２薬品貯留タンク（８５）よりフルフラールを分離処理用の第２薬品用流量制御装置連動定量ポンプ（８６）によって、ポリ塩化ビフェニル類化合物による分解残留物に対してフルフラールを１：１の容量比における割合によって、定量を被処理液に注入添加させ、再度分離処理に関与されるすべての装置を作動させて、被処理液に対して各種の処理条件下において、フルフラールにより充分に溶媒分離処理をさせ、溶媒分離処理時間については１０〜１５分間により完璧に分解残留物に含有していた油分に対する溶媒分離処理を完結させるのである。次に溶媒分離処理を完結させた後において、分離処理に関与したすべての装置を停止させ、分離処理装置を静置させることにより、分離処理槽内における被処理液においては比重によって総体的に上・下による２層部分に分離され、上層部分においては油分及びノルマルヘキサンとの混合液であり、また下層部分にはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液とに分離処理されるのである。更に分離処理槽よりシステム外に装備されているガラス管測定装置または導電率液面測定装置による分離処理用の境界面検出装置（８７）によって、２層部分に対する境界面の位置を検出処理させ、次に２層部分における境界面の位置を検出測定処理させた後において、分離処理槽内より処理液を分離処理装置のシステム外に摘出処理させるのであるが、真空蒸留処理用の移送ポンプによって流出量に対する摘出処理の分量を制御させるか、または超音波レベル計によって液面レベルの降下位置を制御させるかに対する方法により、分離処理槽内における処理液を摘出処理させる分量について調整及び制御させるのである。更に分離処理槽の下部に装着させている分離処理用の処理液排出電磁弁（８８）を作動させ開放状態にさせることによって、最初においては分離処理槽内の下層部分におけるフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液を分離処理装置のシステム外に摘出処理させ、次に分離処理させた各々に対する溶媒及び残留物とを個々に分別処理させるために、摘出処理された処理液を真空蒸留処理させるのであるが、予め真空蒸留処理槽において２槽に分割装備をさせておき、真空蒸留処理用の移送ポンプによって、真空蒸留処理槽における片方の槽内に分離処理装置より摘出させたフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液を導入させ、完全に導入処理を完結させた時点において、分離処理槽の下部における処理液排出電磁弁を自動的に作動させて閉塞状態にさせ、同時に真空蒸留処理用の移送ポンプを同調させて自動的に停止させるのである。次に分離処理槽内において残留されている油分及びノルマルヘキサンとの混合液に対して分離処理装置のシステム外に摘出処理をさせるために、再度処理液排出電磁弁を自動的に作動させて開放状態にさせ、同時に真空蒸留処理用の移送ポンプを同調させ再度自動的に作動させて、分離処理槽内における油分及びノルマルヘキサンとの混合液を分離処理装置のシステム外に摘出処理させ、更に真空蒸留処理用の移送ポンプによって、油分及びノルマルヘキサンとの混合液を真空蒸留処理槽における他方の槽内に導入させるのである。次に真空蒸留処理槽における分割装備された２槽内に収納されている２種類の２種類の混合液を再度同時に真空蒸留処理させ、ノルマルヘキサン［沸点６８．７°Ｃ（７６０ｍｍＨｇ）］及びフルフラール［沸点１６１．８°Ｃ（７６０ｍｍＨｇ）］における溶媒の沸点差により、真空蒸留処理装置を作動させ最初においてはノルマルヘキサン、次にはフルフラールとを区分的に分留処理させ、真空蒸留処理装置のシステム外に摘出処理させて溶媒を回収処理させるのである。更に溶媒を完全に回収処理が完結させた後において真空蒸留処理に関与したすべての装置を停止させ、真空蒸留処理槽における２槽内に残留されている蒸留残留物の油分及びポリ塩化ビフェニル類化合物による分解残留物とを冷却処理させて、分別処理させた油分及びポリ塩化ビフェニル類化合物による分解残留物とを真空蒸留処理装置のシステム外に各々別個に摘出処理させるのである。なお、ポリ塩化ビフェニル類化合物による分解残留物において油分を含有してない場合には分離処理の工程が必要でないのである。更に真空蒸留処理により回収処理させた各溶媒については連続的にポリ塩化ビフェニル類化合物を分解処理させるため、各々必要な時点において再度使用させるのである。次に回収処理された油分については熱媒体油・潤滑油等で工業的に再度利用させ、また回収処理されたポリ塩化ビフェニル類化合物による分解残留物については再度分離処理させ塩化ナトリウム等を抽出処理させて工業的に再度利用させ、更に工業的に再度利用できない部分については焼却処理装置により焼却処理させるのである。次にポリ塩化ビフェニル類化合物の分解処理に関与する装置をトレーラー車に搭載して車上にて分解処理させるのである。
（作用）本発明についてはトランス内部より摘出処理させたトランス油、コンデンサー本体、ノーカーボン紙、土壌・底質及び被覆電線による絶縁用の被覆部分に多量使用されていたポリ塩化ビフェニル類化合物を完璧に分解処理させる場合において、各品種については総塩素含有率の高い濃度によるポリ塩化ビフェニル類化合物が使用されていたので耐腐蝕性にさせるため、被処理液の接触部分においてチタン製の鋼材を使用するのであり、各種の品類よりポリ塩化ビフェニル類化合物を抽出処理させるため、チタン製による抽出処理槽内に導入させ、更にイソプロピールアルコールまたはノルマルヘキサンにおける溶媒を注入添加させて、高真空・冷却処理による低温とに対する状態を持続させ、抽出処理槽の下部における超音波発振装置により強力な超音波を発振させて、被処理液に対して強力な超音波による振動を付加させ、強力な超音波により激しいミクロ的な攪拌作用を付与させる状態の処理条件下により、抽出処理装置によってポリ塩化ビフェニル類化合物を抽出処理させ、更にポリ塩化ビフェニル類化合物を完璧に抽出処理させ完結させた処理液において、抽出処理装置よりシステム外に摘出処理させるのである。次にポリ塩化ビフェニル類化合物を抽出処理させた後の処理液において、チタン製による超音波分解処理槽内に導入させ、更にナトリウムアルコラートまたは金属ナトリウムの定量を被処理液に注入添加させて、高真空・冷却処理による低温とに対する状態を持続させる処理条件下により、ポリ塩化ビフェニル類化合物の含有している被処理液に対して超音波発振装置より強力な超音波を発振させ、強力な超音波により被処理液を激しく振動させて、超音波自体による作用及び超音波によって惹起されたキャビテーションの発効により、被処理液の構成をされている溶媒及びポリ塩化ビフェニル類化合物との間において相対速度が生じて、両者との間に対して摩擦力が作用して、摩擦力の作用によってポリ塩化ビフェニル類化合物の結合分子鎖による主鎖結合及び側鎖結合とを盛んに切断されるのであり、ポリ塩化ビフェニル類化合物の側鎖結合における塩素分子については超音波処理により超音波自体の作用・超音波によって惹起されたキャビテーションの発効及び摩擦力とにより側鎖結合が切断され、側鎖に結合していた塩素分子は遊離されるのであり、遊離状態にされたすべての塩素分子については超音波分解処理させる以前において被処理液に予め注入添加させていたナトリウムアルコラートまたは金属ナトリウムによるナトリウム分子とが結合されて、塩化ナトリウムが生成されるのである。更にポリ塩化ビフェニル類化合物における主鎖結合についても超音波分解処理によって超音波自体の作用・超音波により惹起されたキャビテーションの発効及び摩擦力の作用とにより主鎖結合が切断されて、ベンゼン環は遊離をされるのである。更に遊離状態にされたすべてのベンゼン環についても強力な超音波を効率的に照射処理させ、強力な超音波分解処理によって超音波自体の作用・超音波により惹起されたキャビテーションの発効及び相対速度による摩擦力とにて、遊離状態にされたすべてのベンゼン環においては強力な超音波分解処理における酸化作用によってベンゼン環が開裂され、不飽和ジカルボン酸によるムコン酸が生成されるのである。更にポリ塩化ビフェニル類化合物に対して超音波分解処理の完結させた処理液を超音波分解処理装置のシステム外に摘出処理させるのである。次にポリ塩化ビフェニル類化合物に対して未分解による部分を分解処理させるため、ポリ塩化ビフェニル類化合物に対する超音波分解処理の完結させた処理液を超音波分解処理装置より摘出処理させ、チタン製による紫外線分解処理槽内に導入させて、更にナトリウムアルコラートまたは金属ナトリウムの定量を被処理液に注入添加させ、次に紫外線分解処理の速度を加速させるため、光電導性を保有している二酸化チタンの定量を添加させ、高真空・冷却処理による低温との状態を持続させておき、紫外線分解処理槽の下部における超音波発振装置により強力な調音波を被処理液に対して発振させ、強力な超音波による振動を付加させて、激しいミクロ的な攪拌作用を付与させる各種に対する処理条件下により、高圧水銀ランプまたは高圧キセノンランプを冷却装備させているランプハウスユニットより熱線の少ない紫外線を放射させ、被処理液に対して紫外線を照射により紫外線分解処理させて、紫外線分解処理によって被処理液に含有しているポリ塩化ビフェニル類化合物の未分解による部分の分子に対して紫外線を照射処理させ、光化学反応を惹起されて、基底状態におけるポリ塩化ビフェニル類化合物の未分解による分子においては紫外線の照射処理によって生じる紫外線光の作用により、基底状態におけるポリ塩化ビフェニル類化合物の未分解による分子に関与する電子において、紫外線光における高エネルギーの電磁波によって生じる光子エネルギーを吸収されることにより、電子がポリ塩化ビフェニル類化合物の未分解による分子内において、より高いエネルギー準位に遷移される際に、ポリ塩化ビフェニル類化合物の未分解による分子については電子的な光励起状態になり、分子内に励起エネルギーを得ることによって、分子においては活性化の状態になるのであり、活性化された状態のポリ塩化ビフェニル類化合物の未分解による分子が他のポリ塩化ビフェニル類化合物の未分解による分子に作用をして、励起エネルギーを授与させる反応により自動連鎖反応を次々と進行され、励起エネルギーを他の分子に放出させ授与させて失活状態になり再度基底状態に復帰するのであるが、基底状態におけるポリ塩化ビフェニル類化合物の未分解による分子に対して紫外線を照射処理させて、ポリ塩化ビフェニル類化合物の未分解による分子については紫外線による高エネルギーの吸収により、ポリ塩化ビフェニル類化合物の未分解による分子においては励起されて高いエネルギーの状態になって、光励起エネルギーを得ることにより、活性化されて励起状態になり、励起状態になると同時にポリ塩化ビフェニル類化合物の未分解による分子に対する側鎖結合により、側鎖に結合されている塩素分子においては急速に解離状態が惹起され遊離された状態になるのであり、遊離状態になったすべての塩素分子については紫外線分解処理の着手以前において被処理液に予め注入添加させていたナトリウムアルコラートまたは金属ナトリウムによるナトリウム分子とが結合され塩化ナトリウムが生成されるのであり、ポリ塩化ビフェニル類化合物に対して超音波分解処理を経過させ、更に紫外線分解処理をさせた後において、完璧にポリ塩化ビフェニル類化合物に対する分解処理を完結できるのである。従ってポリ塩化ビフェニル類化合物に対する分解処理において、単独による分解処理装置については完全な分解処理ができないのであり、超音波分解処理及び紫外線分解処理とを複合的に併用させた分解処理方法を採り入れているため、完璧にポリ塩化ビフェニル類化合物に対する分解処理を完結できるのである。次にポリ塩化ビフェニル類化合物に対して完璧に分解処理が完結させた後の処理液を紫外線分解処理装置よりシステム外に摘出処理させ、溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを分別処理させるために、溶媒及びポリ塩化ビフェニル類化合物による分解残留物とを含有している処理液を真空蒸留処理槽内に導入させて、被処理液を真空蒸留処理させるのであり、真空蒸留処理槽内における被処理液に含有している溶媒において、高真空による状態の処理条件下により、溶媒の沸点温度以上に昇進処理させ、溶媒を溶媒蒸気の状態にさせて、更に溶媒蒸気を溶媒の沸点温度以下に冷却処理させ、被処理液に含有していた溶媒を回収処理させて、真空蒸留処理させた後に真空蒸留処理槽内に残留されているポリ塩化ビフェニル類化合物による分解残留物を真空蒸留処理装置のシステム外に摘出処理させるのである。次にポリ塩化ビフェニル類化合物による分解残留物において油分を含有している場合には油分を除去処理させるため、ポリ塩化ビフェニル類化合物による分解残留物を分離処理槽内に導入させ、更にノルマルヘキサンの定量をポリ塩化ビフェニル類化合物による分解残留物に対して注入添加させて、高真空・冷却処理による低温とに対する状態を持続させ、分離処理槽の下部における超音波発振装置によって、強力な超音波をポリ塩化ビフェニル類化合物による分解残留物及びノルマルヘキサンとを含有している被処理液に対して発振させ、強力な超音波により被処理液を振動させて、強力な超音波により激しいミクロ的な攪拌作用を付与させる状態に対する各種の処理条件下によって、ポリ塩化ビフェニル類化合物による分解残留物に含有していた油分をノルマルヘキサンに抽出処理させ、次に溶媒における溶解度・沸点及び比重による差異を利用して分離処理させるために、油分及びノルマルヘキサンに対して難溶解性によるフルフラールの定量を被処理液に注入添加させて、被処理液を溶媒分離処理させ完璧に分離処理させた後において、分離処理に関与したすべての装置を停止させ、分離処理装置を静置させて、被処理液を比重の差異により総体的に上層・下層の２層部分に分離処理され、上層部分においてはノルマルヘキサン及び油分との混合液、下層部分においてはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液とに分離処理された状態になるのである。更に境界面の位置を検出処理させた後に、分離処理槽内の２層部分に分離処理された２種類の各々混合液を分離処理装置のシステム外に各々別個に摘出処理させるのである。次に分離処理装置のシステム外に各々別個に摘出処理させた２種類の混合液に対して分別処理させるため、再度真空蒸留処理させるのであるが、予め真空蒸留処理槽において２槽に分割装備させておき、真空蒸留処理槽における片方の槽内においてはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液、また他方の槽内にはノルマルヘキサン及ぶ油分との混合液を各々別個に導入させ、２種類の混合液に対するノルマルヘキサン及びフルフラールによる溶媒において沸点温度の差異により、真空蒸留処理槽における２槽について各々槽内による２種類の混合液を同時に真空蒸留処理させ、各々別個の槽内に収納させている２種類の混合液において、各々に含有しているノルマルヘキサン及びフルフラールによる溶媒については同時に２種類の混合液に対する真空蒸留処理により、沸点温度の差において分留処理させ、最初においてはノルマルヘキサン、次にはフルフラールと順次溶媒を回収処理させて、２種類の混合液に対する真空蒸留処理を完結させた後において、真空蒸留処理槽における２槽について各々別個の槽内に油分及びポリ塩化ビフェニル類化合物による分解残留物とが残留されている状態になるのである。次に真空蒸留処理槽において各々別個の槽内に残留されている油分及びポリ塩化ビフェニル類化合物による分解残留物とを真空蒸留処理装置のシステム外に各々別個の状態によって摘出処理させるのである。更に真空蒸留処理により回収処理させた各種の溶媒についてはポリ塩化ビフェニル類化合物を連続的に分解処理させるため、各種の溶媒を再度循環使用させるのである。次に回収処理させた油分及びポリ塩化ビフェニル類化合物による分解残留物については再度利用させ、更に再度利用できない部分については焼却処理装置により焼却処理をさせるのである。
（実施例）本発明によるポリ塩化ビフェニル類化合物に対して分解処理をさせる場合において、実施例により詳細について説明をすると下記の通りである。トランスにおける内部に収納されていたポリ塩化ビフェニル類化合物を含有しているトランス油（絶縁油）について、トランスの内部より器具の外部に摘出処理させ、次に摘出処理させたトランス油に対してチタン製による抽出処理槽内に導入させて、抽出処理槽の最上部をチタン製による上部板のセットにより完全に閉塞させ、抽出処理槽内を完璧な密閉状態にさせて、更に薬品用流量制御装置連動定量ポンプの作動により、トランス油に対してイソプロピルアルコールを１：１の容量比における割合によって、定量を抽出処理槽内におけるトランス油に注入添加させ、次に抽出処理装置のシステム外における真空ポンプを作動させて、抽出処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせ、更にデジタル真空一定装置により高真空の状態を持続させておき、次に抽出処理装置のシステム外における水冷却装置及び冷却水循環ポンプとを作動させて、抽出処理槽の外側に接触装着させている水冷ジャケット内において冷却処理させた冷却水を流動循環させ、抽出処理槽内における被処理液を冷却処理させ温度調節器により、温度を調整させて、抽出処理槽内における被処理液の温度について０〜４°Ｃによる低温の状態を持続させるのである。次に抽出処理槽の下部において超音波発振装置を接触装着させておき、抽出処理装置のシステム外における超音波発生装置及び超音波電力計を作動させて、超音波の発振出力を調整させ、超音波発振装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μ、強度１．０Ｗ／ｃｍ^２による強力な超音波を抽出処理槽内の下部より被処理液に対して発振させて、抽出処理槽内における被処理液に対して強力な超音波による振動を付与させ、被処理液については強力な超音波により激しいミクロ的な攪拌作用を付加させる状態における各種の処理条件下によって、ポリ塩化ビフェニル類化合物に対する抽出処理を促進させ、完全に抽出処理をさせるための抽出処理時間においては１０〜１５分間の処理により、完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。次にポリ塩化ビフェニル類化合物を含有しているコンデンサーについて、外装部品を除去処理させ、摘出処理させたポリ塩化ビフェニル類化合物を含有しているコンデンサー本体においては全体的にアスファルト状に固結化されているため、破砕処理装置または粉砕処理装置により、固結化されているコンデンサー本体を０．５〜１．０μによる微細な状態に粉化処理させ、粉化処理させた後において微粉状にさせたコンデンサーによる微粉をチタン製による抽出処理槽内に導入させて、抽出処理槽の最上部をチタン製による上部板のセットにより完全に閉塞させ、抽出処理槽内を完璧な密閉状態にさせて、更に薬品用流量制御装置連動定量ポンプを作動させ、コンデンサーによる微粉に対してイソプロピルアルコールを１：１の容量比における割合により、定量を抽出処理槽内におけるコンデンサーによる微粉に対して注入添加させ、次に前記のトランス油におけるポリ塩化ビフェニル類化合物に対する抽出処理の状態と同様な抽出処理における処理条件下により、抽出処理槽内における被処理液に対して強力な超音波による振動を付与させ、強力な超音波により激しいミクロ的な攪拌作用を付加させる状態によって、ポリ塩化ビフェニル類化合物に対する抽出処理を促進させ、完全に抽出処理させるための抽出処理時間については１５〜２０分間の処理によって、コンデンサーによる微粉より完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。次に抽出処理に関与させたすべての装置を停止させた後において、抽出処理の完結させた処理液を抽出処理槽内より摘出処理させて真空濾過処理槽内に導入させ、真空濾過処理装置により被処理液を真空濾過処理させて、完全にポリ塩化ビフェニル類化合物に対する抽出処理を完結させるのである。なお、濾過処理後における残留物については再度イソプロピルアルコールにより洗浄処理させた後において、焼却処理装置により焼却処理をさせるのであり、また洗浄処理において使用させたイソプロピルアルコールについては連続的にポリ塩化ビフェニル類化合物に対する抽出処理させるため再度溶媒として使用させるのである。次にポリ塩化ビフェニル類化合物を含有しているノーカーボン紙（感圧紙）・紙製品について、ノーカーボン紙及び紙製品をシュレッダーによって、細い線上に切断処理させ、更に切断処理させたノーカーボン紙及び紙製品をチタン製による抽出処理槽内に導入させて、抽出処理槽の最上部をチタン製による上部板のセットにより完全に閉塞させて、抽出処理槽内を完璧な密閉状態にさせて、次に薬品用流量制御装置連動定量ポンプを作動させ、切断処理させたノーカーボン紙及び紙製品に対してイソプロピルアルコールまたはアセトンを１：１の容量比における割合により、定量を抽出処理槽内におけるノーカーボン紙及び紙製品に対して注入添加させ、更に前記のトランス油におけるポリ塩化ビフェニル類化合物に対する抽出処理の状態と同様な抽出処理における処理条件下により、抽出処理槽内の被処理液・紙片に対して下部より強力な超音波による振動を付与させ、強力な超音波により激しいミクロ的な攪拌作用を付加させる状態によって、ポリ塩化ビフェニル類化合物に対する抽出処理を促進させ、完全に抽出処理をさせるための抽出処理時間については９〜１５分間の処理によって、細い線上に切断処理させたノーカーボン紙及び紙製品より完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。次に抽出処理に関与させたすべての装置を停止させた後において、抽出処理の完結された処理液を抽出処理槽内より摘出処理させて真空濾過処理槽内に導入させ、真空濾過処理装置により被処理液を真空濾過処理させて、完全にポリ塩化ビフェニル類化合物に対する抽出処理を完結させるのである。なお、抽出処理槽における残留物及び濾過処理後における残留物に対する紙片等については再度イソプロピルアルコールまたはアセトンに対する溶媒によって洗浄処理させた後において、焼却処理装置により焼却処理をさせるのであり、また洗浄処理において使用させたイソプロピルアルコールまたはアセトンについては連続的にポリ塩化ビフェニル類化合物に対する抽出処理をさせるため再度溶媒として使用させるのである。次にポリ塩化ビフェニル類化合物を含有している土壌または底質について、ポリ塩化ビフェニル類化合物の含有している土壌または底質をチタン製による抽出処理槽内に導入させ、抽出処理槽の最上部をチタン製による上部板のセットにより完全に閉塞させて、抽出処理槽内を完璧に密閉状態にさせ、更に薬品用流量制御装置連動定量ポンプを作動させて、土壌または底質に対してノルマルヘキサンを１：２の容量比における割合により、定量を抽出処理槽内における土壌または底質に対して注入添加させ、次に前記のトランス油におけるポリ塩化ビフェニル類化合物に対する抽出処理の状態と同様な抽出処理における処理条件下により、抽出処理槽内の被処理液・土石類に対して下部より強力な超音波による振動を付与させ、強力な超音波により激しいミクロ的な攪拌作用を付加させる状態によって、ポリ塩化ビフェニル類化合物に対する抽出処理を促進させ、完全に抽出処理をさせるための抽出処理時間において１０〜１５分間の処理により、土壌または底質より完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。更に抽出処理に関与させたすべての装置を停止させた後において、抽出処理の完結させた処理液を抽出処理槽内より摘出処理させて真空濾過処理槽内に導入させ、被処理液を真空濾過処理させて、真空濾過処理させた後において、土壌または底質に含有していた水分によって生じた抽出水分を処理液より分離処理させ、分離処理させた抽出水分については廃棄処理させて、水分を含有していない状態の抽出処理液にさせ完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。なお、抽出処理槽内における残留物及び濾過処理後における残留物に対する土類または石類については再度ノルマルヘキサンによって洗浄処理させた後に廃棄処理させ、また洗浄処理に使用させたノルマルヘキサンは連続的にポリ塩化ビフェニル類化合物を抽出処理させるために、再度溶媒として使用させるのである。次に被覆電線においてポリ塩化ビフェニル類化合物を含有しているゴムまたは合成樹脂類による被覆部分について、内部の電線を除去処理させ被覆部分だけの状態にさせて、ポリ塩化ビフェニル類化合物の含有している被覆部分をチタン製による抽出処理槽内に導入させ、抽出処理槽の最上部をチタン製による上部板のセットによって完全に閉塞させて、抽出処理槽内を完璧な密閉状態にさせ、更に薬品用流量制御装置連動定量ポンプを作動させて、被覆部分に対してジメチルフォルムアミドを１：２の容量比における割合により、定量を抽出処理槽内における被覆部分に対して注入添加させ、次に前記のトランス油におけるポリ塩化ビフェニル類化合物に対する抽出処理の状態と同様な溶解処理における処理条件下により、抽出処理槽内における被覆部分及びジメチルフォルムアミドとを下部より強力な超音波による振動を付与させ、強力な超音波により激しいミクロ的な攪拌作用を付加させる状態によって、ゴムまたは合成樹脂類における被覆部分に対して溶解処理を促進させ、被覆部分についてジメチルフォルムアミドにより完全に溶解処理させるための溶解処理時間おいては４０〜５０分間の処理により、完璧に被覆部分の溶解処理を完結できるのである。更に溶解処理に関与させたすべての装置を停止させた後において、溶解処理の完結させた溶解処理液を抽出処理槽内より摘出処理させて真空濾過処理槽内に導入させ、真空濾過処理装置により溶解処理液を真空濾過処理させて、真空濾過処理の完結させた後における溶解処理液を再度抽出処理槽内に導入させ、次に他の薬品用流量制御装置連動定量ポンプを作動させて、溶解処理液に対してジメチルフォルムアミドに不溶解性でありポリ塩化ビフェニル類化合物について溶解抽出性が保有しているノルマルヘキサンを１：１の容量比における割合により、ノルマルヘキサンの定量を抽出処理槽内における被覆部分の溶解処理液に対して注入添加させ、前記のトランス油におけるポリ塩化ビフェニル類化合物に対する抽出処理の状態と同様な抽出処理における処理条件下により、抽出処理槽内における被処理液に対して抽出処理槽の下部より強力な超音波による振動を付与させ、強力な超音波により激しいミクロ的な攪拌作用を付加させる状態によって、ポリ塩化ビフェニル類化合物に対する抽出処理を促進させるのであり、抽出処理槽内におけるポリ塩化ビフェニル類化合物を含有している被覆部分の溶解処理液による被処理液に対して注入添加させたノルマルヘキサンにより、ポリ塩化ビフェニル類化合物に対する抽出処理をさせ、各種の処理条件及び超音波の振動・攪拌作用下により被処理液に含有しているポリ塩化ビフェニル類化合物に対する抽出処理を促進させて、完全に抽出処理をさせるための抽出処理時間において１０〜１５分間の処理によって、被覆部分の溶解処理液における被処理液より完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。更に抽出処理に関与させたすべての装置を停止させた後において、抽出処理装置を静置させることにより、抽出処理槽内における被処理液については総体的に上層部分及び下層部分との２層部分とに分離処理されるのであり、上層部分においてはノルマルヘキサン及びポリ塩化ビフェニル類化合物とによる溶解処理液、また下層部分にはジメチルフォルムアミド及びゴムまたは合成樹脂類とによる溶解処理液とに分離処理をされるのである。次に境界両面に対する位置を検出処理させた後において、抽出処理槽内における下層部分に位置しているジメチルフォルムアミド及びゴムまたは合成樹脂類とによる溶解処理液の部分を抽出処理槽内より抽出処理装置のシステム外に摘出処理させて除去処理させ、抽出処理槽内においてはノルマルヘキサンによるポリ塩化ビフェニル類化合物に対する抽出処理液を残留させ、完璧にポリ塩化ビフェニル類化合物に対する抽出処理を完結できるのである。なお、抽出処理装置のシステム外に摘出処理させたジメチルフォルムアミド及びゴムまたは合成樹脂類との溶解処理液の部分については真空蒸留処理装置により真空蒸留処理させ、ジメチルフォルムアミドを回収処理させて再度被覆部分に対する溶解処理に使用させるのであり、また残留されたゴムまたは合成樹脂類における残留物については再度利用させるのである。次にポリ塩化ビフェニル類化合物に対する抽出処理を完結させた抽出処理液については超音波分解処理をさせるために、抽出処理液を超音波分解処理用の移送ポンプによって、チタン製による超音波分解処理槽内に導入させ、更に薬品用流量制御装置連動定量ポンプを作動させて、ポリ塩化ビフェニル類化合物を分解処理させるための化学的な反応について必要なナトリウムアルコラートまたは金属ナトリウムの全量に対して２／３の分量における割合によって、定量を超音波分解処理槽内における被処理液に対して注入添加させ、次に超音波分解処理装置のシステム外における真空ポンプを作動させて、超音波分解処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせておき、更にデジタル真空一定装置によって高真空における状態を持続させるのである。次に超音波分解処理槽における外側に水冷ジャケットを接触装着させておき、超音波分解処理装置のシステム外における水冷却装置を作動させ、水を冷却処理させて、冷却処理させた冷却水について超音波分解処理装置のシステム外における冷却水循環ポンプを作動させ、水冷ジャケット内に冷却水を導入させて、水冷ジャケット内において冷却水を流動循環させ、超音波分解処理槽内における被処理液を冷却水により冷却処理させて、超音波分解処理槽内における被処理液の温度状態を温度調節器により、温度を調整させ、超音波分解処理槽内における被処理液の温度について０〜４°Ｃによる低温の状態を持続させるのであり、高真空・冷却処理による低温の状態における処理条件下により、超音波分解処理槽内における被処理液に対して被処理循環ポンプを作動させて、低流速による状態において循環させるのであるが、被処理液に対する流速については被処理液を強力な超音波に照射処理させ、照射反応時間に対応させる流速が必要であり、強力な超音波による照射反応時間に対応させるための流速についてはできる限り低流速にさせ、最高の流速においては１０〜１５ｍ／分の低流速による循環処理の状態にさせるのである。低流速により循環処理をさせて再度超音波分解処理槽内に返送導入させるのであり、更に被処理液を循環処理させる工程中において、中間による任意の位置に超音波分解処理部を装備させておき、超音波分解処理部内に循環処理させている被処理液を低流速により導入させ、超音波分解処理部内においては低流速によって循環処理させている被処理液の進行流に対して直角の状態において超音波発振装置を接触装着させておき、超音波発生装置及び超音波電力計とにより、超音波の発振出力について調整させ、超音波発振装置より実効出力１，２００Ｗ、周波数（振動数）１９、５ＫＨｚ、振幅６０〜８０μ及び超音波の強度５０Ｗ／ｃｍ^２による強力な超音波を循環処理させている被処理液に対して発振させ、被処理液においては強力な超音波の照射処理により激しく振動をさせて、超音波自体による作用及び超音波によって多量に発生されたキャビテーションの発効により、被処理液における溶媒及びポリ塩化ビフェニル類化合物との間において相対速度が生じて、両者との間に対して摩擦力が作用され、摩擦力の作用によってポリ塩化ビフェニル類化合物による結合分子鎖において主鎖結合及び側鎖結合が盛んに切断処理され、更にベンゼン環についても開裂をされて、被処理液に含有しているポリ塩化ビフェニル類化合物においては次第に分解処理をされるのであり、被処理液に対して超音波分解処理を着手させた時点より２０〜２３分間後における時点において、被処理液については急激に粘土が降下した状態になり、粘土が降下した時点においてポリ塩化ビフェニル類化合物が超音波により分解処理された状態になったのであり、ポリ塩化ビフェニル類化合物に対して超音波分解処理を着手させた時点より２５〜３０分間後において超音波分解処理を完結させるのである。次に超音波分解処理に対して完結させた処理液において、含有していたポリ塩化ビフェニル類化合物については未分解による部分を含有しているのである。更にポリ塩化ビフェニル類化合物に対して完璧に分解処理をさせるために、超音波分解処理槽内における超音波分解処理を完結させた処理液については超音波分解処理槽の下部に装着させている処理液排出電磁弁を作動させて開放状態にさせ、処理液排出電磁弁と同調をさせている紫外線分解処理用の移送ポンプにより、超音波分解処理に対して完結させた処理液を超音波分解処理装置のシステム外に摘出処理させると同時に紫外線分解処理用の移送ポンプによって、紫外線分解処理槽内に導入させるのである。次に紫外線分解処理槽内に導入させた被処理液に対する紫外線分解処理について、被処理液に含有しているポリ塩化ビフェニル類化合物の未分解による部分を完璧に分解処理させるために、超音波分解処理の完結させた処理液を紫外線分解処理槽内に導入させ、更に第１薬品用流量制御装置連動定量ポンプを作動させて、ポリ塩化ビフェニル類化合物を完璧に分解処理させるための化学的な反応に必要なナトリウムアルコラートまたは金属ナトリウムの全量に対する残部の１／３における分量の割合により、定量を紫外線分解処理槽内の被処理液に対して注入添加させ、次に紫外線分解処理について反応速度を加速させるために、第２薬品添加量制御装置連動スクリュー定量供給装置を作動させ、被処理液に対して光電導性を有する二酸化チタンを１〜４％の容量比における割合により、二酸化チタンの定量を紫外線分解処理槽内の被処理液に導入添加させて、更に紫外線分解処理装置のシステム外における真空ポンプを作動させ、紫外線分解処理槽内を５×１０^−４Ｔｏｒｒによる高真空の状態にさせて、デジタル真空一定装置により高真空の状態を持続させ、次に紫外線分解処理槽の外側に水冷ジャケットを接触装着させておき、紫外線分解処理装置のシステム外における水冷却装置を作動させ、水を冷却処理させて、冷却処理させた冷却水に紫外線分解処理装置のシステム外における冷却水循環ポンプを作動させ、水冷ジャケット内に冷却水を導入させて、水冷ジャケット内を冷却水が流動循環させ、紫外線分解処理槽内の被処理液を冷却水により冷却処理させて、紫外線分解処理槽内の被処理液による温度を温度調節器の温度調整により、被処理液において０〜４°Ｃによる低温の状態を持続させ、更に紫外線分解処理槽の下部に超音波発振装置を接触装着させておき、超音波発生装置及び超音波電力計とにより、超音波の発振出力を調整させ、超音波発生装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μ、強度１．０Ｗ／ｃｍ^２による強力な超音波を紫外線分解処理槽内の被処理液に対して発振させ、被処理液の下部より強力な超音波による振動を付与させて、被処理液に強力な超音波により激しいミクロ的な攪拌作用を付加させ、紫外線分解処理反応を促進させるのである。次に石英ガラス製によるランプハウスユニットにおいて、最内部の位置に分解物が最初に含有している塩素１％に対して１００Ｗの割合による定格電力５ＫＷの高圧水銀ランプまたは高圧キセノンランプを挿入させ、高圧水銀ランプまたは高圧キセノンランプを冷却処理させるために、石英ガラスにより作製させた二重の円形状態による隔壁による隔壁によって空間を装備させておき、ランプハウスユニットの最内部に挿入させた高圧水銀ランプまたは高圧キセノンランプの管外壁と石英ガラスによる円形状態の隔壁との空間を装備させておき、ランプハウスユニットのシステム外における消費電力２５０Ｗ、叶出圧力４Ｋｇ／ｃｍ^２、叶出空気量９５ｌ／分による空気ポンプを作動させ、装備させている空冷ジャケットに対して外気を導入させ、空冷ジャケットの他端より導入させた外気と共に高圧水銀ランプまたは高圧キセノンランプにより発熱された熱量を装置の外部に排出拡散させて、高圧水銀ランプまたは高圧キセノンランプを気流により冷却処理させ、更に気流にて冷却処理させる空冷ジャケットの外側に石英ガラス製による純水冷却ジャケットを溶着装備させて、ランプハウスユニットのシステム外における純水冷却装置及びイオン交換器を作動させ、高純度の純水を冷却処理させて、高純度の純水において２〜３°Ｃによる低温の状態に冷却処理をさせ、装置のシステム外における叶出量３０ｌ／分による冷却純水循環ポンプを作動させて、高純度の冷却純水を純水冷却ジャケット内に導入させ、純水冷却ジャケット内の高純度による冷却純水を流動循環処理させて、高圧水銀ランプまたは高圧キセノンランプより放出された熱量及び放射された熱線とを冷却処理させ、ランプハウスユニットに対して装置の外部より空気を導入させて排出させまた高純度の冷却純水を循環処理させて、気流及び冷却純水により高圧水銀ランプまたは高圧キセノンランプを冷却処理させるのであり、結果としてランプハウスユニットより熱線の少ない紫外線を放射処理させるのである。次にランプハウスユニットを紫外線分解処理槽内における被処理液の液面より上部または被処理液中に装備させるのであり、また紫外線分解処理槽による内壁面及び外壁面とランプハウスユニットとの接触面に対してシリコンゴムなどのゴム類またはプラスチック樹脂類によるシール材によって完全に密閉状態にさせ、高真空の状態に耐性を有し外気に対して吸引性がない完全な密閉状態にさせる必要があり、紫外線分解処理槽内における被処理液に対してランプハウスユニットより熱線の少ない紫外線を照射処理させ、紫外線分解処理反応を惹起させる状態の各種における処理条件化により、ポリ塩化ビフェニル類化合物の未分解による部分に対して紫外線分解処理反応をさせ、被処理液に含有しているポリ塩化ビフェニル類化合物の未分解による部分に対して次第に紫外線分解処理反応によって分解処理をさせるのであり、被処理液に含有しているポリ塩化ビフェニル類化合物の未分解による部分を完全に分解処理させるための紫外線分解処理時間については紫外線分解処理反応に対して着手させた時点より２７〜３０分間の紫外線分解処理によって、完璧にポリ塩化ビフェニル類化合物に対する分解処理を完結できるのである。更にポリ塩化ビフェニル類化合物については紫外線分解処理反応を経過させて完璧に分解処理を完結させた結果、分解残留物においては塩化ナトリウム・ムコン酸及び微少量のビフェニルが生成されるのである。次に紫外線分解処理槽内における分解残留物を含有している処理液については紫外線分解処理槽の下部に装着させている処理液排出電磁弁を作動させて開放状態にさせ、同調をさせた真空蒸留処理用の移送ポンプにより、紫外線分解処理させポリ塩化ビフェニル類化合物に対して完璧に分解処理させ完結させた処理液を紫外線分解処理装置のシステム外に摘出処理させると同時に移送ポンプによって処理液を真空蒸留処理槽内に導入させるのである。次に真空蒸留処理槽内に導入させた被処理液に含有している溶媒及びポリ塩化ビフェニル類化合物による分解残留物とに対して各々を分別処理させるための真空蒸留処理について、紫外線分解処理を完結させた処理液に対して真空蒸留処理槽内に導入させ、真空蒸留処理装置のシステム外における真空ポンプにより、真空蒸留処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせて、更にデジタル真空一定装置によって高真空の状態を持続させ、次に真空蒸留処理槽の下部に加熱処理装置を接触装着させておき、加熱処理装置により真空蒸留処理槽内における被処理液に含有している溶媒及びポリ塩化ビフェニル類化合物による分解残留物とに対して間接的に加熱処理をさせ、被処理液による溶媒については高真空の状態において沸点以上の温度に対する第１温度調節器によって温度を調整させて、持続させる処理条件下により、被処理液について加熱処理をさせ、被処理液に含有している溶媒を高真空の状態における沸点以上の温度に対する加熱処理をさせて、被処理液による溶媒については溶媒の状態により溶媒蒸気の状態になり、真空蒸留処理装置内を上昇されるのである。更に真空蒸留処理装置内の上部に装備させている冷却処理装置に対する蛇管によって、溶媒における沸点以下の温度を第２温度調節器により温度状態の調整をさせて冷却処理させ、真空蒸留処理装置内を上昇された溶媒蒸気については溶媒における沸点以下の温度により冷却処理させて、溶媒蒸気を凝縮処理させて液化させ、真空蒸留処理装置内の冷却部における冷却用蛇管の下部に装備させている凝縮液滴下受納回収器によって、凝縮液における溶媒を回収処理させて収納させ、回収処理させた溶媒を第１電磁弁における自動的な開閉作動によって、開放状態にさせ真空蒸留処理装置のシステム外における回収溶媒貯留タンク内に導入させ、更に回収処理させた溶媒を回収溶媒貯留タンクの下部に装備させている第２電磁弁における自動的な開閉作動によって、開放状態にさせ回収処理させた溶媒を真空蒸留処理装置のシステム外に摘出処理させることにより、完璧に溶媒の回収処理を完結させるのである。次に真空蒸留処理によって真空蒸留処理槽内における被処理液に含有しているすべての溶媒に対して回収処理を完結させた後において、真空蒸留処理に関与させたすべての装置を停止させ、真空蒸留処理槽内の残留物を冷却処理させて、完璧に真空蒸留処理を完結させた後に、真空蒸留処理槽内に残留されているポリ塩化ビフェニル類化合物による分解残留物を冷却処理後において、真空蒸留処理装置のシステム外に摘出処理をさせるのである。次に摘出処理させた分解残留物に対して油分が含有している場合には分解残留物より油分を除去処理させる分離処理について、分解残留物を分離処理槽内に導入させ、更に分離処理槽の上部に対して上部板により閉塞させ分離処理槽内を密閉状態にさせておき、次に第１薬品用流量制御装置連動定量ポンプを作動させ、ポリ塩化ビフェニル類化合物による分解残留物に対してノルマルヘキサンを１：２の容量比における割合により、ノルマルヘキサンの定量をポリ塩化ビフェニル類化合物による分解残留物に対して注入添加させ、次に分離処理装置のシステム外における真空ポンプにより、分離処理槽内において５×１０^−４Ｔｏｒｒによる高真空の状態にさせて、更にデジタル真空一定装置によって高真空の状態を持続させるのである。次に分解処理槽における外側に対して水冷ジャケットを接触装着させ装備させておき、分離処理装置のシステム外における水冷却装置を作動させ、水を冷却処理させて、冷却処理させた冷却水については分離処理装置のシステム外における冷却水循環ポンプを作動させ、水冷ジャケット内に冷却水を導入させて、水冷ジャケット内において冷却水を流動循環処理させ、水冷ジャケット内に導入をさせた冷却水によって、分離処理槽内におけるノルマルヘキサン及びポリ塩化ビフェニル類化合物による分解残留物とを含有している被処理液を冷却処理させ、分離処理槽内における被処理液の温度状態を温度調節器により、温度を調整させて、被処理液の温度において０〜４°Ｃによる低温の状態を持続させるのである。更に分離処理槽の下部に超音波発振装置を接触装着させておき、超音波発生装置及び超音波電力計とにより、超音波の発振出力を調整させ、超音波発振装置より実効出力６００Ｗ、周波数（振動数）２６ＫＨｚ、振幅２００μ、超音波の強度１．０Ｗ／ｃｍ^２による強力な超音波を被処理液に対して発振させて、分離処理槽内における被処理液に対して分離処理槽内の下部より強力な超音波による振動を付与させ、被処理液において強力な超音波により激しいミクロ的な攪拌作用を付加させる状態の各種における処理条件下により、ポリ塩化ビフェニル類化合物による分解残留物に含有している油分をノルマルヘキサンによって抽出処理させて、ポリ塩化ビフェニル類化合物による分解残留物より油分を抽出処理させるための抽出処理時間については１５〜２０分間における抽出処理により、ポリ塩化ビフェニル類化合物による分解残留物に含有している油分を完璧に抽出処理させ、抽出処理を完結させた後において、抽出処理に関与させたすべての装置を停止させるのである。次に第２薬品用流量制御装置連動定量ポンプを作動させ、ポリ塩化ビフェニル類化合物による分解残留物に対してノルマルヘキサン及び油分について難溶解性による溶媒のフルフラールを１：１の容量比における割合により、フルフラールの定量を分離処理槽内における被処理液に対して注入添加させて、次に再度すべての装置を作動させ、前記と同様な処理条件下による状態にまで復帰をさせて、被処理液において高真空・冷却処理による低温の状態における処理条件下により、強力な超音波による振動及び激しいミクロ的な攪拌作用を付加させ、被処理液に対して完全に溶媒分離処理させるための溶媒分離処理時間については１０〜１５分間による溶媒分離処理をさせた後に、溶媒分離処理に関与させたすべての装置を停止させ、分離処理装置を静置させた後において、分離処理槽内における被処理液については比重差によって上層部分及び下層部分との２層部分に分離処理をされるのである。上層部分においてはノルマルヘキサン及び油分による混合液であり、また下層部分にはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液とに分離処理をされるのである。更に２層部分に分離処理された被処理液において分離処理槽よりシステム外に装備されているガラス管測定装置または導電率液面測定装置による境界面検出装置によって２層部分に対する境界面の位置を検出測定処理させ、次に上層部分及び下層部分に分離処理された処理液に含有しているノルマルヘキサン及びフルフラールにより溶媒を分留処理させるため再度真空蒸留処理槽内に導入させるのであるが、予め真空蒸留処理槽を２槽に分割装備させておき、分離処理槽の下部に装着させている処理液排出電磁弁を作動させて開放状態にさせ、処理液排出電磁弁の作動に同調させた真空蒸留処理用の移送ポンプを作動させて、分離処理槽内において下層部分に位置しているフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液を最初に真空蒸留処理槽における片方の槽内に導入させ、フルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液を真空蒸留処理槽における片方の槽内に導入処理させ完結させた後において、移送ポンプ及び処理液排出電磁弁とを作動させ閉塞停止の状態にさせるのである。更に分離処理槽内において上層部分に位置していたノルマルヘキサン及び油分による混合液を真空蒸留処理槽における他方の槽内に導入させるために、再度分離処理槽の下部による処理液排出電磁弁を作動させて開放状態にさせ、同時に処理液排出電磁弁の作動状態に同調をさせている真空蒸留処理用の移送ポンプを作動させて、ノルマルヘキサン及び油分による混合液を真空蒸留処理槽における他方の槽内に導入させ、ノルマルヘキサン及び油分による混合液を分離処理槽内より真空蒸留処理槽における他方の槽内に導入処理させた後において、真空蒸留処理用移送ポンプ及び分離処理用処理液排出電磁弁とを作動させ閉塞停止の状態にさせるのである。次に再度真空蒸留処理槽において分割装備させている２槽の各々別個による槽内に導入させた２種類の混合液に対して同時に真空蒸留処理させ、ノルマルヘキサン及びフルフラールによる沸点の温度差［ノルマルヘキサン、沸点６８．７°Ｃ（７６０ｍｍＨｇ）、フルフラール、沸点１６１．８°Ｃ（７６０ｍｍＨｇ）］によって、最初においてはノルマルヘキサン、次にはフルフラールを真空蒸留処理により回収処理させるのである。更に真空蒸留処理によって完璧にノルマルヘキサン及びフルフラールによる２種類の溶媒を回収処理させ完結させた後において、真空蒸留処理槽を分割装備させた２槽に対して各々別個の槽内に油分及びポリ塩化ビフェニル類化合物による分解残留物との２種類が残留されるのであり、真空蒸留処理槽を分割装備させている２槽に対して各々別個の槽内について残留された油分及びポリ塩化ビフェニル類化合物による分解残留物とにおいては各々別個における状態によって真空蒸留処理装置のシステム外に摘出処理をさせるのである。次にポリ塩化ビフェニル類化合物による分解残留物に対して油分が含有してない場合においては分離処理をさせる必要がないのである。更に２種類の混合液を真空蒸留処理装置によって真空蒸留処理させ、分留処理により溶媒を回収処理させた後において、回収処理させた各種の溶媒については連続的にポリ塩化ビフェニル類化合物を分解処理させるので各種における溶媒の各々については個々に必要な時点により再度使用させるのである。次に分離処理の工程を経過させ真空蒸留処理させた後において、真空蒸留処理槽内より摘出処理させた油分及びポリ塩化ビフェニル類化合物による分解残留物とを各々別個に回収処理させ、油分については熱媒体油・潤滑油等に再度利用させて、また分解残留物については再度分離処理させ塩化ナトリウム等の部分を抽出処理させて工業的に再度利用させるのである。更に再度利用できない部分については焼却処理装置により焼却処理させるのである。
（発明の効果）本発明によるポリ塩化ビフェニル類化合物に対する分解処理方法及び分解処理装置に従うと、ポリ塩化ビフェニル類化合物に対する分解処理においては物理的・化学的分解処理とを併用させた分解処理の方法を採り入れており、抽出処理・超音波分解処理・紫外線分解処理・真空蒸留処理・分離処理による分解処理方法を順次各々における分解処理装置によって分解処理させ、ポリ塩化ビフェニル類化合物に対して非常に効率的に分解処理ができ１００％による分解率が確実に実現できるのであり、ポリ塩化ビフェニル類化合物に対して完璧に分解処理を効率的に完結できるのである。次にポリ塩化ビフェニル類化合物を含有している対象品類よりポリ塩化ビフェニル類化合物に対する抽出処理について、抽出処理槽内に導入させた被処理物に対してイソプロピルアルコール・アセトン及びノルマルヘキサンによる抽出溶媒を注入添加させ、短時間により完璧にポリ塩化ビフェニル類化合物の抽出処理を完結できるのである。次にポリ塩化ビフェニル類化合物に対する分解処理による超音波分解処理について、超音波分解処理槽内に導入させた抽出処理が完結の被処理液にナトリウムアルコラートまたは金属ナトリウムの定量を注入添加させ、被処理液に対して大きな加速度の有する強力な超音波を発振させて、ポリ塩化ビフェニル類化合物に対して超音波自体の作用及び超音波によって発生されたキャビテーションの発効とにより、被処理液を構成している溶媒及びポリ塩化ビフェニル類化合物との間において相対速度が生じ、両者との間に対して摩擦力が作用されて、摩擦力の作用によってポリ塩化ビフェニル類化合物による結合分子鎖において主鎖結合及び側鎖結合とが盛んに切断され、解離され遊離状態にされた塩素分子と予め被処理液に注入添加させていたナトリウムアルコラートまたは金属ナトリウムによるナトリウム分子とが結合されて塩化ナトリウムが生成されるのであり、また解離され遊離状態にされたベンゼン環についてもベンゼン環は開裂処理されてムコン酸が生成されるのである。更に超音波分解処理による反応を完結させた処理液についてはポリ塩化ビフェニル類化合物の未分解による部分が含有しているので、ポリ塩化ビフェニル類化合物を完璧に分解処理させるために、処理液を紫外線分解処理させるのである。次にポリ塩化ビフェニル類化合物に対して完璧に分解処理させる紫外線分解処理について、紫外線分解処理槽内に導入させた被処理液にナトリウムアルコラートまたは金属ナトリウムの定量を注入添加させ、更に光電導性を保有している二酸化チタンの定量を導入添加させて、被処理液に対して強力な紫外線を照射処理させ紫外線分解処理によって、ポリ塩化ビフェニル類化合物の未分解による部分の分子については基底状態を維持されていた分子が強力な紫外線の照射処理により、紫外線光による光子エネルギーの保持している高エネルギーを基底状態の分子に吸収されて、ポリ塩化ビフェニル類化合物の未分解による分子内においてはより高いエネルギー準位に遷移される際に分子は光励起状態になり、分子内に光励起エネルギーを得ることによって活性化の状態になるのであり、活性化された状態になったポリ塩化ビフェニル類化合物の未分解による分子が他の未分解による分子に作用をして、未分解による分子が他の未分解による分子に励起エネルギーを授与させる反応により自動連鎖反応が次々に進行され、他の未分解による分子に励起エネルギーを放出させた後において、再度元の基底状態に復帰されて失活の状態になるのである。次に励起エネルギーを授与された分子においては励起状態になると同時にポリ塩化ビフェニル類化合物の未分解による分子の結合分子鎖に対する側鎖結合によって結合されている塩素分子は解離の状態にされ遊離状態にされるのである。更に遊離状態にされたすべての塩素分子については予め被処理液に注入添加させていたナトリウムアルコラートまたは金属ナトリウムによるナトリウム分子とが結合されて塩化ナトリウムが生成されるのであり、光化学反応によってすべての塩素分子については消滅された状態になるのである。従って紫外線分解処理装置によってポリ塩化ビフェニル類化合物の未分解による分子に対して紫外線分解処理させ完璧に分解処理を完結させるのであり、ポリ塩化ビフェニル類化合物を完璧に分解処理させた後において、分解残留物については塩化ナトリウム・ムコン酸及び微少量のビフェニルとが含有されているのである。更に処理液を構成している溶媒及び分解残留物とを分別処理させるため真空蒸留処理させるのである。次に紫外線分解処理を完結させた処理液に含有している溶媒及び分解残留物とを分別処理させるための真空蒸留処理について、真空蒸留処理槽内に導入させた溶媒及び分解残留物とを含有している被処理液を高真空の状態により溶媒の沸点以上に対する温度状態において間接加熱処理させ、溶媒蒸気の状態によって真空蒸留処理槽内を上昇されて、上部の位置に装備させている冷却装置により溶媒の沸点以下に対する温度状態において冷却処理させ、溶媒蒸気を凝縮処理させ液化状態にさせて、凝縮液における溶媒を真空蒸留処理装置のシステム外に摘出処理させて回収処理させ、真空蒸留処理槽内における被処理液に対して真空蒸留処理させ完璧に含有している溶媒を回収処理させて、溶媒及び分解残留物とを分別処理させた後において、真空蒸留処理槽内に対して残留されている分解残留物を真空蒸留処理装置のシステム外に摘出処理させるのである。更に摘出処理させた分解残留物に対して油分が含有している場合には油分を完全に除去処理させる必要があるために、分解残留物より油分を分離処理させるのである。次に真空蒸留処理装置より摘出処理させた分解残留物に含有している油分に対する分離処理について、分離処理槽内に導入させたポリ塩化ビフェニル類化合物による分解残留物に対してノルマルヘキサンの定量を注入添加させ、分解残留物に含有している油分をノルマルヘキサンに溶解抽出処理させ、更に分解残留物より油分を完璧に抽出処理させ完結させた後において、被処理液にフルフラールの定量を注入添加させ、被処理液に対して溶媒分離処理をさせて、完璧に被処理液に対する溶媒分離処理が完結させた後に分離処理装置を静置させることにより、被処理液においては比重の差によって上層部分及び下層部分との２層部分に分離処理をされ、上層部分についてはノルマルヘキサン及び油分による混合液、また下層部分にはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液とに分離処理をされるのである。次に両境界面の検出測定処理をさせた後において、２種類の各々混合液に含有しているノルマルヘキサン及びフルフラールにおける溶媒を蒸留処理させ各々の混合液について分別処理させるために、処理液を再度真空蒸留処理槽内に導入させるが、予め真空蒸留処理槽内において２槽に分割装備をさせておき、真空蒸留処理槽における片方の槽内についてはフルフラール及びポリ塩化ビフェニル類化合物による分解残留物との混合液を導入させ、また他方の槽内にはノルマルヘキサン及び油分との混合液を導入させるのである。次に真空蒸留処理槽における２槽に分割装備させた槽内に２種類の混合液を各々別個に導入させ各々を分別処理させるための真空蒸留処理について、真空蒸留処理槽における２槽の各々別個に導入させた２種類の各々混合液においては各々に対する混合液について含有をしているノルマルヘキサン及びフルフラールにおける溶媒に対して沸点の温度差により、分留処理による真空蒸留処理をさせ、最初においてはノルマルヘキサン、次にはフルフラールを真空蒸留処理により回収処理させるのである。更にノルマルヘキサン及びフルフラールにおける２種類の溶媒に対して完璧に回収処理を完結させた後において、真空蒸留処理槽に対して分割装備させている各々別個の２槽内に油分及びポリ塩化ビフェニル類化合物による分解残留物とが残留されるのである。次に分割装備させている各々別個の２槽内に残留された油分及びポリ塩化ビフェニル類化合物による分解残留物を真空蒸留処理装置のシステム外に個々の槽より各々別個に摘出処理させるのである。なお、ポリ塩化ビフェニル類化合物による分解残留物に対して油分を含有していない場合においては分離処理させる工程が必要なのである。更に真空蒸留処理装置によって真空蒸留処理させ、分留処理により溶媒を回収処理させた後において、回収処理させた各種の溶媒については連続的にポリ塩化ビフェニル類化合物を分解処理させるために、各種における溶媒の各々については個々に必要な時点により再度使用させるのである。次に真空蒸留処理槽において分割装備させている２槽に対して個々の真空蒸留処理槽より各々別個に摘出処理させ回収処理させた油分については工業的な分野の熱媒体油・潤滑油等に再度利用させるのであり、また回収処理させた分解残留物については再度分離処理させるて塩化ナトリウム等の部分を抽出処理させ工業的に再度利用できるのである。更に再度利用できない部分については焼却処理装置により２次公害が発生しない状態にて焼却処理をさせるのである。従ってポリ塩化ビフェニル類化合物に対する分解処理においては抽出処理・超音波分解処理・紫外線分解処理については完璧な分解処理における工程であり、また真空蒸留処理・分離処理については分解残留物に対して再度利用させるためのリサイクルに対する工程である。更にポリ塩化ビフェニル類化合物に対する分解処理については分解処理による工程を順次各々における分解処理装置によって分解処理を経過させ完結により、ポリ塩化ビフェニル類化合物に対して１００％による完璧な分解処理を完結させ無公害化できるのである。次に本発明によるポリ塩化ビフェニル類化合物に対する分解処理については時間当り多量の分解処理ができる工業的な規模の分解処理であり、工業的な規模による分解処理装置及び付属装置の分解処理に必要な装置をトレーラー車に搭載させてセットさせ、車上において分解処理をさせるために、分解処理に対する移動性が得られるので特定危険物質であるポリ塩化ビフェニル類化合物を運搬移動させて分解処理させる必要がないので、ポリ塩化ビフェニル類化合物を移動させる危険がなくなり、更に工業的に多量の分解処理による周辺の環境についても２次公害の発生は皆無である。
【図面の簡単な説明】
【第１図】本発明の実施に対する態様を示す工程説明図下記における各図面については本発明による装置の１例である。
【第２図】抽出処理装置に対する各器具類の配置図
【第３図】抽出処理装置における正面図
【第４図】抽出処理装置における左側面図
【第５図】抽出処理装置における右側面図
【第６図】超音波分解処理装置に対する各器具類の配置図
【第７図】超音波分解処理装置における正面図
【第８図】超音波分解処理装置における左側面図
【第９図】超音波分解処理装置における右側面図
【第１０図】紫外線分解処理装置に対する各器具類の配置図
【第１１図】紫外線分解処理装置における正面図
【第１２図】紫外線分解処理装置における左側面図
【第１３図】紫外線分解処理装置における右側面図
【第１４図】紫外線分解処理装置に対するランプハウスユニットの側面図
【第１５図】紫外線分解処理装置に対するランプハウスユニットのＡ−Ａ断面図
【第１６図】真空蒸留処理装置に対する各器具類の配置図
【第１７図】真空蒸留処理装置における正面図
【第１８図】真空蒸留処理装置における左側面図
【第１９図】真空蒸留処理装置における右側面図
【第２０図】分離処理装置に対する各器具類の配置図
【第２１図】分離処理装置における正面図
【第２２図】分離処理装置における左側面図
【第２３図】分離処理装置における右側面図
【符号の説明】
抽出処理装置
１ 抽出処理槽
２ 抽出処理用の上部板
３ 抽出処理用の薬品貯留タンク
４ 抽出処理用の薬品用流量制御装置連動定量ポンプ
５ 抽出処理用の真空ポンプ
６ 抽出処理用のデジタル真空一定装置
７ 抽出処理用の水冷ジャケット
８ 抽出処理用の水冷却装置
９ 抽出処理用の冷却水循環ポンプ
１０ 抽出処理用の水貯留タンク
１１ 抽出処理用の超音波発振装置
１２ 抽出処理用の超音波発生装置
１３ 抽出処理用の超音波電力計
１４ 抽出処理用の処理液排出電磁弁
９０ 抽出処理用の温度調節器
超音波分解処理装置
１５ 超音波分解処理用の移送ポンプ
１６ 超音波分解処理槽
１７ 超音波分解処理用の薬品貯留タンク
１８ 超音波分解処理用の薬品用流量制御装置連動定量ポンプ
１９ 超音波分解処理用の真空ポンプ
２０ 超音波分解処理用のデジタル真空一定装置
２１ 超音波分解処理用の水冷ジャケット
２２ 超音波分解処理用の水冷却装置
２３ 超音波分解処理用の冷却水循環ポンプ
２４ 超音波分解処理用の水貯留タンク
２５ 超音波分解処理用の被処理液循環ポンプ
２６ 超音波分解処理用の超音波分解処理部
２７ 超音波分解処理用の超音波発振装置
２８ 超音波分解処理用の超音波発生装置
２９ 超音波分解処理用の超音波電力計
３０ 超音波分解処理用の処理液排出電磁弁
９１ 超音波分解処理用の温度調節器
紫外線分解処理装置
３１ 紫外線分解処理用の移送ポンプ
３２ 紫外線分解処理槽
３３ 紫外線分解処理用の第１薬品貯留タンク
３４ 紫外線分解処理用の第１薬品用流量制御装置連動定量ポンプ
３５ 紫外線分解処理用の第２薬品貯留タンク
３６ 紫外線分解処理用の第２薬品用添加量制御装置連動スクリュー定量供給装置
３７ 紫外線分解処理用の真空ポンプ
３８ 紫外線分解処理用のデジタル真空一定装置
３９ 紫外線分解処理用の水冷ジャケット
４０ 紫外線分解処理用の水冷却装置
９２ 紫外線分解処理用の温度調節器
４１ 紫外線分解処理用の冷却水循環ポンプ
４２ 紫外線分解処理用の水貯留タンク
４３ 紫外線分解処理用の超音波発振装置
４４ 紫外線分解処理用の超音波発生装置
４５ 紫外線分解処理用の超音波電力計
４６ 紫外線分解処理用のランプハウスユニット
４７ 高圧水銀ランプまたは高圧キセノンランプ
４８ ランプ冷却処理用の空冷ジャケット
４９ ランプ冷却処理用の空気ポンプ
５０ ランプ冷却処理用の水冷ジャケット
５１ ランプ冷却処理用の純水冷却装置
５２ ランプ冷却処理用のイオン交換器
５３ ランプ冷却処理用の純水貯留タンク
５４ 紫外線分解処理用の処理液排出電磁弁
真空蒸留処理装置
５５ 真空蒸留処理用の移送ポンプ
５６ 真空蒸留処理槽
５７ 真空蒸留処理用の真空ポンプ
５８ 真空蒸留処理用のデジタル真空一定装置
５９ 真空蒸留処理用の加熱装置
６０ 真空蒸留処理用の第１温度調節器
６１ 真空蒸留処理用の溶媒蒸気凝縮部
６２ 真空蒸留処理用の冷却用蛇管
６３ 真空蒸留処理用の冷却部
６４ 真空蒸留処理用の水冷却装置
６５ 真空蒸留処理用の冷却水循環ポンプ
６６ 真空蒸留処理用の水貯留タンク
６７ 真空蒸留処理用の第２温度調節器
６８ 真空蒸留処理用の凝縮液滴下受納回収器
６９ 真空蒸留処理用の第１電磁弁
７０ 真空蒸留処理用の回収溶媒貯留タンク
７１ 真空蒸留処理用の第２電磁弁
分離処理装置
７２ 分離処理槽
７３ 分離処理用の第１薬品貯留タンク
７４ 分離処理用の第１薬品用流量制御装置連動定量ポンプ
７５ 分離処理用の上部板
７６ 分離処理用の真空ポンプ
７７ 分離処理用のデジタル真空一定装置
７８ 分離処理用の水冷ジャケット
７９ 分離処理用の水冷却装置
８０ 分離処理用の冷却水循環ポンプ
８１ 分離処理用の水貯留タンク
８２ 分離処理用の超音波発振装置
８３ 分離処理用の超音波発生装置
８４ 分離処理用の超音波電力計
８５ 分離処理用の第２薬品貯留タンク
８６ 分離処理用の第２薬品用流量制御装置連動定量ポンプ
８７ 分離処理用の境界面検出装置
８８ 分離処理用の処理液排出電磁弁
８９ 分離処理用の温度調節器(Field of Industrial Use) The present invention relates to a decomposition treatment method and a decomposition treatment apparatus for polychlorinated biphenyl compounds which are environmental pollutants. More specifically, each bond molecular chain in the polychlorinated biphenyl compounds is not a laboratory scale, but an industrial scale, extraction process, ultrasonic decomposition process, ultraviolet decomposition process, vacuum distillation process, and separation process. In the unit of the apparatus, each of these treatments is automatically and sequentially progressed, each of the binding molecular chains is cleaved, and the polychlorinated biphenyl compound is completely decomposed to make it a non-polluting substance and its mechanism The present invention relates to a decomposition processing apparatus.
(Conventional technology) Regarding the decomposition treatment of polychlorinated biphenyl compounds, which are extremely troublesome environmental pollutants, in the technologies for various conventional decomposition treatment methods, incineration treatment methods by various combustion treatment devices, biological by yeast and bacteria The treatment method, the adsorption treatment method with activated carbon, the chemical treatment method with chemicals, and the physical treatment method by irradiating with radiation are the decomposition treatment methods. It is a decomposition method that does not deviate from the experimental and research stage with a device of a reasonable scale, and for the decomposition method that can be carried out on a practical industrial scale, a method with a complete certainty of the decomposition method has been established. It is not done, and there is a problem in terms of appropriate practicality. The solution processing method is not practical at present.
(Problems to be solved by the invention) In the conventional decomposition method for polychlorinated biphenyl compounds, when the incineration process is performed at a relatively low temperature when the incineration process is performed by various combustion processing apparatuses, Thermal decomposition of polychlorinated biphenyl compounds will produce extremely toxic polychlorinated dibenzofurans, which are combustion intermediates. Therefore, the furnace temperature is at an extremely high temperature of about 1,300 to 2,000 ° C. is required. In addition, the furnace temperature distribution must be equalized. It is important to eliminate local low-temperature conditions, but it is impossible to maintain the temperature distribution in the furnace by equalizing the temperature distribution in the high temperature, and it is impossible to maintain the state of the furnace body due to the heat resistance to extremely high temperature conditions. There is also a problem with the material. Because of these problems, various incineration treatment methods have difficulties, and thus an incineration treatment method that is immediately ready for perfect practicality has not been developed. For this reason, the installation of an incineration treatment apparatus for polychlorinated biphenyl compounds is accompanied by various social difficulties and has not been put into practical use. Next, in order to decompose the polychlorinated biphenyl compounds by the biological treatment method in yeast and bacteria, a culture period of 7 to 10 days is required. Therefore, a large amount of equipment is required, and the degradation rate is as low as 30 to 40%, which is a difficulty in biological treatment methods for degradation treatment of polychlorinated biphenyl compounds by yeast and bacteria. The current situation is that it has not been put into practical use. Furthermore, when polychlorinated biphenyl compounds are decomposed in the adsorption treatment method using activated carbon, the adsorption treatment capacity is about 0.1 mg / l, and the adsorption treatment capacity is limited, and the adsorption removal rate is not so high. A large amount of activated carbon is required because it cannot be expected efficiently. In addition, sufficient attention must be paid to regeneration, incineration, and disposal of activated carbon after adsorption treatment. Since this is a difficulty with the adsorption treatment method in the decomposition treatment of the polychlorinated biphenyl compounds with activated carbon, it has not been put into practical use. Next, when polychlorinated biphenyl compounds are decomposed by chemical treatment methods in chemicals, compounds that are chemically stable and inert with respect to polychlorinated biphenyl compounds, and have high drug resistance Therefore, the decomposition treatment is difficult, and in the hydrothermal treatment method under high pressure and high temperature, a polychlorinated biphenyl compound is obtained by adding a sodium hydroxide aqueous solution or hydrogen peroxide water by heat treatment at 300 to 400 ° C. under 200 to 300 atm. However, in some cases, the treatment may be performed at 500 atm or higher, and there is a problem in various facilities for performing the decomposition treatment under these treatment conditions. It is dangerous because it must be done. Since this is a difficulty in the chemical treatment method for the decomposition treatment of polychlorinated biphenyl compounds with chemicals, it has not been put into practical use. Furthermore, in the case of physical treatment in the case of irradiation with radiation, protective measures against radiation are necessary, and the degradation rate for polychlorinated biphenyl compounds in irradiation with radiation is as low as about 50%, which is dangerous. However, it is not very efficient. Since this is a difficult point in the physical treatment method for the decomposition treatment of the polychlorinated biphenyl compounds when irradiated with radiation, it has not been put into practical use. Accordingly, the degradation treatment methods for these various polychlorinated biphenyl compounds are each accompanied by drawbacks and disadvantages, and these degradation treatment methods are in the range of the experimental research stage with a laboratory-scale apparatus. There is no practically established method of decomposition treatment that does not take off, and there are various problems in terms of appropriate practicality, so that a perfect polychlorinated biphenyl compound that can be implemented with industrial scale equipment The present situation is that the decomposition method has not been put to practical use, but the present invention overcomes the respective drawbacks and difficulties in the conventional techniques for various decomposition methods for polychlorinated biphenyl compounds by the present invention. A treatment that can establish a decomposition treatment method and can decompose a large amount of polychlorinated biphenyl compounds on a practical and industrial scale. Actuates the location, by carrying out efficient and perfect decomposition treatment, for the purpose of providing a cracking process and decomposition treating apparatus for polychlorinated biphenyls compound is of the present invention has been completed.
(Means for Solving the Problems) As a result of earnest research on the decomposition treatment method for polychlorinated biphenyl compounds in the present inventor, various products containing polychlorinated biphenyl compounds which are environmental pollutants. If the polychlorinated biphenyl compound is extracted by an extraction treatment device, and the polychlorinated biphenyl compound is further subjected to an ultrasonic decomposition treatment device, an ultraviolet decomposition treatment device, a vacuum distillation treatment device, and a separation treatment device, It has been found that polychlorinated biphenyl compounds can be decomposed, and based on this finding, the present invention has been completed. Next, the polychlorinated biphenyl compound that is an environmental pollutant is not a single compound, but there are about 210 kinds of compounds depending on the combination of positions in chlorination that is theoretically possible. There is a species. Therefore, the polychlorinated biphenyl compounds are a mixture of these compounds, and in these mixtures, all chlorine molecules are bonded. Furthermore, when polychlorinated biphenyl compounds contained in various products are extracted, ethyl alcohol and methyl alcohol are very slow in the extraction solvent for the polychlorinated biphenyl compounds. In isopropyl alcohol, the numerical values for the solubility parameter and dielectric constant are approximate values, and the size is similar in terms of molecular size and intermolecular interaction. It possesses properties that are more soluble than other solvents for chlorine-based compounds, and in particular has the highest properties for solubility in polychlorinated biphenyl compounds compared to other solvents. It has been found that isopropyl alcohol in the secondary alcohol having an isopropyl group is most suitable as an extraction solvent for the polychlorinated biphenyl compounds, and the performance is maximized in extraction efficiency. Therefore, in the extraction process for polychlorinated biphenyl compounds, the best extraction process can be performed efficiently by adding isopropyl alcohol. Next, transformer oil containing polychlorinated biphenyl compounds with chlorination numbers 5 and 6 and chlorine content of 54% and 60% extracted from the transformer in the electrical equipment is polychlorinated from the transformer oil. In order to extract the biphenyl compounds, trans oil is introduced into the extraction processing tank, and a fixed amount of isopropyl alcohol in a volume ratio of 1: 1 is injected and added to the trans oil. The inside of the extraction tank is 5x10 by the vacuum pump outside. ^-4 The high vacuum state of Torr is maintained, and the high vacuum state is further maintained with a digital vacuum constant device, and the liquid to be processed is cooled by circulation of the cooled cooling water to maintain the low temperature state of 0 to 4 ° C. Under the processing conditions, an ultrasonic wave generator with an effective output of 600 W, a frequency (frequency) of 26 KHz, and an amplitude of 200 μ is oscillated with respect to the liquid to be processed by the ultrasonic oscillator attached in contact with the lower part of the extraction processing tank. Ultrasonic vibration is added to give a strong microscopic stirring action by ultrasonic waves, and the ultrasonic wave accelerates the extraction process for the liquid to be processed, which is an efficient function. The polychlorinated biphenyl compound is extracted. Next, with regard to capacitors in electrical equipment, polychlorinated biphenyl compounds having a chlorination number of 3 as the main component, which was removed by removing the exterior part and rarely 4, and a chlorine content of 42% as the main component and rarely 48%. About the condenser which contains, in the condenser solidified in the asphalt form, it is pulverized into a fine powder state of about 0.5 to 1.0 μm by a crushing device, and the fine powder is introduced into the extraction treatment tank, A fixed amount of isopropyl alcohol is injected into a fine powder condenser at a ratio in a volume ratio of 1: 1, and in the same manner as in the case of the above transformer oil, depending on the processing conditions in a low temperature state by high vacuum and cooling treatment. The ultrasonic wave is oscillated in the same manner as described above by the ultrasonic oscillator attached to the lower part of the extraction processing tank, and the polysalt is generated by the ultrasonic vibration. The biphenyls compound with the extraction process, further to the introduction into the vacuum filtration apparatus, is cause to extraction treatment with polychlorinated biphenyls compound by filtration. Next, carbonless paper (pressure sensitive paper) and paper products containing polychlorinated biphenyl compounds having a chlorination number of 3 and a chlorine content of 42% are cut into thin lines with a shredder, By introducing linear strips of paper into the extraction processing tank, the ratio of 1: 1 to the volume ratio of isopropyl alcohol or acetone to the carbon strips and paper products of the linear strips, As in the case of the transformer oil described above, the ultrasonic oscillation device attached to the lower part of the extraction processing tank is in contact with the lower portion of the extraction processing tank under the processing conditions in the low temperature state by high vacuum and cooling processing as in the case of the transformer oil. Oscillates in an ultrasonic state, and the polychlorinated biphenyl compound is extracted by microscopic stirring using the vibration of the ultrasonic wave. It is of letting extraction chloride biphenyls compound. In addition, after the polychlorinated biphenyl compounds are subjected to extraction treatment and subjected to filtration treatment, the residual paper is further washed once or twice with isopropyl alcohol or acetone, and then the polychlorinated biphenyl compounds. After assessing the persistence of the paper, the papers are incinerated. Next, the soil and sediment containing the polychlorinated biphenyl compounds are introduced into the extraction treatment tank, the moisture contained in the soil and sediment is considered, and the extraction solvent is polychlorinated with normal hexane. The biphenyl compound is extracted and processed by adding a fixed amount of normal hexane to the soil and sediment at a ratio of 1: 2 in a volume ratio. Depending on the processing conditions in the low temperature state due to the cooling treatment, the ultrasonic oscillation device that is in contact with the lower part of the extraction treatment tank oscillates ultrasonic waves in the same state as described above, and vibrates with ultrasonic waves to make microscopic stirring. After the polychlorinated biphenyl compound is extracted by the action, and further introduced into the vacuum filtration device and subjected to the filtration treatment, water is present when water is present in the lower layer portion. It was removal treatment is to be extracted handle polychlorinated biphenyls compound. In addition, after the polychlorinated biphenyl compounds are extracted and subjected to filtration treatment, and the residual debris is further washed once or twice with normal hexane, the persistence of the polychlorinated biphenyl compounds is increased. After the assessment, it is discarded. Next, about the covering part of the insulating material in the covered electric wire containing the polychlorinated biphenyl compound, after the electric wire is removed, the covering part is introduced into the extraction processing tank, and the solvent for dissolving the covering part is used. The dimethylformamide is dissolved with dimethylformamide, and a fixed amount of dimethylformamide is injected into the coated part at a ratio of 1: 2 in a volume ratio, and the high vacuum is applied as in the case of the above-mentioned transformer oil.・ According to the processing conditions in the low temperature state by the cooling process, ultrasonic waves in the same state as described above are oscillated by the ultrasonic oscillator attached to the lower part of the extraction processing tank, and are vibrated by ultrasonic waves. After the coating portion is completely dissolved by stirring, it is further introduced into a vacuum filtration device and filtered, and then filtered again. The solution is introduced into the extraction treatment tank, and normal hexane is injected and added at a ratio of 1: 1 in the volume ratio with respect to the dissolution treatment solution of the coating portion, and again by the same high vacuum and cooling treatment as described above. The polychlorinated biphenyl compounds are completely extracted in normal hexane under the treatment conditions that cause ultrasonic vibrations at low temperatures. Further, by stopping all extraction processing devices and attached devices and leaving them to stand, the dissolution treatment liquid of the coated portion is separated, so that the dissolution treatment solution portion is removed, and polychlorinated biphenyls It completes the compound extraction process. Next, regarding the extraction processing apparatus for polychlorinated biphenyl compounds, the extraction object is introduced into the titanium extraction processing tank (1), and the upper plate (2) made of titanium is set on the upper part of the extraction processing tank. The inside is sealed, and the extraction solvent is injected into the extraction target from the chemical storage tank (3) for extraction processing, and the fixed amount of the extraction solvent is injected into the extraction target by the chemical flow control device linked quantitative pump (4) for extraction processing. Next, 5 × 10 5 in the extraction processing tank by the vacuum pump (5) for extraction processing outside the system of the extraction processing apparatus. ^-4 The high vacuum state in Torr is maintained, and the high vacuum state is automatically maintained by the digital vacuum constant apparatus (6) for extraction processing. Further, a water cooling jacket (7) for extraction processing is attached to the outside of the extraction processing tank, and the water is cooled by the water cooling device (8) for extraction processing outside the system of the extraction processing device. The cooling water is introduced into the water cooling jacket by the cooling water circulation pump (9) for extraction processing, the liquid to be processed in the extraction processing tank is cooled by cooling water, and the temperature controller (90) for extraction processing is used. The temperature is adjusted, and the low temperature state of 0 to 4 ° C. is maintained at the temperature of the liquid to be treated. Further, the treated water after the cooling treatment is discharged from the water cooling jacket, stored in the extraction water storage tank (10), introduced again into the water cooling device, and the cooling water is circulated. Next, the ultrasonic oscillator (11) for extraction processing is attached in contact with the lower part of the extraction processing tank, and the ultrasonic generator (12) for extraction processing and the ultrasonic power meter (13) for extraction processing are used. By adjusting the ultrasonic oscillation output, the ultrasonic oscillation device oscillates an ultrasonic wave with an effective output of 600 W, a frequency (frequency) of 26 KHz, and an amplitude of 200 μ to vibrate the liquid to be processed in the extraction processing tank with the ultrasonic wave. And the extraction treatment apparatus completes the extraction treatment of the polychlorinated biphenyl compound, thereby operating the extraction treatment liquid discharge solenoid valve (14) attached to the lower portion of the extraction treatment tank to open it. The extraction processing liquid is extracted outside the system of the extraction processing apparatus. Next, with respect to the decomposition treatment of polychlorinated biphenyl compounds by ultrasonic treatment, the extraction treatment of the polychlorinated biphenyl compounds is completed by completing the extraction treatment of the polychlorinated biphenyl compounds and the ultrasonic treatment of the extracted solution of the polychlorinated biphenyl compounds extracted from the extraction treatment apparatus In a liquid to be treated containing a polychlorinated biphenyl compound introduced into the ultrasonic decomposition tank made of titanium by a transfer pump for treatment, and further introduced into the ultrasonic decomposition tank, polychlorinated biphenyl Sodium alcoholate (sodium ethylate → sodium ethoxide and sodium methylate → sodium methoxide) or sodium in a quantity of 2/3 relative to the total amount of metallic sodium required for the chemical reaction to cause decomposition of the compounds Alcoholate or metallic sodium is injected and added, In order to improve the transmission of ultrasonic waves in the ultrasonic decomposition treatment tank and increase the efficiency of ultrasonic waves, a vacuum pump outside the system of the ultrasonic decomposition treatment apparatus 5 is used in the ultrasonic decomposition treatment tank. × 10 ^-4 A high vacuum state is generated by Torr, and a high vacuum state is maintained by a digital vacuum constant device. Next, a water cooling jacket is attached to the outside of the ultrasonic decomposition treatment tank, the water is cooled by a cooling device outside the ultrasonic decomposition treatment system, and the cooling water is introduced into the water cooling jacket by a circulation pump. Then, the liquid to be processed in the ultrasonic decomposition treatment tank is cooled, the temperature of the liquid to be processed is adjusted by a temperature controller, and the low temperature state of 0 to 4 ° C. is maintained. The treated water after cooling is discharged from the water cooling jacket, stored in the water storage tank, introduced again into the cooling device, and the cooling water is circulated. Next, the liquid to be treated is transferred and circulated at a low flow rate from the ultrasonic decomposition treatment tank by a liquid circulation pump to be treated. In order to sonicate the polychlorinated biphenyl compounds by circulating the water, it is necessary to change the flow rate to be transported and circulated depending on the amount of the liquid to be treated. When sonication treatment is performed, a decomposition reaction is induced in the polychlorinated biphenyl compound for each part in the liquid to be treated by circulating the liquid in the liquid to be treated and irradiating with ultrasonic waves. In the irradiation reaction time for the overall decomposition treatment of polychlorinated biphenyl compounds, it is necessary to irradiate with ultrasonic waves for 25 to 30 minutes. It was found by experiment Rukoto. Therefore, with regard to the circulation treatment for the liquid to be treated, in the case where the overall decomposition treatment of the polychlorinated biphenyl compounds is performed by ultrasonic irradiation, the state of the circulation treatment for the liquid to be treated is set in order to correspond to the irradiation reaction time by the ultrasonic wave. It is necessary to decide on the flow rate to be transferred. Next, the liquid to be treated is circulated from within the ultrasonic decomposition treatment tank by the liquid circulation pump to be treated, and the polychlorinated biphenyl compounds are irradiated with ultrasonic waves and transferred at a low flow rate for decomposition treatment. In the ultrasonic decomposition processing unit, the ultrasonic oscillation device is attached to the ultrasonic decomposition processing unit at a right angle to the traveling flow of the liquid to be processed. By adjusting the oscillation output of the sound wave, the effective output 1,200 from the ultrasonic oscillation device

980cm / sec for the acceleration of gravity ² Therefore, G = 1.118 × 10 ⁷ / 5980≈11,200. Therefore, by oscillating strong ultrasonic waves with a huge acceleration about 11,200 times the acceleration of gravity, and vigorously vibrating the liquid to be treated with strong ultrasonic waves, a large amount of cavitation is generated. Relative velocity is generated between the solvent and polychlorinated biphenyl compounds due to the action of ultrasonic waves and the effect of cavitation by ultrasonic waves. The main chain and side chain in the binding molecular chain of the polychlorinated biphenyl compound are actively cleaved and further cleaved in the benzene ring, so that the polychlorinated biphenyl compound is decomposed and again in the ultrasonic decomposition treatment tank By introducing the liquid to be processed at a low flow rate into the liquid, the liquid to be processed is circulated at a low flow rate and subjected to ultrasonic decomposition treatment, Li chloride biphenyl compound is being gradually decomposed,

GC-ECD (Gas Chromatograph with Electron Capture Type Detector) was used to measure the degradation rate for the degradation of polychlorinated biphenyl compounds by irradiating the polychlorinated biphenyl compounds with ultrasonic waves. It is a result, the treatment liquid is circulated at a low flow rate, irradiated with ultrasonic waves, and each part of each of the polychlorinated biphenyl compounds contained in the treatment liquid is decomposed, It has been proved by experiments that an irradiation time of ultrasonic waves of 25 to 30 minutes is necessary in the decomposition reaction processing time by the irradiation of ultrasonic waves with respect to the overall decomposition treatment of the polychlorinated biphenyl compounds. Even if the decomposition treatment is performed for 30 minutes or more in the reaction treatment, the decomposition rate by the same degree or more cannot be exhibited. Therefore, it is necessary to irradiate each part of the polychlorinated biphenyl compounds contained in the liquid to be treated effectively with ultrasonic waves for as long as possible with respect to the irradiation reaction time in contact with the ultrasonic waves. Therefore, in order to adapt to this, it was proved by experiments that circulation treatment was performed at a low flow rate, and that an irradiation reaction by ultrasonic waves was necessary in the overall decomposition treatment of the polychlorinated biphenyl compounds. Next, in the binding molecular chain of the polychlorinated biphenyl compound, the side chain of the chlorine molecule is cleaved by the frictional force in the ultrasonic decomposition treatment and the cavitation induced by the ultrasonic decomposition treatment and bonded to the side chain. Chlorine molecules are released, and all the released chlorine molecules are injected with sodium alcoholate (sodium ethyl acetate) before the polychlorinated biphenyl compounds are decomposed by ultrasonic waves. Sodium chloride is formed by the combination of sodium molecules with free sodium ethoxide and sodium methylate → sodium methoxide) or metallic sodium and all free chlorine molecules. Furthermore, the main chain bond in the binding molecular chain of the polychlorinated biphenyl compound is also broken by the frictional force by ultrasonic decomposition treatment and the cavitation induced by ultrasonic decomposition treatment, and the benzene ring is released. For all the benzene rings brought into the state, powerful ultrasonic waves are efficiently and most effectively irradiated, so that by the action of frictional force caused by strong ultrasonic waves and the action of cavitation induced by strong ultrasonic waves, The benzene ring that has been brought into the free state undergoes a powerful ultrasonic oxidation action that causes benzene to pass through phenol (hydroxybenzene), which is further oxidized from hydroquinone to quinone (benzoquinone), and then the oxidation action is promoted. The benzene ring is cleaved and cleaved, resulting in a linear unsaturated di A phosphate muconic acid (HOOCCH = CHCH = CHCOOH) is the is produced. Therefore, all the benzene rings brought into a free state are caused to oxidize by the action of frictional force caused by strong ultrasonic waves and the action of cavitation induced by strong ultrasonic waves. It is cleaved and cleaved to finally produce muconic acid (2.4-hexadienic acid). Next, regarding the ultrasonic decomposition processing apparatus in the ultrasonic decomposition processing, in the extraction processing liquid in which the extraction processing for the polychlorinated biphenyl compounds is completed, the ultrasonic decomposition processing made of titanium is performed by the transfer pump (15) for ultrasonic decomposition processing. Sodium alcoholate or metal is introduced into the tank (16) and further from sodium alcoholate (sodium ethylate → sodium ethoxide and sodium methylate → sodium methoxide) or chemical storage tank (17) for ultrasonic decomposition treatment in metallic sodium. Sodium is injected and added in a fixed amount to the liquid to be processed in the ultrasonic decomposition treatment tank by means of a chemical flow rate controller linked quantitative pump (18) for ultrasonic decomposition treatment. Next, a vacuum pump (19) for ultrasonic decomposition processing outside the system with respect to the ultrasonic decomposition processing device, 5 × 10 5 in the ultrasonic decomposition processing tank. ^-4 The high vacuum state is maintained by Torr, and the high vacuum state is maintained by the digital vacuum constant device (20) for ultrasonic decomposition. Next, a water cooling jacket (21) for ultrasonic decomposition treatment is attached in contact with the outside of the ultrasonic decomposition treatment tank, and a water cooling device for ultrasonic decomposition treatment outside the system (with respect to the ultrasonic decomposition treatment device ( 22) the water is cooled, and the cooling water is introduced into the water-cooling jacket by the cooling water circulation pump (23) for ultrasonic decomposition treatment to cool the liquid to be treated in the ultrasonic decomposition treatment tank. The low temperature state is maintained by adjusting the temperature of the low temperature state at 4 ° C. with the temperature controller (91) for ultrasonic decomposition treatment. Further, the treated water after cooling the liquid to be treated is discharged from the water-cooling jacket, the treated water is stored in the water storage tank (24) for ultrasonic decomposition treatment, and again introduced into the cooling device to be cooled. Is circulated. Next, the liquid to be treated is subjected to ultrasonic decomposition treatment from the ultrasonic decomposition treatment tank under the treatment conditions for maintaining the low temperature state by high vacuum and cooling treatment for the liquid to be treated in the ultrasonic decomposition treatment tank. The treatment liquid is circulated by the treatment liquid circulation pump (25), and each portion of the polychlorinated biphenyl compound contained in the treatment liquid is subjected to an ultrasonic irradiation reaction treatment for decomposition treatment. However, in order to adapt to this, the polychlorinated biphenyl compounds are decomposed depending on the flow rate of circulating the liquid to be treated under the treatment conditions at a low flow rate. Next, with respect to the irradiation treatment with ultrasonic waves, the liquid to be treated which is circulated under the processing conditions at a low flow rate is introduced into the ultrasonic decomposition processing section (26), and in the ultrasonic decomposition processing section, the polychlorinated biphenyl compounds are introduced. In a state perpendicular to the traveling flow in the liquid to be treated, an ultrasonic oscillator (27) for ultrasonic decomposition treatment is attached in contact with the ultrasonic generator (28 for ultrasonic decomposition treatment). ) And the ultrasonic power meter (29) for ultrasonic decomposition treatment, the ultrasonic oscillation output is adjusted, and the effective output is 1,200 W, the frequency (frequency) is 19.5 KHz, and the amplitude is 60 to 80 μm. , Ultrasonic intensity 50W / cm ² By oscillating powerful ultrasonic waves, the liquid to be treated is vibrated vigorously with strong ultrasonic waves depending on the processing conditions in a low temperature state by high vacuum and cooling treatment, and the action of ultrasonic friction force and strong super Because of the action of cavitation induced by sonic waves, polychlorinated biphenyl compounds are decomposed by an ultrasonic irradiation reaction treatment, and the liquid to be treated is again introduced into the ultrasonic decomposition treatment tank at a low flow rate and circulated. Yes, by subjecting the liquid to be treated to ultrasonic treatment and circulating treatment at a low flow rate, the polychlorinated biphenyl compounds contained in the liquid to be treated are gradually decomposed by powerful ultrasonic radiation treatment. . Next, the polychlorinated biphenyl compounds contained in the liquid to be treated are decomposed by ultrasonic treatment, and the treatment liquid that has been completely decomposed by ultrasonic waves is attached to the lower part of the ultrasonic decomposition tank. The processing liquid discharge solenoid valve (30) for ultrasonic decomposition processing is operated to open, and the processing liquid that has been completely decomposed by ultrasonic irradiation processing is removed from the system in the ultrasonic decomposition processing apparatus. In addition, in order to completely decompose the polychlorinated biphenyl compound, the processing solution extracted outside the system in the ultrasonic decomposition processing apparatus is subjected to ultraviolet decomposition processing. Next, with regard to the ultraviolet decomposition treatment for completely decomposing polychlorinated biphenyl compounds, the polychlorinated biphenyl compounds are irradiated with ultrasonic waves to complete the decomposing process, and the ultrasonic decomposing apparatus outside the system. In order to completely decompose the polychlorinated biphenyl compounds in the treatment liquid that also contains the undegraded portion of the polychlorinated biphenyl compounds that have been subjected to the ultrasonic treatment for the polychlorinated biphenyl compounds that have been extracted into By introducing a polychlorinated biphenyl compound with ultraviolet rays to the liquid to be treated introduced into the ultraviolet decomposition treatment tank made of titanium by a transfer pump for use in the ultraviolet decomposition treatment tank, Sodium alcoholate (sodium ethylate) required in chemical reaction for decomposition treatment Sodium ethoxide and sodium methylate → sodium methoxide) or sodium alcoholate or sodium metal in an amount of 1/3 of the remainder relative to the total amount of metallic sodium is injected and added to the liquid to be treated, and undecomposed in polychlorinated biphenyl compounds. In the case where the portion is subjected to irradiation reaction treatment with ultraviolet rays and subjected to decomposition treatment, in order to increase the reaction rate for the irradiation reaction treatment with ultraviolet rays, the titanium dioxide having photoelectric conductivity is 1 to 4% of the liquid to be treated. A vacuum pump outside the system of the UV decomposition processing system in order to introduce and add a fixed amount by the ratio in the volume ratio, and then to improve the UV transmittance in the UV decomposition treatment tank and also increase the efficiency due to UV rays In the UV decomposition tank 5 × 10 ^-4 A high vacuum is generated by Torr, and a high vacuum is maintained by a digital vacuum constant device. Next, in order to bring the liquid to be treated in the ultraviolet decomposition treatment tank into a low temperature state by the cooling treatment, a water cooling jacket is attached in contact with the outside of the ultraviolet decomposition treatment tank, and the water outside the system of the ultraviolet decomposition treatment apparatus is attached. Water is cooled by the cooling device, the cooled cooling water is introduced into the water cooling jacket by the cooling water circulation pump, and the liquid to be treated in the ultraviolet decomposition treatment tank is cooled by the cooling water in the water cooling jacket. The temperature of the treatment liquid is adjusted by a temperature controller, and the low temperature state of 0 to 4 ° C. is maintained in the cooled treatment liquid, and the treatment water after the treatment liquid is cooled. The water is discharged from the water cooling jacket, and the treated water is introduced into the water storage tank and stored, and then introduced into the cooling device again. Than is circulating. Next, an ultrasonic oscillator is attached to the lower part of the UV decomposition bath under the processing conditions in a low temperature state by high vacuum and cooling treatment, and the ultrasonic oscillation output is output by the ultrasonic generator and ultrasonic wattmeter. , By oscillating a powerful ultrasonic wave with an effective output of 600 W, a frequency (frequency) of 26 KHz, and an amplitude of 200 μm from the ultrasonic oscillator to the liquid to be processed, and vibrating the liquid to be processed with a strong ultrasonic wave, The chemical reaction is promoted by adding a vigorous microscopic stirring action by vigorous ultrasonic vibration. Next, in a quartz glass lamphouse unit that generates ultraviolet light, a double-tube jacket cooling method is used to insert a high-pressure mercury lamp or high-pressure xenon lamp that generates ultraviolet light inside the lamphouse unit, and both ends are fixed with quartz glass. The air pump is attached to the innermost space around the lamp and is equipped with an air cooling jacket made of quartz glass and a water cooling jacket made of pure water made of quartz glass on the outside. The external air is pumped and introduced into the air-cooling jacket, the heat generated by the lamp is forcibly cooled by the airflow, and the air after the lamp is cooled is discharged out of the system, and the UV decomposition process The pure water is cooled by a pure water cooling device outside the system. The cooled pure water, which has been passed through an ion exchanger and brought into a state of pure water at a high purity, is pumped and introduced into a water-cooled jacket made of pure water, and the cooled pure water forcibly generates heat from the lamp and heat rays from the lamp. The pure water after cooling is discharged from the water-cooled jacket with pure water, further introduced and stored in the pure water storage tank, and introduced again into the pure water cooling device. Cooling pure water is circulated, and the heat generated by the high-pressure mercury lamp or high-pressure xenon lamp and the heat rays emitted from the lamp are forcibly cooled by the airflow and cooling pure water, thereby suppressing the temperature rise due to ultraviolet rays. Therefore, it can emit ultraviolet rays with less heat rays than the lamp house unit. Next, the lamp house unit is fixedly mounted above the liquid surface of the liquid to be treated in the ultraviolet decomposition treatment tank or at a position in the liquid to be treated, and between the inner and outer walls of the ultraviolet decomposition treatment tank and the lamp house unit, In order to be able to withstand the high vacuum state in the UV decomposition treatment tank and to maintain an airtight state with no suction to the outside air, it is brought into close contact with a sealant made of rubber such as silicon rubber and plastic resins. It is necessary to irradiate the liquid to be treated in the ultraviolet decomposition treatment tank with ultraviolet rays emitted from a high-pressure mercury lamp or high-pressure xenon lamp. However, the polychlorinated biphenyl compounds are decomposed by ultraviolet rays. In some cases, the required output from a high-pressure mercury lamp or high-pressure xenon lamp is Experiments have revealed that the proportion of chlorine in a phenyl compound differs depending on the chlorine content, and that a proportional output is required depending on the ratio of the reference at 100 W with respect to 1% by volume. Decomposition of polychlorinated biphenyl compounds In the treatment, a method of adapting and proportional to the numerical value with respect to the chlorine content at the time before starting is simple. Furthermore, when the polychlorinated biphenyl compounds are decomposed by ultraviolet rays, the light having a wavelength in the ultraviolet region of 250 to 370 nm effectively acts on the effective wavelength light for the high-pressure mercury lamp or the high-pressure xenon lamp. Experiments have shown that a decomposition treatment for polychlorinated biphenyl compounds is induced in the vicinity of the absorption wavelength. Next, light that can be absorbed in the titanium dioxide introduced and added to the liquid to be processed by irradiating the liquid to be processed containing an undecomposed portion of the polychlorinated biphenyl compound with ultraviolet rays. Because of the wide wavelength range, the UV treatment of ultraviolet rays at the active site in the irradiation treatment with ultraviolet rays, and the catalytic action by the photoconductivity possessed by titanium dioxide, the polychlorinated biphenyl compounds are decomposed with ultraviolet rays. Will accelerate the decomposition rate and increase the acceleration of the reaction process in the photochemical reaction. Furthermore, micro-stirring treatment by high vacuum state, low temperature state by cooling treatment and ultrasonic vibration for the liquid to be treated containing undecomposed portion of polychlorinated biphenyl compounds in the ultraviolet decomposition treatment tank The photochemical reaction is induced by irradiating ultraviolet light to the undecomposed portion of the polychlorinated biphenyl compound depending on the treatment conditions in the above state, and in the molecule due to the undegraded polychlorinated biphenyl compound in the ground state, The photon energy generated by the high-energy electromagnetic wave in the ultraviolet light can be absorbed by the electrons involved in the undecomposed molecules of the polychlorinated biphenyl compounds in the ground state by the action of the ultraviolet light generated by the ultraviolet irradiation treatment of the treatment liquid. The electrons of polychlorinated biphenyl compounds When transitioning to a higher energy level in the molecule due to decomposition, the polychlorinated biphenyl compound is in an electronic photoexcited state in the undecomposed molecule, and the polychlorinated biphenyl compound is in an electronic photoexcited state. In an undecomposed molecule of a biphenyl compound, an excitation energy is obtained in the molecule, so that an activated state is obtained in an undecomposed molecule of a polychlorinated biphenyl compound, and an activated polychlorinated biphenyl compound The undecomposed molecules of other polychlorinated biphenyl compounds act on the undegraded molecules of other polychlorinated biphenyl compounds, and the excitation energy is obtained by ultraviolet light. Giving excitation energy to undecomposed molecules of polychlorinated biphenyl compounds The reaction is being advanced one after another automatic chain reaction. Furthermore, when the excitation energy is obtained from the ultraviolet light, the undecomposed molecules of the activated polychlorinated biphenyl compounds react with the undegraded molecules of the other polychlorinated biphenyl compounds, and the excitation energy is changed. By the reaction imparted to the undecomposed molecule of the polychlorinated biphenyl compound, the excitation energy is released in the undegraded molecule of the polychlorinated biphenyl compound to be in an inactivated state and return to the ground state again. Next, regarding the undecomposed molecules of the polychlorinated biphenyl compounds, the chlorine molecules bonded by the side chain bonds in the binding molecular chain are irradiated with ultraviolet rays to the undegraded molecules of the polychlorinated biphenyl compounds in the ground state. Thus, in the molecules of polychlorinated biphenyl compounds, ultraviolet light is absorbed and excitation energy is obtained, so that an excited state is obtained, and at the same time, dissociated states are present in chlorine molecules that are bonded by side chain bonds in the polychlorinated biphenyl compounds. It is released. Further, all the chlorine molecules in a free state are combined with sodium alcoholate or sodium molecules that have been injected and added to the liquid to be treated at the time before starting the UV decomposition process by the photochemical reaction. This produces sodium chloride.

GC-ECD (Gas Chromatograph with Electron Capture Type Detector) is used for the measurement when UV decomposition is applied to undecomposed chlorine molecules after completing the ultrasonic decomposition for polychlorinated biphenyl compounds. This is the result of the analysis. Therefore, it has been experimentally found that an undecomposed portion of a polychlorinated biphenyl compound after ultrasonic decomposition treatment needs to be irradiated with ultraviolet rays for 27 to 30 minutes in the decomposition reaction treatment time by ultraviolet rays of the photochemical reaction. As a result, the polychlorinated biphenyl compounds can be completely decomposed by irradiation with ultraviolet rays. After the decomposition treatment, sodium chloride, muconic acid and a small amount of biphenyl are produced as decomposition products for the polychlorinated biphenyl compounds. Next, after completing the ultrasonic decomposition treatment for the polychlorinated biphenyl compounds, the UV decomposition treatment equipment for complete decomposition treatment is completed by ultrasonically decomposing the polychlorinated biphenyl compounds. The treated liquid is extracted out of the system of the ultrasonic decomposition processing apparatus, and further, the processing liquid is extracted from the ultrasonic decomposition processing apparatus to completely decompose the processing liquid containing the undecomposed portion. The liquid is introduced into the ultraviolet decomposition tank (32) made of titanium by the transfer pump (31) for ultraviolet decomposition treatment, and the undecomposed portion of the polychlorinated biphenyl compound contained in the liquid to be treated Sodium alcoholate (sodium) required in chemical reactions for complete decomposition by UV irradiation Tilate → sodium ethoxide and sodium methylate → sodium methoxide) or first chemical storage tank (33) for ultraviolet decomposition treatment for metallic sodium, sodium alcoholate or metallic sodium is controlled for flow rate for the first chemical for ultraviolet decomposition treatment. By means of an apparatus-linked metering pump (34), a metered amount of sodium alcoholate or metallic sodium is injected and added to the liquid to be treated in the UV decomposition treatment tank, and further, by the catalytic action of titanium dioxide having photoconductivity for UV light. In order to accelerate and increase the decomposition rate when the undecomposed portion of the polychlorinated biphenyl compounds is irradiated with ultraviolet rays for decomposition treatment, it is for ultraviolet decomposition treatment for titanium dioxide possessing photoconductive properties. Second of From the product storage tank (35), titanium dioxide is quantified with respect to the liquid to be treated in the ultraviolet decomposition treatment tank by the second chemical addition amount control device interlocking screw quantitative supply device (36) for ultraviolet decomposition treatment. Next, 5 × 10 5 in the ultraviolet decomposition tank by the vacuum pump (37) for ultraviolet decomposition outside the system of the ultraviolet decomposition apparatus. ^-4 The high vacuum state by Torr is maintained, and further, the high vacuum state is maintained in the ultraviolet decomposition treatment tank by the digital vacuum constant device (38) for ultraviolet decomposition treatment. Next, a water cooling jacket (39) for ultraviolet decomposition treatment is attached to the outside of the ultraviolet decomposition treatment tank, and water is supplied by a water cooling device (40) for ultraviolet decomposition treatment outside the system of the ultraviolet decomposition treatment device. Cooling treatment is performed, and the cooling water further cooled is introduced into the water cooling jacket by a cooling water circulation pump (41) for ultraviolet decomposition treatment, and the liquid to be treated in the ultraviolet decomposition treatment tank is cooled with the cooling water, and 0 The low temperature state is maintained by adjusting the temperature of the low temperature state of ˜4 ° C. with the temperature controller (92) for ultraviolet decomposition treatment. Next, the treated water after cooling the liquid to be treated is discharged from the water cooling jacket, the treated water is stored in the water storage tank (42) for ultraviolet decomposition treatment, and again introduced into the water cooling device. Cooling water is circulated. Furthermore, an ultrasonic oscillator (43) for ultraviolet decomposition treatment is provided in the lower part of the ultraviolet decomposition treatment tank under the treatment conditions for maintaining the low temperature state by the high vacuum and cooling treatment for the liquid to be treated in the ultraviolet decomposition treatment tank. From the ultrasonic generator, the ultrasonic output is adjusted by the ultrasonic generator (44) for ultraviolet decomposition treatment and the ultrasonic power meter (45) for ultraviolet decomposition treatment. An ultrasonic wave having an effective output of 600 W, a frequency (frequency) of 26 KHz, and an amplitude of 200 μ is oscillated with respect to the liquid to be processed, and the ultrasonic wave is added to the liquid to be processed in the ultraviolet decomposition treatment tank. As a result, the reaction area for the UV decomposition treatment is remarkably increased. Since molecules themselves by undegraded alkenyl such compounds are also vibrating at the interface an ideal active, it become in a state that promotes photochemical reaction by ultraviolet degradation process. Next, a lamp house unit (46) made of quartz glass is fixedly mounted above the surface of the liquid to be treated in the ultraviolet decomposition treatment tank or at a position in the liquid to be treated, and the inner and outer walls and the lamp house in the ultraviolet decomposition treatment tank. With the sealant made of rubber such as silicon rubber and plastic resin between the units, the airtight state by high vacuum is maintained in the UV decomposition treatment tank, so that it can withstand high vacuum and is resistant to the outside air. In order to maintain an airtight state without suction, it is necessary to make a perfect seal by closely contacting with an inner wall / outer wall and a lamp house unit in the ultraviolet decomposition bath. Next, regarding the mechanism of the lamp house unit, the double tube jacket cooling method is necessary in order to completely decompose the inner part of the lamp house unit against the undecomposed portion of the polychlorinated biphenyl compound. Insert a high-pressure mercury lamp or high-pressure xenon lamp (47) that generates ultraviolet light that is adapted to the conditions of the correct output and wavelength, and fix both ends of the lamp with quartz glass. The air cooling jacket (48) made of quartz glass for the lamp cooling process is welded and installed in the space portion, and the outside air is put inside the air cooling jacket by the air pump (49) for the lamp cooling process outside the system of the ultraviolet decomposition processing apparatus. Air flow generated by outside air in the air cooling jacket Therefore it than forcibly cooling process the heat generated by the lamp, the air flow in the After cooling processes lamp is to be exhausted from the lamp house unit out of the system. Further, in order to cool the lamp with cooling pure water outside the air cooling jacket, a water cooling jacket (50) made of quartz glass for lamp cooling treatment is contact welded, and the lamp cooling treatment outside the system of the UV decomposition processing apparatus. The pure water is cooled by the pure water cooling device (51), and the cooled pure water is then introduced into the ion exchanger (52) for the lamp cooling treatment to circulate the cooled pure water. The metal ion generated in the pure water is removed by the ion exchanger during the process. By passing the cooled pure water through the ion exchanger, the metal ion is removed and the high purity is obtained. Cooled pure water made into pure water by pressure is introduced into the water-cooled jacket by pressure, and the cooled pure water introduced into the water-cooled jacket is used by the lamp. It is the forcibly cooling process and a heat ray emitted from the heat and the lamp. The treated pure water after further cooling treatment is discharged from the water cooling jacket to the outside of the lamp house unit system, and the discharged treated pure water is then subjected to a lamp cooling treatment outside the lamp house unit system by an ultraviolet decomposition device. The purified pure water is circulated by being introduced and stored in the pure water storage tank (53) for use, and introduced again into the pure water cooling device. Therefore, the heat generation by the lamp and the heat rays radiated from the lamp are forcibly cooled by the ventilation process of the air flow by the outside air and the circulation process of the purified pure water inside the lamp house unit system, so the temperature rise due to the generation of ultraviolet rays is suppressed. Therefore, ultraviolet rays with less heat rays than the lamp house unit are emitted. Furthermore, in the ultra-violet decomposition tank, the liquid to be treated containing the undecomposed portion of the polychlorinated biphenyl compound is in a high vacuum state, a low temperature state by cooling treatment, and a state in intense microscopic stirring treatment by ultrasonic waves. The high pressure mercury lamp or the high pressure xenon lamp emits ultraviolet rays under the treatment conditions that are sustained, and passes through the lamp house unit, so that strong ultraviolet rays with less heat rays are applied to the undecomposed portion of the polychlorinated biphenyl compounds. In contrast, the polychlorinated biphenyl compounds are completely decomposed by subjecting them to irradiation treatment, UV decomposition treatment by photochemical reaction, and completely decomposing the undecomposed portion of the polychlorinated biphenyl compounds. It is. Next, in the treatment liquid that has been completely decomposed by the ultraviolet decomposition treatment for the polychlorinated biphenyl compounds, the treatment liquid discharge solenoid valve for ultraviolet decomposition treatment installed in the lower part of the ultraviolet decomposition treatment tank ( 54) is operated to open the ultraviolet decomposition process by the photochemical reaction, and the treatment liquid in which the decomposition process is completely completed for the polychlorinated biphenyl compounds is removed from the system by the ultraviolet decomposition apparatus. For the vacuum distillation treatment to separate the treatment liquid from the solvent and the decomposition residue of the polychlorinated biphenyl compounds, the extracted treatment liquid is vacuum-distilled by a transfer pump for vacuum distillation treatment. It is introduced inside. Next, regarding the vacuum distillation treatment to separate the solvent and decomposition residue from the treatment liquid that completely decomposed the polychlorinated biphenyl compounds, the decomposition treatment was completely completed for the polychlorinated biphenyl compounds. The treatment liquid is extracted out of the system of the UV decomposition treatment apparatus, introduced into the vacuum distillation treatment tank by a transfer pump for vacuum distillation treatment, and contains the decomposition residue due to the solvent and the polychlorinated biphenyl compound. The inside of the vacuum distillation treatment tank into which the liquid to be treated is introduced is 5 × 10 5 in the vacuum distillation treatment tank by a vacuum pump for vacuum distillation treatment outside the system of the vacuum distillation treatment apparatus. ^-4 A high vacuum state is obtained by Torr, and a high vacuum state is maintained by a digital vacuum constant device for vacuum distillation. Next, a heating device for vacuum distillation treatment is attached in contact with the lower part of the vacuum distillation treatment tank, and the liquid to be treated in the vacuum distillation treatment tank is treated under high vacuum conditions by the heating device for vacuum distillation treatment. The temperature of the solvent is adjusted by the first temperature controller, and the solvent contained in the liquid to be treated is indirectly heated under a temperature condition equal to or higher than the boiling point, whereby the solvent is vaporized into a solvent vapor state. Ascending inside the vacuum distillation processing apparatus, introducing a cooling serpentine tube in the upper part of the vacuum distillation processing apparatus into the solvent vapor condensing part in the cooling part, and vacuum distillation processing equipped in the solvent vapor condensing part The temperature is adjusted by the second temperature controller for the solvent, and the solvent vapor is cooled at a temperature below the boiling point of the solvent, thereby condensing the solvent vapor. The state of the solvent is reproduced by liquefaction and the solvent is recovered, and the liquid to be treated containing the solvent introduced into the vacuum distillation treatment tank and the decomposition residue of the polychlorinated biphenyl compound is removed. After the solvent is completely recovered by vacuum distillation, the solvent and the decomposition residue of the polychlorinated biphenyl compound can be separately treated. Furthermore, the decomposition residue due to the polychlorinated biphenyl compound remaining in the vacuum distillation tank is extracted out of the system of the vacuum distillation apparatus. In addition, if the decomposition residue from the polychlorinated biphenyl compound contains oil, the decomposition residue from the polychlorinated biphenyl compound is removed from the system of the vacuum distillation treatment apparatus, and then the oil is removed. Therefore, it is introduced into the separation processing tank. Next, regarding the vacuum distillation treatment equipment that separates the solvent and decomposition residue from the treatment liquid that completely decomposed the polychlorinated biphenyl compounds, the decomposition treatment of the polychlorinated biphenyl compounds is completed completely. The treated liquid was extracted outside the system of the ultraviolet decomposition processing apparatus, and the extracted processed liquid was introduced into the vacuum distillation treatment tank (56) by the transfer pump (55) for vacuum distillation treatment. A vacuum pump for vacuum distillation treatment outside the system of the vacuum distillation treatment apparatus inside the vacuum distillation treatment tank into which the liquid to be treated containing the solvent and the decomposition residue by the polychlorinated biphenyl compound is introduced (57) 5 × 10 5 in a vacuum distillation tank ^-4 A high vacuum state is caused by Torr, and the high vacuum state is maintained in the vacuum distillation treatment tank by a digital vacuum constant device (58) for vacuum distillation treatment. Next, a heating device (59) for vacuum distillation treatment is placed in contact with the lower part of the vacuum distillation treatment tank, and the liquid to be treated in the vacuum distillation treatment tank is subjected to treatment conditions in a high vacuum state by the heating device. Indirect heat treatment is performed, and the temperature is adjusted by the first temperature controller (60) for vacuum distillation treatment provided for the heating device, so as to correspond to the treatment conditions in a high vacuum state, The state of the heat treatment under the set temperature condition higher than the boiling point temperature for the solvent contained in the liquid to be treated is maintained, and the solvent contained in the liquid to be treated is vaporized by the heat treatment above the boiling temperature, Depending on the state, the inside of the vacuum distillation processing apparatus is raised and introduced into the solvent vapor condensing unit (61) for vacuum distillation processing by the upper part of the vacuum distillation processing apparatus, and the vacuum distillation processing is performed around the solvent vapor condensing part. A cooling section (63) for vacuum distillation treatment provided with a cooling serpentine pipe (62) is provided, and water is cooled by a water cooling device (64) for vacuum distillation treatment outside the system of the vacuum distillation treatment apparatus. The cooling water further cooled is introduced into the cooling serpentine pipe provided for the cooling unit in the upper part of the vacuum distillation processing apparatus by the cooling water circulation pump (65) for vacuum distillation processing. The solvent vapor introduced into the solvent vapor condensing unit at the upper part in the vacuum distillation processing apparatus is subjected to a cooling treatment, and the second temperature controller (67) for vacuum distillation processing provided in the solvent vapor condensing unit Thus, the temperature is adjusted, and the state of the cooling treatment is maintained under a set temperature condition not higher than the boiling point temperature of the solvent contained in the liquid to be treated. Further, the treated water after cooling the solvent vapor is discharged from the cooling serpentine tube, and the treated water is introduced into the water storage tank (66) for vacuum distillation treatment outside the system of the vacuum distillation treatment apparatus and stored. Then, it is introduced again into the water cooling device and the cooling water is circulated. Next, the solvent vapor introduced into the solvent vapor condensing part in the vacuum distillation treatment apparatus is condensed and liquefied by cooling treatment under a temperature condition below the boiling point temperature of the solvent, and the cooling serpentine in the cooling part in the solvent vapor condensing part The solvent as a condensate is collected and stored by a condensate drop receiving / recovering device (68) for vacuum distillation processing, which is equipped at the bottom of the container, and recovered in the condensing droplet receiving / collecting device. The first electromagnetic valve (69) for vacuum distillation treatment opens the solvent by an automatic opening / closing operation and introduces the solvent into the recovery solvent storage tank (70) for vacuum distillation treatment outside the system of the vacuum distillation treatment apparatus. When the amount of the recovered solvent stored reaches a fixed amount, the recovered solvent in the recovered solvent storage tank is automatically collected by the second electromagnetic valve (71) for vacuum distillation. It is made open by an open / close operation and extracted outside the system of the vacuum distillation processing device, and the liquid to be treated is completely vacuum distilled by the vacuum distillation processing device and completed by the solvent and polychlorinated biphenyl compounds. The decomposition residue is separated. Next, the apparatus relating to the vacuum distillation treatment is stopped, the decomposition residue due to the polychlorinated biphenyl compounds remaining in the vacuum distillation treatment tank is cooled, and extracted outside the system of the vacuum distillation treatment apparatus, If the decomposition residue contains oil, it is introduced into the separation treatment tank. Next, with regard to the decomposition treatment for removing the oil contained in the decomposition residue by the polychlorinated biphenyl compound, the treatment liquid after the polychlorinated biphenyl compound is completely decomposed is subjected to vacuum distillation treatment. After all the solvent contained in the liquid to be treated has been recovered, the decomposition residue due to the polychlorinated biphenyl compounds remaining in the vacuum distillation tank is extracted outside the system of the vacuum distillation apparatus. Further, when the decomposition residue by the polychlorinated biphenyl compound contains an oil, it is introduced into the separation treatment tank in order to remove the oil. Next, a fixed amount of normal hexane is injected into the decomposition residue at a ratio of 1: 2 in the volume ratio with respect to the decomposition residue of the polychlorinated biphenyl compound introduced into the separation treatment tank. In order to improve the permeability, deoilability and oil extraction efficiency of the decomposition residue by biphenyl compounds, the separation processing equipment of the separation processing equipment is used to extract the oil contained in the decomposition residue. 5x10 in the separation tank by a vacuum pump outside the system ^-4 The high vacuum state by Torr is maintained, and further, the inside of the separation processing tank is maintained in the high vacuum state by the digital vacuum constant device. Next, a water cooling jacket is contacted and attached to the outside of the separation treatment tank, the water is cooled by a water cooling device outside the system of the separation treatment device, and the cooled cooling water is cooled outside the system of the separation treatment device. It is introduced into the water cooling jacket by the water circulation pump, the liquid to be treated in the separation treatment tank is cooled with the cooling water in the water cooling jacket, and the temperature is adjusted by the temperature controller provided in the separation treatment device, and then cooled. In the treated liquid to be treated, a low temperature state of 0 to 4 ° C. is maintained, and the treated water after cooling the treated liquid is discharged from the water cooling jacket, and further the separation processing apparatus. The treated water is introduced into the water storage tank outside the system and stored, and then introduced again into the water cooling device to circulate the cooling water. It is. Next, under the processing conditions in the low temperature state by high vacuum and cooling treatment, an ultrasonic oscillator is attached to the lower part of the separation tank, and the ultrasonic oscillation is generated by the ultrasonic generator and the ultrasonic wattmeter. The output is adjusted, and an ultrasonic output is used to oscillate powerful ultrasonic waves with an effective output of 600 W, frequency (frequency) of 26 kHz, and amplitude of 200 μm on the liquid to be treated. And the liquid to be treated containing normal hexane is vibrated by ultrasonic waves, and a vigorous microscopic stirring action is applied by vigorous ultrasonic vibrations, thereby adding oil content contained in the decomposition residue. The extraction treatment reaction is promoted and the polychlorinated biphenyls are sufficiently compounded with normal hexane under various treatment conditions for the liquid to be treated. After the oil is extracted from the decomposition residue mixed with oil, and the extraction processing time is completed for 15 to 20 minutes to complete the extraction of the oil contained in the decomposition residue, In order to stop all the equipment involved in the extraction process and further perform separation using the solubility, boiling point and specific gravity difference in the solvent, select and use furfural with poor solubility in oil and normal hexane, A fixed amount of furfural is injected into the liquid to be treated at a ratio of 1: 1 in the volume ratio with respect to the decomposition residue of the polychlorinated biphenyl compound, and all devices are operated again. Under the above processing conditions, the solvent separation treatment was sufficiently performed with furfural, and the solvent separation treatment time was completed in 10 to 15 minutes. Completely complete the solvent separation process for the oil contained in the decomposition residue, and then complete the solvent separation process, stop all the devices involved in the separation process, and let the separation apparatus stand still As a result, the liquid to be treated is separated into two layers due to the difference in specific gravity, the upper layer is a mixture of oil and normal hexane, and the lower layer is decomposed by furfural and polychlorinated biphenyl compounds. It is separated into a liquid mixture with the product. Further, the position of the boundary surface with respect to the two-layer portion is detected and measured by a boundary surface detection device using a glass tube measuring device or a conductivity liquid level measuring device provided outside the system from the separation processing tank, and then the boundary surface in the two-layer portion. In the case where the processing solution is extracted from the separation processing tank outside the separation processing system after the position is detected and measured, the amount of the extraction processing relative to the outflow amount is controlled by the transfer pump for vacuum distillation processing. Alternatively, the liquid level drop position is controlled by an ultrasonic level meter to perform extraction processing, and the amount of processing liquid to be extracted in the separation processing tank is adjusted and controlled. Furthermore, by operating the treatment liquid discharge solenoid valve mounted at the bottom of the separation treatment tank to open it, first mixing with the decomposition residue by furfural and polychlorinated biphenyl compounds in the lower layer part in the separation treatment tank The extracted processing solution is vacuum-distilled in order to separate the solvent and the residue for each of the separated treatments separately from the system of the decomposition processing apparatus. However, furfural and polychlorinated biphenyls that have been preliminarily divided into two vacuum distillation tanks and extracted from the separation tank into one of the vacuum distillation tanks by a transfer pump for vacuum distillation. When the mixed solution with the decomposition residue due to the compound is introduced and the introduction process is completely completed, it is placed in the lower part of the separation treatment tank. That the process liquid discharge solenoid valve by automatically operated to the closed state, it being stopped automatically in conjunction with transfer pump for vacuum distillation process at the same time. Next, in order to extract the oil remaining in the separation tank and the mixture with normal hexane outside the separation processing system, the treatment liquid discharge solenoid valve is automatically operated again and opened. At the same time, the transfer pump for vacuum distillation treatment is interlocked and automatically activated again, and the mixture of oil and normal hexane in the separation treatment tank is extracted out of the system of the separation treatment device, and further vacuumed The liquid mixture with oil and normal hexane is introduced into the other tank in the vacuum distillation tank by a transfer pump for distillation. Next, with regard to the separation processing device for removing the oil contained in the decomposition residue by polychlorinated biphenyl compounds, vacuum distillation treatment is applied to the treatment liquid after the polychlorinated biphenyl compounds are completely decomposed. After the vacuum distillation treatment by the device and the solvent contained in the liquid to be treated is all collected by the vacuum distillation treatment device, the decomposition residue due to the polychlorinated biphenyl compounds remaining in the vacuum distillation treatment tank is removed. Polychlorinated biphenyl compounds removed from the system of the vacuum distillation treatment device, and if the oil contained in the decomposition residue due to the polychlorinated biphenyl compounds that have been removed is contained in order to remove the oil The decomposition residue is introduced into the separation treatment tank (72). Next, normal hexane is separated from the first chemical storage tank (73) for separation processing outside the system of the separation processing device by the first chemical flow control device interlocking metering pump (74) for separation processing, and the polychlorinated biphenyl compounds. A fixed amount of normal hexane is injected into the decomposition residue by the polychlorinated biphenyl compound introduced into the separation treatment tank at a ratio of 1: 2 in the volume ratio with respect to the decomposition residue, and further separated in the separation treatment tank. The upper plate (75) is set against the upper part of the separation processing tank, and the upper part of the separation processing tank is closed to keep the inside of the separation processing tank in a sealed state, outside the system of the separation processing apparatus. 5 × 10 5 in the separation processing tank by the vacuum pump (76) for separation processing. ^-4 A high vacuum state is produced by Torr, and a high vacuum state is maintained in the separation treatment tank by a digital vacuum constant device (77) for separation treatment. Next, a water cooling jacket (78) for separation treatment is attached to the outside of the separation treatment tank, and the water is cooled by the water cooling device (79) for separation treatment outside the system of the separation treatment device. The cooled cooling water is introduced into the water cooling jacket by a cooling water circulation pump (80) for separation treatment outside the system of the separation treatment device, and the liquid to be treated in the separation treatment tank is cooled by the cooling water in the water cooling jacket. The temperature is adjusted by the temperature controller (89) for separation processing provided in the separation processing apparatus, and the low temperature state of 0 to 4 ° C. is maintained in the cooled liquid to be treated. The treated water after being cooled with respect to the treatment liquid is discharged from the water cooling jacket, and further used for separation treatment outside the system of the separation treatment apparatus. To introduce treated water to the storage tank (81) is stored in, it is to circulate the cooling water by again introduced into water cooler. Next, an ultrasonic oscillator (82) for separation processing is attached to the lower part of the separation processing tank in contact with the lower part of the separation processing tank under the processing conditions in a low temperature state by high vacuum / cooling processing, and ultrasonic waves for separation processing are generated. The ultrasonic oscillation output is adjusted by the apparatus (83) and the ultrasonic power meter (84) for separation processing, and the ultrasonic oscillation apparatus has an effective output of 600 W, a frequency (frequency) of 26 KHz, and a powerful ultrasonic wave with an amplitude of 200 μm. Oscillates to the liquid to be treated, vibrates with ultrasonic waves the liquid to be treated containing the decomposition residue mixed with polychlorinated biphenyl compounds and normal hexane, and by strong ultrasonic vibration By adding a vigorous microscopic stirring action, the extraction reaction by the solvent is promoted for the oil contained in the decomposition residue, Under the treatment conditions of the seeds, normal hexane is sufficient to extract the oil from the decomposition residue mixed with oil by polychlorinated biphenyl compounds, and the extraction treatment time is completely contained in the decomposition residue by 15 to 20 minutes. After completing the oil extraction process and completing the oil extraction process contained in the decomposition residue with normal hexane, all the equipment involved in the extraction process was stopped, and the solubility and boiling point in the solvent and In order to separate and utilize the difference in specific gravity, furfural due to poor solubility in oil and normal hexane is selected and used. Next, the furfural from the second chemical storage tank (85) for separation processing outside the system of the separation processing device is decomposed by the polychlorinated biphenyl compound by the second chemical flow rate controller linked meter pump (86) for separation processing. A fixed amount of furfural with respect to the residue in a ratio of 1: 1 by volume is injected and added to the liquid to be treated, and all devices involved in the separation process are operated again. Under the processing conditions, the solvent separation treatment is sufficiently performed with furfural, and the solvent separation treatment is completed for 10 to 15 minutes with respect to the oil contained in the decomposition residue completely. Next, after completing the solvent separation treatment, all the devices involved in the separation treatment are stopped and the separation treatment device is allowed to stand. -Separated into a two-layer part at the bottom, the upper part is a mixture with oil and normal hexane, and the lower part is separated into a mixture with a furfural and polychlorinated biphenyl compounds decomposition residue It is. Furthermore, the boundary surface detection device (87) for separation processing by the glass tube measuring device or the conductivity liquid level measuring device equipped outside the system from the separation processing tank is used to detect and process the position of the boundary surface with respect to the two-layer part, Next, after detecting and measuring the position of the boundary surface in the two-layer portion, the processing liquid is extracted from the separation processing tank outside the system of the separation processing apparatus, but is discharged by a transfer pump for vacuum distillation processing. The amount of the extraction liquid in the separation processing tank is adjusted and controlled according to the method for controlling the amount of extraction processing relative to the amount or controlling the descent position of the liquid level with an ultrasonic level meter. . Further, by operating the separation treatment liquid discharge solenoid valve (88) attached to the lower part of the separation treatment tank to open it, initially furfural and polychlorinated biphenyls in the lower layer portion in the separation treatment tank In order to extract the mixed solution of the decomposition residue from the compound out of the system of the separation processing apparatus, and then separate the solvent and the residue for each of the separated processing, the extracted processing solution is used. The vacuum distillation treatment is carried out, but the vacuum distillation treatment tank is preliminarily divided into two tanks, and is extracted from the separation treatment apparatus into one of the vacuum distillation treatment tanks by a transfer pump for vacuum distillation treatment. When the mixture of the furfural and polychlorinated biphenyl compounds and the decomposition residue was introduced and the introduction process was completed, Automatically activates the processing liquid discharge solenoid valve in the lower part of the treatment tank is in the closed state, it is for stopping automatically tuned to transfer pump for vacuum distillation process at the same time. Next, in order to extract the oil remaining in the separation tank and the mixture with normal hexane outside the separation processing system, the treatment liquid discharge solenoid valve is automatically operated again and opened. At the same time, synchronize the transfer pump for vacuum distillation processing and automatically operate it again to extract the oil and normal hexane mixed liquid in the separation processing tank out of the system of the separation processing device, and further vacuum The liquid mixture with oil and normal hexane is introduced into the other tank in the vacuum distillation tank by a transfer pump for distillation. Next, two kinds of two kinds of liquid mixture stored in two tanks equipped with a division in a vacuum distillation treatment tank were again subjected to vacuum distillation treatment again, and normal hexane [boiling point 68.7 ° C (760 mmHg)] and furfural Due to the difference in boiling point of the solvent at [boiling point 161.8 ° C. (760 mmHg)], the vacuum distillation treatment apparatus is operated and first, normal hexane and then furfural are fractionally fractionated. The solvent is recovered by extracting it out of the system. Furthermore, after the solvent is completely recovered, all the equipment involved in the vacuum distillation process is stopped, and the oil content of the distillation residue remaining in the two tanks and the polychlorinated biphenyl compounds in the vacuum distillation process tank The decomposition residue obtained by the above is cooled, and the separated oil component and the decomposition residue caused by the polychlorinated biphenyl compound are separately extracted outside the system of the vacuum distillation apparatus. In addition, when the decomposition residue by a polychlorinated biphenyl compound does not contain an oil component, a separation process step is not necessary. Further, each solvent recovered by vacuum distillation is continuously used again at a necessary point in order to continuously decompose the polychlorinated biphenyl compounds. Next, the recovered oil is industrially reused with heat transfer oil / lubricating oil, etc., and the decomposition residue of the recovered polychlorinated biphenyl compounds is separated again to extract sodium chloride, etc. Then, it is industrially reused, and the part that cannot be reused industrially is incinerated by an incinerator. Next, an apparatus involved in the decomposition treatment of the polychlorinated biphenyl compounds is mounted on the trailer vehicle and decomposed on the vehicle.
(Operation) The present invention is perfect for polychlorinated biphenyl compounds that have been used in large amounts in transformer oil extracted from the transformer, condenser body, carbonless paper, soil / sediment, and coated parts for insulation by coated wires. In order to make it resistant to corrosion, a steel product made of titanium is used at the contact area of the liquid to be treated, since polychlorinated biphenyl compounds with a high concentration of total chlorine were used for each variety. In order to extract polychlorinated biphenyl compounds from various products, it is introduced into an extraction tank made of titanium, and a solvent in isopropyl alcohol or normal hexane is injected and added to the high vacuum and cooling process. Ultrasonic generator at the lower part of the extraction tank Extraction processing equipment depending on processing conditions in which powerful ultrasonic waves are oscillated, strong ultrasonic vibrations are applied to the liquid to be processed, and intense microscopic stirring action is imparted by strong ultrasonic waves Thus, the polychlorinated biphenyl compound is subjected to extraction treatment, and the polychlorinated biphenyl compound is completely extracted and completed, and then extracted from the extraction processing apparatus outside the system. Next, in the treatment liquid after extracting the polychlorinated biphenyl compounds, it is introduced into an ultrasonic decomposition treatment tank made of titanium, and a fixed amount of sodium alcoholate or metallic sodium is injected and added to the liquid to be treated. Strong ultrasonic waves are oscillated from the ultrasonic oscillation device to the liquid to be processed containing polychlorinated biphenyl compounds under the processing conditions that maintain the state against the low temperature due to vacuum and cooling treatment. The liquid to be treated is vibrated vigorously, and the relative speed between the solvent and the polychlorinated biphenyl compound is constituted by the action of the ultrasonic wave itself and the effect of cavitation induced by the ultrasonic wave. The frictional force acts between the two, and the binding force of the polychlorinated biphenyl compound is caused by the frictional force. The main chain bond and the side chain bond due to cis are actively cut, and the chlorine molecules in the side chain bond of polychlorinated biphenyl compounds are affected by the action of the ultrasonic wave itself and the cavitation induced by the ultrasonic wave. The side chain bond is broken by the effect and frictional force, and the chlorine molecules bound to the side chain are released. All the released chlorine molecules are treated before the ultrasonic decomposition treatment. Sodium alcoholate previously injected and added to sodium molecules or sodium molecules with metallic sodium are combined to form sodium chloride. Furthermore, the main chain bonds in polychlorinated biphenyl compounds are also broken by the action of ultrasonic waves by the ultrasonic decomposition treatment, the effect of ultrasonic cavitation and the action of frictional forces, and the benzene rings It is liberated. Furthermore, all of the benzene rings that have been brought into a free state are efficiently irradiated with strong ultrasonic waves, and the action of the ultrasonic waves themselves by the powerful ultrasonic decomposition treatment, the effect of the cavitation induced by the ultrasonic waves, and the relative velocity. The frictional force causes all benzene rings released into a free state to be cleaved by the oxidizing action in the powerful ultrasonic decomposition treatment to produce muconic acid by unsaturated dicarboxylic acid. Furthermore, the treatment liquid in which the ultrasonic decomposition treatment is completed with respect to the polychlorinated biphenyl compound is extracted out of the system of the ultrasonic decomposition processing apparatus. Next, in order to decompose the undecomposed portion of the polychlorinated biphenyl compound, the treatment liquid that has been subjected to the ultrasonic decomposition treatment for the polychlorinated biphenyl compound is extracted from the ultrasonic decomposition apparatus, and is made of titanium. Introduce it into the UV decomposition treatment tank, and add a fixed amount of sodium alcoholate or metallic sodium to the liquid to be treated, and then accelerate the rate of UV decomposition treatment. Add a fixed amount, keep the state of low temperature by high vacuum and cooling treatment, oscillate strong sonic waves to the liquid to be processed by ultrasonic oscillating device in the lower part of UV decomposition treatment tank, High pressure mercury lamp or high pressure depending on the processing conditions for various to add vigorous microscopic stirring action by adding vibration by sound wave Polychlorinated biphenyl contained in the liquid to be treated by ultraviolet decomposition by radiating ultraviolet rays with less heat rays than the lamp house unit equipped with a cooling lamp and irradiating the liquid with ultraviolet rays. The action of ultraviolet light caused by ultraviolet irradiation treatment in the undegraded molecules of the polychlorinated biphenyl compounds in the ground state by irradiating ultraviolet light to the undegraded part of the molecules of the organic compound and inducing a photochemical reaction By absorbing the photon energy generated by the high-energy electromagnetic wave in the ultraviolet light in the electrons involved in the undecomposed molecules of the polychlorinated biphenyl compounds in the ground state, the electrons are caused by the undecomposed of the polychlorinated biphenyl compounds. Higher energy within the molecule When the polychlorinated biphenyl compound is undegraded, the molecule is in an electronic photoexcited state, and by obtaining excitation energy in the molecule, the molecule is activated. The activated chain reaction proceeds one after another by a reaction in which the undegraded molecules of the activated polychlorinated biphenyl compounds act on the undegraded molecules of the other polychlorinated biphenyl compounds to impart excitation energy. The excitation energy is released and imparted to other molecules to be deactivated and return to the ground state again. However, the undecomposed molecules of the polychlorinated biphenyl compounds in the ground state are irradiated with ultraviolet rays. In the case of undecomposed molecules of polychlorinated biphenyls, polychlorinated biphenyls are absorbed by high energy absorption by ultraviolet rays. In the undecomposed molecule of the nyl compound, it is excited to become a high energy state, and by obtaining photoexcitation energy, it becomes activated and becomes an excited state. At the same time, the polychlorinated biphenyl compound is undecomposed. As a result of the side chain binding to the molecule, the chlorine molecules bound to the side chains are rapidly dissociated and released, and all the released chlorine molecules are subjected to UV decomposition treatment. Sodium alcohol and sodium molecules previously injected and added to the liquid to be treated before the start of binding are combined with sodium molecules to produce sodium chloride. After further UV decomposition treatment, polychlorinated biphenyls are completely formed. You can complete decomposition treatment for objects. Therefore, in the decomposition treatment for polychlorinated biphenyl compounds, a complete decomposition treatment cannot be performed for a single decomposition treatment apparatus, and a decomposition treatment method in which ultrasonic decomposition treatment and ultraviolet decomposition treatment are used in combination is adopted. Therefore, the decomposition treatment for the polychlorinated biphenyl compounds can be completed completely. Next, after the decomposition treatment is completely completed for the polychlorinated biphenyl compounds, the treatment liquid is extracted out of the system from the UV decomposition treatment equipment, and the separation residue from the solvent and polychlorinated biphenyl compounds is separated. In order to achieve this, a treatment liquid containing a solvent and a decomposition residue of a polychlorinated biphenyl compound is introduced into a vacuum distillation treatment tank, and the liquid to be treated is subjected to vacuum distillation treatment. In the solvent contained in the liquid to be treated in the above, under the processing conditions in a high vacuum state, the solvent is promoted to a temperature higher than the boiling point of the solvent, the solvent is brought into a solvent vapor state, and the solvent vapor is further brought into a boiling point of the solvent The polychlorinated biphenyl remaining in the vacuum distillation treatment tank after the following cooling treatment, the solvent contained in the liquid to be treated being recovered and vacuum distillation treated The decomposition residue by compounds of letting excised processed outside the system of the vacuum distillation apparatus. Next, in the case where an oil component is contained in the decomposition residue of the polychlorinated biphenyl compound, in order to remove the oil component, the decomposition residue of the polychlorinated biphenyl compound is introduced into the separation treatment tank, and further the normal hexane A fixed amount is injected and added to the decomposition residue of polychlorinated biphenyl compounds to maintain the state of high vacuum and low temperature by cooling treatment, and powerful ultrasonic waves are generated by the ultrasonic oscillator at the bottom of the separation treatment tank. Oscillate the liquid to be treated containing the decomposition residue of polychlorinated biphenyl compounds and normal hexane, vibrate the liquid to be treated with strong ultrasonic waves, and vigorously microscopic stirring with strong ultrasonic waves Contained in decomposition residue by polychlorinated biphenyl compounds, depending on various treatment conditions for the state of action In order to extract the oil component that had been extracted into normal hexane, and then to perform separation using the differences in solubility, boiling point, and specific gravity in the solvent, the amount of furfural that was hardly soluble in the oil and normal hexane was determined. After the liquid to be treated is completely separated by solvent separation treatment, all the devices involved in the separation treatment are stopped and the separation treatment device is allowed to stand so that the liquid to be treated has a specific gravity. Due to the difference, the upper layer and the lower layer are generally separated into two layers. In the upper layer, a mixture of normal hexane and oil, and in the lower layer, a mixture of decomposition products of furfural and polychlorinated biphenyl compounds. It will be in the state of separation processing. Further, after detecting the position of the boundary surface, each of the two types of mixed solutions separated into the two-layer portions in the separation processing tank is separately extracted outside the system of the separation processing apparatus. Next, vacuum separation is performed again to separate the two types of liquid mixture that have been separately extracted outside the system of the separation processing apparatus. Separately, in one of the vacuum distillation treatment tanks, a mixed liquid with furfural and polychlorinated biphenyl compounds and a residue of decomposition by a polychlorinated biphenyl compound, and a mixed liquid with normal hexane and other oil components are introduced separately into the other tank. Due to the difference in boiling point temperature in the solvent of normal hexane and furfural with respect to the two kinds of mixed liquids, two kinds of mixed liquids in each of the two tanks in the vacuum distillation treatment tank are simultaneously vacuum distilled, and each in a separate tank. In the two types of mixed liquids contained in each, the solvent containing normal hexane and furfural contained in each At the same time, a vacuum distillation process is performed on two kinds of mixed liquids, so that a fractional distillation process is performed at a difference in boiling point temperature. First, normal hexane, and then furfural and a solvent are sequentially recovered, and vacuum is applied to the two kinds of mixed liquids. After the distillation treatment is completed, the oil component and the decomposition residue due to the polychlorinated biphenyl compound remain in two separate tanks in the vacuum distillation treatment tank. Next, in the vacuum distillation tank, the oil remaining in the separate tank and the decomposition residue due to the polychlorinated biphenyl compound are extracted out of the system of the vacuum distillation apparatus in a separate state. Furthermore, for various solvents recovered by vacuum distillation, various solvents are recycled for continuous decomposition of the polychlorinated biphenyl compounds. Next, the recovered oil and the decomposition residue due to the polychlorinated biphenyl compound are reused, and the portion that cannot be reused is further incinerated by an incinerator.
(Examples) In the case where the polychlorinated biphenyl compounds according to the present invention are decomposed, the details of the examples are as follows. The transformer oil (insulating oil) containing the polychlorinated biphenyl compounds contained inside the transformer is extracted from the inside of the transformer to the outside of the instrument, and then the extracted transformer oil is titanium. The product is introduced into the extraction processing tank, and the uppermost part of the extraction processing tank is completely closed by a set of upper plates made of titanium, the inside of the extraction processing tank is completely sealed, and a chemical flow control device By operating the interlocking metering pump, isopropyl alcohol is added to the transformer oil in the extraction processing tank at a ratio of 1: 1 by volume ratio to the transformer oil, and then the vacuum pump outside the system of the extraction processing apparatus is added. And 5 × 10 in the extraction treatment tank ^-4 The high vacuum state is caused by Torr, and the high vacuum state is maintained by the digital vacuum constant device, and then the water cooling device and the cooling water circulation pump outside the system of the extraction processing device are operated, and the extraction processing tank The cooling water cooled in the water-cooled jacket that is in contact with the outside is fluidly circulated, the liquid to be treated in the extraction treatment tank is cooled, the temperature is adjusted by the temperature controller, and the inside of the extraction treatment tank is adjusted. Thus, the temperature of the liquid to be treated is maintained at a low temperature of 0 to 4 ° C. Next, the ultrasonic oscillator is attached to the lower part of the extraction processing tank, and the ultrasonic generator and the ultrasonic power meter outside the extraction processing system are operated to adjust the ultrasonic oscillation output. Effective output 600W from sound wave oscillator, frequency (frequency) 26KHz, amplitude 200μ, intensity 1.0W / cm ² The powerful ultrasonic wave generated by oscillates to the liquid to be processed from the lower part of the extraction processing tank, and gives strong vibration to the liquid to be processed in the extraction processing tank. The extraction treatment time for polychlorinated biphenyl compounds is promoted under various treatment conditions in a state where intense microscopic stirring action is applied by simple ultrasonic waves, and the extraction treatment time for complete extraction treatment is 10-15. By performing the treatment for a minute, the extraction treatment for the polychlorinated biphenyl compounds can be completed completely. Next, the capacitor body containing the polychlorinated biphenyl compound is subjected to a removal treatment of the exterior parts, and the condenser body containing the extracted polychlorinated biphenyl compound is solidified asphalt as a whole. Therefore, the solidified capacitor body is pulverized into a fine state of 0.5 to 1.0 μm by a crushing device or a pulverizing device, and after pulverizing, it is made into a fine powder. The fine powder from the condenser was introduced into the extraction processing tank made of titanium, the uppermost part of the extraction processing tank was completely closed by the set of the upper plate made of titanium, and the inside of the extraction processing tank was completely sealed, Furthermore, the metering pump linked with the flow rate control device for chemicals is operated, and the volume ratio of isopropyl alcohol to the fine powder by the condenser is 1: 1. Depending on the processing conditions in the extraction process similar to the state of the extraction process for the polychlorinated biphenyl compounds in the above-mentioned transformer oil, the fixed amount is injected and added to the fine powder by the condenser in the extraction processing tank. By applying strong ultrasonic vibrations to the liquid to be treated in the treatment tank and adding intense microscopic stirring action with strong ultrasonic waves, the extraction treatment for polychlorinated biphenyl compounds is promoted and complete. With respect to the extraction treatment time for the extraction treatment, the treatment for 15 to 20 minutes can complete the extraction treatment for the polychlorinated biphenyl compounds more completely than the fine powder by the condenser. Next, after stopping all the devices involved in the extraction process, the processing liquid that has completed the extraction process is extracted from the extraction process tank and introduced into the vacuum filtration process tank. The liquid to be treated is subjected to a vacuum filtration treatment to completely complete the extraction treatment for the polychlorinated biphenyl compounds. The residue after filtration is washed again with isopropyl alcohol and then incinerated by an incinerator, and the isopropyl alcohol used in the washing is continuously polychlorinated biphenyls. In order to extract the compound, it is used again as a solvent. Next, for carbonless paper (pressure-sensitive paper) and paper products containing polychlorinated biphenyl compounds, carbonless paper and paper products are cut into thin lines with a shredder, and further cut into carbonless paper and paper products. The paper product is introduced into the extraction tank made of titanium, and the uppermost part of the extraction tank is completely closed by the set of the upper plate made of titanium so that the inside of the extraction tank is completely sealed. The chemical flow control device linked metering pump is operated, and the carbon dioxide and paper products that have been cut are quantified according to the ratio of isopropyl alcohol or acetone in a 1: 1 volume ratio. The state of the extraction treatment for polychlorinated biphenyl compounds in the above-mentioned transformer oil added to paper and paper products. Under the same processing conditions in the extraction process, a powerful ultrasonic vibration is applied to the liquid to be processed and the paper piece in the extraction tank from the bottom, and a strong microscopic stirring action is added by the strong ultrasonic wave. To accelerate the extraction process for polychlorinated biphenyl compounds, and the extraction process time for complete extraction process is more perfect than carbon paper and paper products cut into thin lines by treatment for 9-15 minutes In addition, the extraction treatment for the polychlorinated biphenyl compounds can be completed. Next, after stopping all the devices involved in the extraction process, the processing liquid after completion of the extraction process is extracted from the extraction process tank and introduced into the vacuum filtration process tank. The liquid to be treated is subjected to a vacuum filtration treatment to completely complete the extraction treatment for the polychlorinated biphenyl compounds. In addition, about the paper piece etc. with respect to the residue in an extraction processing tank and the residue after a filtration process, after making it wash again with the solvent with respect to isopropyl alcohol or acetone, it is made to incinerate with an incineration processing apparatus, The used isopropyl alcohol or acetone is used again as a solvent in order to continuously extract the polychlorinated biphenyl compounds. Next, for the soil or sediment containing the polychlorinated biphenyl compounds, the soil or sediment containing the polychlorinated biphenyl compounds is introduced into the titanium extraction treatment tank, and the top of the extraction treatment tank Is completely closed by setting the upper plate made of titanium, the inside of the extraction tank is completely sealed, and the metering pump linked with the flow rate control device for chemicals is operated to normal hexane against the soil or sediment Is added to the soil or sediment in the extraction tank by a ratio in a volume ratio of 1: 2, and then extracted in the same manner as the extraction process for polychlorinated biphenyl compounds in the trans oil. Depending on the processing conditions in the processing, powerful ultrasonic waves are applied to the liquid to be processed and the debris in the extraction tank from the lower part. By adding more intense microscopic agitation action, the extraction treatment for polychlorinated biphenyl compounds is promoted, and the treatment for 10-15 minutes in the extraction treatment time for complete extraction treatment is more effective than soil or sediment. The extraction process for polychlorinated biphenyl compounds can be completed completely. Further, after stopping all the devices involved in the extraction process, the processing liquid that has completed the extraction process is extracted from the extraction processing tank and introduced into the vacuum filtration processing tank, and the liquid to be processed is vacuum filtered. After being treated and vacuum filtered, the extracted moisture generated by the moisture contained in the soil or sediment is separated from the treatment liquid, and the separated extracted moisture is discarded and the moisture is removed. It is possible to complete the extraction treatment for the polychlorinated biphenyl compounds by using the extraction treatment liquid in a state of not containing. In addition, the earth or stone for the residue in the extraction treatment tank and the residue after the filtration treatment is washed again with normal hexane and discarded, and the normal hexane used for the washing treatment is continuously. In order to extract the polychlorinated biphenyl compound, it is used again as a solvent. Next, in the covered electric wire, with respect to the covered portion of the rubber or synthetic resin containing the polychlorinated biphenyl compound, the inner electric wire is removed so that only the covered portion is contained, and the polychlorinated biphenyl compound is contained. The coated part is introduced into the extraction tank made of titanium, the uppermost part of the extraction tank is completely closed by the set of the upper plate made of titanium, the inside of the extraction tank is completely sealed, and the chemical The metering pump interlocked with the flow rate controller is operated, and dimethylformamide is injected and added to the coating portion in the extraction treatment tank at a ratio of 1: 2 in the volume ratio with respect to the coating portion. Depending on the treatment conditions in the dissolution treatment similar to the state of the extraction treatment for polychlorinated biphenyls compounds in trans oil, The coating part and dimethylformamide are dissolved in the coating part in rubber or synthetic resins by applying strong ultrasonic vibration from the lower part and adding intense micro-stirring action by strong ultrasonic wave. In the dissolution treatment time for accelerating the treatment and completely dissolving the coated portion with dimethylformamide, the dissolution treatment of the coated portion can be completed completely by treatment for 40 to 50 minutes. Furthermore, after stopping all the devices involved in the dissolution treatment, the dissolution treatment liquid after completion of the dissolution treatment is extracted from the extraction treatment tank and introduced into the vacuum filtration treatment tank. Dissolve the solution by vacuum filtration and re-introduce the solution after completion of the vacuum filtration process into the extraction tank, and then operate the other chemical flow rate controller linked metering pump. Normal hexane is quantified in the extraction processing tank based on the ratio of normal hexane, which is insoluble in dimethylformamide to the processing solution and has a soluble extractability for polychlorinated biphenyl compounds, in a 1: 1 volume ratio. The same extraction as that of the extraction treatment for the polychlorinated biphenyl compounds in the above-mentioned transformer oil Depending on the processing conditions in the processing, depending on the state in which strong ultrasonic vibration is applied to the liquid to be processed in the extraction processing tank from the lower part of the extraction processing tank, and intense microscopic stirring action is added by the strong ultrasonic waves. The extraction treatment for the polychlorinated biphenyl compounds is promoted by normal hexane injected and added to the solution to be treated by the dissolution treatment liquid of the coating portion containing the polychlorinated biphenyl compounds in the extraction treatment tank. Extraction treatment for polychlorinated biphenyl compounds is performed, and the extraction treatment for polychlorinated biphenyl compounds contained in the liquid to be treated is promoted under various treatment conditions and ultrasonic vibration / stirring action for complete extraction. Dissolving the coated part by processing for 10-15 minutes in the extraction processing time for processing You can complete the extraction process for perfectly polychlorinated biphenyls compounds than the liquid to be treated in. Furthermore, after stopping all the devices involved in the extraction processing, the extraction processing device is allowed to stand, so that the liquid to be processed in the extraction processing tank is generally a two-layer portion including an upper layer portion and a lower layer portion. The upper layer part is separated into a solution treated with normal hexane and a polychlorinated biphenyl compound, and the lower layer part is separated into a solution treated with dimethylformamide and rubber or synthetic resins. It is done. Next, after detecting the position on both sides of the boundary, the portion of the solution treated with dimethylformamide and rubber or synthetic resin located in the lower layer in the extraction tank is extracted from the extraction tank. Extraction treatment is performed outside the system of the apparatus, and removal treatment is performed. In the extraction treatment tank, the extraction treatment liquid for polychlorinated biphenyl compounds with normal hexane remains, and the extraction treatment for polychlorinated biphenyl compounds can be completed completely. . In addition, the portion of the solution treated with dimethylformamide and rubber or synthetic resin extracted outside the system of the extraction processing apparatus is subjected to vacuum distillation using a vacuum distillation processing apparatus, and dimethylformamide is recovered and processed again. It is used for the dissolution treatment of the coated portion, and the remaining rubber or synthetic resin residues are reused. Next, in order to perform ultrasonic decomposition processing on the extraction processing liquid that has completed the extraction processing for the polychlorinated biphenyl compounds, the ultrasonic processing tank made of titanium is used for the extraction processing liquid by a transfer pump for ultrasonic decomposition processing. 2/3 of the total amount of sodium alcoholate or metallic sodium required for the chemical reaction for decomposing the polychlorinated biphenyl compound by operating the metering pump linked with the flow rate control device for chemicals. Depending on the ratio of the amount of the lysate, the fixed amount is injected and added to the liquid to be treated in the ultrasonic decomposition treatment tank, and then the vacuum pump outside the system of the ultrasonic decomposition treatment apparatus is operated, 5 × 10 ^-4 The high vacuum state by Torr is kept, and the high vacuum state is maintained by a digital vacuum constant device. Next, a water cooling jacket is attached to the outside of the ultrasonic decomposition treatment tank, and the water cooling device outside the ultrasonic decomposition treatment system is operated to cool the water. The cooling water circulation pump outside the system of the sonication treatment apparatus is operated, the cooling water is introduced into the water cooling jacket, the cooling water is circulated in the water cooling jacket, and the liquid to be treated in the ultrasonic decomposition treatment tank is cooled. The temperature of the liquid to be treated in the ultrasonic decomposition treatment tank is adjusted by the temperature controller, and the temperature of the liquid to be treated in the ultrasonic decomposition treatment tank is lowered by 0 to 4 ° C. Depending on the processing conditions in the low-temperature state by high vacuum and cooling treatment, the liquid to be processed in the ultrasonic decomposition treatment tank The processing circulation pump is operated and circulated in a state with a low flow rate. However, the flow rate for the liquid to be processed needs to be irradiated with a powerful ultrasonic wave to correspond to the irradiation reaction time. Yes, the flow rate corresponding to the irradiation reaction time by powerful ultrasonic waves is set as low as possible, and at the highest flow rate, the circulation process is performed at a low flow rate of 10 to 15 m / min. It is circulated at a low flow rate and returned to the ultrasonic decomposition treatment tank again, and in the process of circulating the liquid to be treated, an ultrasonic decomposition processing unit is installed at an arbitrary position in the middle. In a state perpendicular to the progressing flow of the liquid to be treated that is circulated in the ultrasonic decomposition processing unit at a low flow rate, the liquid to be processed to be circulated in the ultrasonic decomposition processing unit is introduced at a low flow rate. The ultrasonic oscillator is attached in contact, and the ultrasonic oscillation output is adjusted by the ultrasonic generator and the ultrasonic wattmeter. The effective output is 1,200 W, the frequency (frequency) 19, from the ultrasonic oscillator. 5KHz, amplitude 60-80μ and ultrasonic intensity 50W / cm ² Oscillation is applied to the liquid to be processed that is circulated by powerful ultrasonic waves, and the liquid to be processed is vibrated vigorously by irradiation with strong ultrasonic waves. Due to the effect of the generated cavitation, a relative velocity is generated between the solvent and the polychlorinated biphenyl compound in the liquid to be treated, and a frictional force is exerted between them, and the polychlorinated biphenyl is caused by the frictional force. The main chain bond and side chain bond are actively cleaved in the binding molecular chain by the compound, and the benzene ring is also cleaved, and the polychlorinated biphenyl compound contained in the liquid to be treated is gradually decomposed. At the time 20 to 23 minutes after the time when the ultrasonic decomposition process is started on the liquid to be processed, As for clay, the clay suddenly descended, and when the clay descended, the polychlorinated biphenyl compounds were in a state of being decomposed by ultrasonic waves, and the polychlorinated biphenyl compounds were ultrasonically decomposed. The ultrasonic decomposition treatment is completed 25 to 30 minutes after the start of the operation. Next, the polychlorinated biphenyl compound contained in the treatment solution completed for the ultrasonic decomposition treatment contains a portion due to undecomposition. Furthermore, in order to completely decompose the polychlorinated biphenyl compounds, the treatment liquid that has been subjected to the ultrasonic decomposition treatment in the ultrasonic decomposition treatment tank is attached to the lower part of the ultrasonic decomposition treatment tank. Operate the liquid discharge solenoid valve to open it, and ultrasonically decompose the treatment liquid that has been completed for the ultrasonic decomposition process using the transfer pump for UV decomposition processing that is synchronized with the treatment liquid discharge solenoid valve. Extraction is performed outside the system of the apparatus, and at the same time, it is introduced into the ultraviolet decomposition tank by a transfer pump for ultraviolet decomposition. Next, in order to completely decompose the undecomposed portion of the polychlorinated biphenyl compounds contained in the treatment liquid, the ultrasonic decomposition is performed on the treatment liquid introduced into the treatment tank. Chemical reaction to completely decompose the polychlorinated biphenyl compounds by introducing the treatment liquid after completion of the treatment into the UV decomposition treatment tank and operating the metering pump linked with the flow control device for the first chemical. The amount of the remaining sodium alcoholate or metal sodium required for the injection is added to the liquid to be treated in the ultraviolet decomposition treatment tank, and the reaction rate is accelerated for the ultraviolet decomposition treatment. In order to achieve this, the second chemical addition amount control device interlocking screw fixed supply device is operated, and the liquid dioxide having photoelectric conductivity with respect to the liquid to be processed is used. The amount of titanium dioxide is introduced and added to the liquid to be treated in the ultraviolet decomposition treatment tank at a ratio of 1 to 4% in the volume ratio, and the vacuum pump outside the system of the ultraviolet decomposition treatment apparatus is operated to perform ultraviolet decomposition. 5 x 10 inside the treatment tank ^-4 A high vacuum state is maintained by Torr, the high vacuum state is maintained by a digital vacuum constant device, and then a water cooling jacket is contacted and attached to the outside of the ultraviolet decomposition treatment tank, and water outside the system of the ultraviolet decomposition treatment device is contacted. Operate the cooling device, cool the water, operate the cooling water circulation pump outside the system of the UV decomposition treatment device to the cooled cooling water, introduce the cooling water into the water cooling jacket, inside the water cooling jacket Cooling water flows and circulates, the liquid to be treated in the ultraviolet decomposition treatment tank is cooled with cooling water, and the temperature of the liquid to be treated in the ultraviolet decomposition treatment tank is adjusted to 0 in the liquid to be treated by adjusting the temperature of the temperature controller. Maintain a low temperature state at -4 ° C, and attach an ultrasonic oscillator to the lower part of the UV decomposition treatment tank. By the meter, to adjust the oscillation output of the ultrasonic wave, the effective output 600W from ultrasonic generator, the frequency (frequency) 26 kHz, amplitude 200 [mu], intensity 1.0 W / cm ² Oscillates strong ultrasonic waves by the treatment liquid in the UV decomposition treatment tank and gives strong vibration from the lower part of the liquid to be treated. A proper stirring action is added to accelerate the UV decomposition treatment reaction. Next, in a lamp house unit made of quartz glass, a high-pressure mercury lamp or a high-pressure xenon lamp with a rated power of 5 KW at a rate of 100 W with respect to 1% of chlorine contained in the decomposition product at the innermost position is inserted, In order to cool the high-pressure mercury lamp or high-pressure xenon lamp, the space is equipped with a partition wall made of quartz glass with a double circular state, and the space is equipped with a high-pressure mercury lamp inserted into the innermost part of the lamp house unit. Alternatively, a space is provided between the outer wall of the high-pressure xenon lamp and the circular partition wall made of quartz glass, and the power consumption is 250 W outside the system of the lamp house unit, and the realized pressure is 4 kg / cm. ² Then, the air pump is operated with the air flow rate of 95 l / min, the outside air is introduced into the air cooling jacket that is equipped, and the outside air introduced from the other end of the air cooling jacket is heated by the high pressure mercury lamp or the high pressure xenon lamp. The high-temperature mercury lamp or high-pressure xenon lamp is cooled by an air flow, and a pure water cooling jacket made of quartz glass is welded to the outside of the air-cooling jacket that is cooled by the air flow. Then, the pure water cooling device and the ion exchanger outside the lamp house unit system are operated to cool the high-purity pure water, and the high-purity pure water is cooled to a low temperature of 2 to 3 ° C. , And operate a cooling pure water circulation pump with a yield of 30 l / min outside the system of the device, Is introduced into the pure water cooling jacket, and the high purity pure water in the pure water cooling jacket is fluidized and circulated to cool the amount of heat emitted from the high-pressure mercury lamp or high-pressure xenon lamp and the radiated heat rays. The high pressure mercury lamp or high pressure xenon lamp is cooled by the air flow and the cooled pure water by introducing and discharging air from the outside of the apparatus to the lamp house unit and circulating the purified pure water with high purity. Yes, as a result, the ultraviolet ray having less heat rays than the lamp house unit is radiated. Next, the lamp house unit is installed above the surface of the liquid to be treated in the ultraviolet decomposition treatment tank or in the liquid to be treated, and the contact surface between the inner and outer wall surfaces of the ultraviolet decomposition treatment tank and the lamp house unit. Must be completely sealed with a sealant made of rubber such as silicon rubber or plastic resin, and must be completely sealed so that it is resistant to high-vacuum conditions and does not absorb air. In the ultraviolet decomposition treatment tank, the treatment liquid is irradiated with ultraviolet rays with less heat rays than the lamp house unit, and the treatment conditions in various states in which the ultraviolet decomposition treatment reaction is induced, the polychlorinated biphenyl compounds are not decomposed. UV decomposition reaction is applied to the part caused by the chemical, and the polychlorinated biphenyl compounds contained in the liquid to be treated As for the UV decomposition treatment time for completely decomposing the undecomposed part of the polychlorinated biphenyl compounds contained in the liquid to be treated, the part by The decomposition treatment for the polychlorinated biphenyl compounds can be completed completely by the ultraviolet decomposition treatment for 27 to 30 minutes from the time of starting the ultraviolet decomposition treatment reaction. Furthermore, with respect to the polychlorinated biphenyl compounds, after the ultraviolet decomposition treatment reaction is passed and the decomposition treatment is completed completely, sodium chloride / muconic acid and a very small amount of biphenyl are formed in the decomposition residue. Next, for the processing liquid containing the decomposition residue in the UV decomposition treatment tank, the processing liquid discharge electromagnetic valve attached to the lower part of the UV decomposition treatment tank is operated to open it, and the synchronized vacuum The treatment liquid that has been subjected to UV decomposition treatment and completely decomposed polychlorinated biphenyl compounds with a distillation transfer pump is extracted out of the system of the UV decomposition treatment apparatus, and at the same time, the treatment liquid is removed with the transfer pump. It is introduced into the vacuum distillation treatment tank. Next, with regard to the vacuum distillation treatment for separating each of the solvent contained in the liquid to be treated introduced into the vacuum distillation treatment tank and the decomposition residue due to the polychlorinated biphenyl compound, ultraviolet decomposition treatment is performed. The completed treatment liquid is introduced into a vacuum distillation treatment tank and 5 × 10 5 in the vacuum distillation treatment tank by a vacuum pump outside the system of the vacuum distillation treatment apparatus. ^-4 A high vacuum state is maintained by Torr, and the high vacuum state is further maintained by a digital vacuum constant device. Next, a heat treatment device is attached to the lower part of the vacuum distillation treatment tank, and the vacuum distillation treatment is performed by the heat treatment device. The solvent contained in the liquid to be treated in the tank and the decomposition residue of the polychlorinated biphenyl compound are indirectly heated, and the solvent of the liquid to be treated is at a temperature higher than the boiling point in a high vacuum state. The temperature of the liquid to be treated is adjusted by the first temperature controller to maintain the temperature of the liquid to be treated, and the solvent contained in the liquid to be treated is heated to a temperature higher than the boiling point in a high vacuum state. After the treatment, the solvent of the liquid to be treated becomes a solvent vapor state depending on the state of the solvent, and is raised in the vacuum distillation treatment apparatus. Furthermore, the temperature below the boiling point of the solvent is adjusted by the second temperature controller by the serpentine tube for the cooling processing device provided at the upper part in the vacuum distillation processing device, and the cooling process is performed by adjusting the temperature state by the second temperature controller. The raised solvent vapor is cooled at a temperature equal to or lower than the boiling point of the solvent, the solvent vapor is condensed and liquefied, and the condensate is installed in the lower part of the cooling serpentine in the cooling section in the vacuum distillation treatment apparatus. The solvent in the condensate is collected and stored by the drop receiving and collecting device, and the collected solvent is opened by the automatic opening / closing operation of the first solenoid valve, and is recovered outside the system of the vacuum distillation processing apparatus. Automatic in the second solenoid valve, which is introduced into the solvent storage tank and the recovered solvent is installed in the lower part of the recovery solvent storage tank By the opening and closing operation, the solvent obtained by collecting process is in an open state be excised processed outside the system of the vacuum distillation apparatus, it can complete the perfect recovery process of the solvent. Next, after completing the recovery process for all the solvents contained in the liquid to be processed in the vacuum distillation tank by vacuum distillation process, all the devices involved in the vacuum distillation process are stopped and vacuum is applied. After the residue in the distillation tank is cooled and the vacuum distillation process is completed completely, the decomposition residue due to the polychlorinated biphenyl compounds remaining in the vacuum distillation tank is cooled and vacuumed. The extraction process is performed outside the distillation processing system. Next, when the oil content is contained in the extracted decomposition residue, the separation residue is introduced into the separation treatment tank for the separation treatment for removing the oil from the decomposition residue, and further the separation treatment tank. The upper part of the separator is closed with an upper plate to keep the inside of the separation processing tank sealed, and then the first chemical flow control device linked metering pump is operated to prevent decomposition residue due to polychlorinated biphenyl compounds. Normal hexane is injected into the decomposition residue of the polychlorinated biphenyl compounds at a ratio of 1: 2 in the volume ratio of normal hexane, and then separated by a vacuum pump outside the separation treatment system. Within 5 × 10 ^-4 The high vacuum state is caused by Torr, and the high vacuum state is maintained by a digital vacuum constant device. Next, the water cooling jacket is contacted and installed on the outside of the decomposition treatment tank, the water cooling device outside the system of the separation treatment device is operated, the water is cooled, and the cooling water subjected to the cooling treatment is Operate the cooling water circulation pump outside the system of the separation treatment system, introduce cooling water into the water cooling jacket, flow and circulate the cooling water in the water cooling jacket, and separate by the cooling water introduced into the water cooling jacket The liquid to be treated containing normal hexane and decomposition residue from polychlorinated biphenyl compounds in the treatment tank is cooled, and the temperature of the liquid to be treated in the separation tank is adjusted with a temperature controller. Thus, the low temperature state of 0 to 4 ° C. is maintained at the temperature of the liquid to be treated. Further, an ultrasonic oscillator is attached to the lower part of the separation treatment tank, and the ultrasonic oscillation output is adjusted by the ultrasonic generator and the ultrasonic wattmeter, and the effective output 600 W, frequency ( Frequency) 26KHz, amplitude 200μ, ultrasonic strength 1.0W / cm ² By oscillating the powerful ultrasonic wave by the liquid to be processed, the liquid to be processed in the separation processing tank is vibrated by the strong ultrasonic wave from the lower part in the separation processing tank, Polychlorinated biphenyl compounds are extracted with normal hexane to extract the oil contained in the decomposition residue of polychlorinated biphenyl compounds under various processing conditions in which intense microscopic stirring action is added by ultrasonic waves. The extraction processing time for extracting the oil from the decomposition residue by the extraction process is 15 to 20 minutes, so that the oil contained in the decomposition residue by the polychlorinated biphenyl compound is completely extracted and extracted. After completing the above, all the devices involved in the extraction process are stopped. Next, the metering pump linked with the flow control device for the second chemical is operated, and the furfural of the solvent due to the poor solubility of the normal hexane and the oil component with respect to the decomposition residue due to the polychlorinated biphenyl compound is in a ratio of 1: 1 volume ratio Then, the fixed amount of furfural is injected and added to the liquid to be treated in the separation treatment tank, and then all the devices are operated again to return to the state under the same treatment conditions as described above. Solvent separation treatment to completely remove the solvent to be treated by adding strong ultrasonic vibration and intense microscopic stirring action depending on the treatment conditions in the low temperature state by high vacuum and cooling treatment Regarding the time, after performing the solvent separation process for 10 to 15 minutes, all the apparatuses involved in the solvent separation process were stopped and the separation process was performed. In After standing device, for the liquid to be treated in the separation treatment tank is being the separation process in the second layer portion of the upper portion and the lower portion by the difference in specific gravity. The upper layer portion is a mixture of normal hexane and oil, and the lower layer portion is separated into a mixture of furfural and a decomposition residue of a polychlorinated biphenyl compound. Furthermore, the position of the boundary surface with respect to the two-layer portion is determined by the boundary detection device using the glass tube measuring device or the conductivity liquid level measuring device that is equipped outside the system from the separation processing tank in the liquid to be processed that has been separated into the two-layer portion. It is detected and measured, and then introduced again into the vacuum distillation tank in order to fractionate the solvent with normal hexane and furfural contained in the treatment liquid separated into the upper layer part and the lower layer part. The vacuum distillation treatment tank is divided into two tanks, and the treatment liquid discharge solenoid valve attached to the lower part of the separation treatment tank is operated to open, and the vacuum is synchronized with the operation of the treatment liquid discharge solenoid valve. Operate the transfer pump for the distillation process to remove the decomposition residue from the furfural and polychlorinated biphenyl compounds located in the lower layer in the separation tank. The mixed solution was first introduced into one of the vacuum distillation treatment tanks, and the mixed solution with the furfural and polychlorinated biphenyl compound decomposition residue was introduced into one of the vacuum distillation treatment tanks to complete the process. Later, the transfer pump and the treatment liquid discharge solenoid valve are operated to stop the blockage. Furthermore, in order to introduce the mixed liquid of normal hexane and oil, which was located in the upper layer in the separation processing tank, into the other tank in the vacuum distillation processing tank, the processing liquid discharge solenoid valve by the lower part of the separation processing tank is activated again. The vacuum distillation treatment transfer pump is operated at the same time to synchronize with the operation state of the treatment liquid discharge solenoid valve, and the liquid mixture of normal hexane and oil is removed from the other tank in the vacuum distillation treatment tank. After introducing the mixed liquid of normal hexane and oil into the other tank in the vacuum distillation tank from the separation tank, the vacuum distillation transfer pump and the separation liquid discharge solenoid valve Are operated to stop the blockage. Next, the two types of mixed liquid introduced into the two separate tanks separately provided in the vacuum distillation tank are simultaneously vacuum distilled, and the temperature difference between the boiling points of normal hexane and furfural [normal Hexane, boiling point 68.7 ° C. (760 mmHg), furfural, boiling point 161.8 ° C. (760 mmHg)], normal hexane and then furfural are recovered by vacuum distillation. Furthermore, after two kinds of solvents by normal hexane and furfural are completely recovered and completed by vacuum distillation, oil and polychlorination are separately contained in two separate tanks with two vacuum distillation tanks. There are two types of residue, biphenyl compounds and decomposition residues, which are divided into two tanks with separate vacuum distillation treatment tanks, respectively, depending on the oil and polychlorinated biphenyl compounds remaining in separate tanks. The decomposition residue is extracted outside the system of the vacuum distillation processing apparatus according to the state of being separately provided. Next, in the case where no oil component is contained in the decomposition residue of the polychlorinated biphenyl compound, it is not necessary to perform a separation treatment. Furthermore, after two kinds of mixed liquids are vacuum-distilled with a vacuum distillation processing device and the solvent is recovered by fractional distillation, the polychlorinated biphenyl compounds are continuously decomposed for the various recovered solvents. Therefore, each of the solvents in the various types is used again at a necessary time. Next, after passing through the separation process and vacuum distillation treatment, the oil component extracted from the vacuum distillation treatment tank and the decomposition residue by the polychlorinated biphenyl compound are separately recovered and processed. It is reused in heat medium oil / lubricating oil and the like, and the decomposition residue is separated again, and a portion such as sodium chloride is extracted and reused industrially. Further, the portion that cannot be used again is incinerated by an incinerator.
(Effect of the Invention) According to the decomposition treatment method and the decomposition treatment apparatus for polychlorinated biphenyl compounds according to the present invention, the decomposition treatment method for the combination of physical and chemical decomposition treatment in the decomposition treatment for the polychlorinated biphenyl compounds. It is highly efficient with respect to polychlorinated biphenyl compounds by decomposing each of the decomposition treatment methods by extraction treatment, ultrasonic decomposition treatment, ultraviolet ray decomposition treatment, vacuum distillation treatment, separation treatment with each decomposition treatment device in sequence. Therefore, the decomposition treatment can be carried out and a decomposition rate of 100% can be reliably realized, and the decomposition treatment can be completed completely and efficiently for the polychlorinated biphenyl compounds. Next, with respect to the extraction treatment of polychlorinated biphenyl compounds from the target products containing polychlorinated biphenyl compounds, the extraction solvent with isopropyl alcohol / acetone and normal hexane was applied to the treatment object introduced into the extraction treatment tank. The extraction process of the polychlorinated biphenyl compound can be completed in a short time by injection. Next, regarding the ultrasonic decomposition process by the decomposition process for polychlorinated biphenyl compounds, the sodium alcoholate or metal sodium is injected and added to the liquid to be processed after the extraction process introduced into the ultrasonic decomposition tank is completed. A strong ultrasonic wave having a large acceleration is oscillated with respect to the liquid, and the liquid to be treated is constituted by the action of the ultrasonic wave itself and the effect of cavitation generated by the ultrasonic wave on the polychlorinated biphenyl compounds. A relative velocity occurs between the solvent and the polychlorinated biphenyl compound, and a frictional force is exerted between the solvent and the polychlorinated biphenyl compound. Side chain bonds are actively cleaved, dissociated, and released into a free state. Sodium alcoholate or is binding and sodium molecules by sodium metal is than sodium chloride is produced and benzene ring also dissociated benzene ring in the free state is of being cleaved processed muconic acid is produced. Furthermore, the treatment solution that has completed the reaction by ultrasonic decomposition treatment contains a portion of the polychlorinated biphenyl compound that has not been decomposed. Therefore, in order to completely decompose the polychlorinated biphenyl compound, the treatment solution is treated with ultraviolet light. Decompose it. Next, for UV decomposition treatment that completely decomposes polychlorinated biphenyl compounds, a fixed amount of sodium alcoholate or sodium metal is injected and added to the liquid to be treated introduced into the UV decomposition treatment tank, and photoelectric conductivity is further increased. Introduce and add a fixed amount of titanium dioxide, and irradiate the liquid to be treated with strong ultraviolet rays to maintain the ground state of the undegraded portion of the polychlorinated biphenyl compounds by ultraviolet decomposition. The high energy that the photon energy of the ultraviolet light is retained is absorbed by the ground state molecule by the irradiation process of the strong ultraviolet light, and the molecule is higher in the molecule due to the undecomposition of the polychlorinated biphenyl compound. When transitioning to the energy level, the molecule becomes photoexcited and obtains photoexcitation energy within the molecule. The activated polychlorinated biphenyl compounds act on the other undegraded molecules, and the undegraded molecules become the other undegraded molecules. The automatic chain reaction proceeds one after another by a reaction that imparts excitation energy to the molecule due to decomposition, and after the excitation energy is released to other undecomposed molecules, it is restored to the original ground state again and deactivated. It becomes. Next, in the molecule to which the excitation energy is applied, the chlorine molecule that is bound by the side chain bond to the molecular chain of the polychlorinated biphenyl compound that is undecomposed is brought into the dissociated state and freed at the same time. It is done. Furthermore, all the chlorine molecules that have been brought into the free state are combined with sodium alcoholate that has been previously added to the liquid to be treated or sodium molecules by metallic sodium to form sodium chloride. The molecule is in an extinguished state. Therefore, ultraviolet decomposition treatment is performed on the undecomposed molecules of the polychlorinated biphenyl compounds by the ultraviolet decomposition treatment apparatus to complete the decomposition treatment completely, and after the polychlorinated biphenyl compounds are completely decomposed, the decomposition remains. The product contains sodium chloride, muconic acid and a small amount of biphenyl. Furthermore, a vacuum distillation treatment is performed to separate the solvent and decomposition residue constituting the treatment liquid. Next, regarding the vacuum distillation treatment for separating the solvent and decomposition residue contained in the treatment liquid that has completed the ultraviolet decomposition treatment, the solvent and decomposition residue introduced into the vacuum distillation treatment tank are contained. A cooling device in which the liquid to be treated is indirectly heated at a temperature above the boiling point of the solvent in a high vacuum state, and the inside of the vacuum distillation treatment tank is raised by the state of the solvent vapor and is installed at the upper position By a cooling process in a temperature state below the boiling point of the solvent, condensing the solvent vapor to a liquefied state, extracting the solvent in the condensate out of the system of the vacuum distillation processing apparatus, recovering it, and vacuum distillation processing tank After subjecting the liquid to be treated in the vacuum distillation process to the complete recovery of the solvent, and separating the solvent and decomposition residue, It cause excised processed outside the system of the vacuum distillation apparatus decomposition residues which are residual on empty distillation treatment tank. Further, when the oil content is contained in the extracted decomposition residue, it is necessary to completely remove the oil component, so that the oil component is separated from the decomposition residue. Next, regarding the separation treatment for the oil contained in the decomposition residue extracted from the vacuum distillation processing apparatus, normal hexane is quantified with respect to the decomposition residue by the polychlorinated biphenyl compound introduced into the separation treatment tank. Inject and add, the oil content in the decomposition residue is dissolved and extracted in normal hexane, and the oil content is completely extracted from the decomposition residue and completed, and then the amount of furfural is injected and added to the liquid to be processed. And by subjecting the liquid to be treated to a solvent separation process, and after completely completing the solvent separation process for the liquid to be treated, the separation processing apparatus is allowed to stand, so that the upper part of the liquid to be treated is caused by the difference in specific gravity. And the lower layer part are separated, the upper layer part is mixed with normal hexane and oil, and the lower part part is full Than it is the mixture and the separation of the decomposition residue by Le and polychlorinated biphenyls compound. Next, after carrying out detection measurement processing of both boundary surfaces, in order to distill the solvent in normal hexane and furfural contained in each of the two kinds of mixed liquids and separate the mixed liquids, It is introduced again into the vacuum distillation tank, but it is preliminarily divided into two tanks in the vacuum distillation tank, and one of the tanks in the vacuum distillation tank is decomposed by furfural and polychlorinated biphenyl compounds. And a mixed liquid of normal hexane and oil is introduced into the other tank. Next, regarding the vacuum distillation process for separately introducing and mixing each of the two types of liquid mixture into the two tanks in the vacuum distillation tank, each of the two tanks in the vacuum distillation tank is separated. In each of the two types of mixed liquids introduced in the above, the vacuum distillation treatment by fractional distillation treatment was performed due to the temperature difference of the boiling points with respect to the solvent in the normal hexane and furfural contained in the mixed liquid for each, Normal hexane and then furfural are recovered by vacuum distillation. In addition, after complete recovery of the two kinds of solvents in normal hexane and furfural, the oil component and the polychlorinated biphenyl compound are separately provided in two separate tanks that are provided separately for the vacuum distillation tank. The decomposition residue is left behind. Next, the oil component remaining in each of the two separate tanks provided with the division and the decomposition residue due to the polychlorinated biphenyl compounds are separately extracted from the individual tanks outside the vacuum distillation processing system. In the case where no oil content is contained in the decomposition residue due to the polychlorinated biphenyl compound, a separation process is necessary. Further, after the vacuum distillation treatment by the vacuum distillation treatment apparatus and the solvent recovery treatment by fractional distillation treatment, in order to continuously decompose the polychlorinated biphenyl compounds with respect to the various recovery solvents, in various ways Each of the solvents is used again depending on the time required. Next, the oil components extracted and recovered separately from the individual vacuum distillation treatment tanks for the two tanks that are separately equipped in the vacuum distillation treatment tanks are used as heat medium oils and lubricating oils in the industrial field. The decomposed residue that has been recovered is separated again, and a portion such as sodium chloride is extracted and industrially reused. In addition, the portion that cannot be reused is incinerated by the incineration processing apparatus in a state where secondary pollution does not occur. Therefore, in the decomposition process for polychlorinated biphenyl compounds, the extraction process, the ultrasonic decomposition process, and the ultraviolet decomposition process are steps in a complete decomposition process, and the vacuum distillation process and separation process are reused for the decomposition residue. This is a process for recycling. Furthermore, with regard to the decomposition treatment for polychlorinated biphenyl compounds, the decomposition treatment process is sequentially performed by each decomposition treatment apparatus and completed, and the complete decomposition treatment for polychlorinated biphenyl compounds by 100% is completed. It can be polluted. Next, the decomposition treatment for the polychlorinated biphenyl compounds according to the present invention is an industrial-scale decomposition treatment capable of performing a large amount of decomposition treatment per hour, and is necessary for the decomposition treatment of the decomposition treatment apparatus and the accessory device on the industrial scale. Since the equipment is mounted on a trailer vehicle and set to be decomposed on the vehicle, mobility for the decomposition process can be obtained, so it is necessary to transport and move the polychlorinated biphenyl compounds, which are specific dangerous substances, to decompose them. Therefore, there is no danger of moving the polychlorinated biphenyl compounds, and there is no secondary pollution in the surrounding environment due to a large amount of industrial decomposition.
[Brief description of the drawings]
FIG. 1 is a process explanatory diagram showing an embodiment of the present invention. Each of the following drawings is an example of an apparatus according to the present invention.
[Fig. 2] Arrangement of tools for extraction processing device
FIG. 3 is a front view of an extraction processing apparatus.
FIG. 4 is a left side view of the extraction processing apparatus.
FIG. 5 is a right side view of the extraction processing apparatus.
[Fig. 6] Arrangement of instruments for ultrasonic decomposition apparatus
FIG. 7 is a front view of an ultrasonic decomposition processing apparatus.
FIG. 8 is a left side view of the ultrasonic decomposition processing apparatus.
FIG. 9 is a right side view of the ultrasonic decomposition processing apparatus.
[Fig. 10] Arrangement of tools for UV decomposition equipment
FIG. 11 is a front view of an ultraviolet decomposition processing apparatus.
FIG. 12 is a left side view of the ultraviolet decomposition processing apparatus.
FIG. 13 is a right side view of the ultraviolet decomposition processing apparatus.
FIG. 14 is a side view of a lamp house unit with respect to an ultraviolet decomposition apparatus.
FIG. 15 is a cross-sectional view of the lamp house unit taken along the line AA with respect to the ultraviolet decomposition processing apparatus.
[Fig. 16] Arrangement of tools for vacuum distillation processing equipment
FIG. 17 is a front view of a vacuum distillation processing apparatus.
FIG. 18 is a left side view of the vacuum distillation processing apparatus.
FIG. 19 is a right side view of the vacuum distillation processing apparatus.
[Fig. 20] Arrangement of tools for the separation processing device
FIG. 21 is a front view of a separation processing apparatus.
FIG. 22 is a left side view of the separation processing apparatus.
FIG. 23 is a right side view of the separation processing apparatus.
[Explanation of symbols]
Extraction processing device
1 Extraction processing tank
2 Upper plate for extraction process
3 Chemical storage tank for extraction process
4 Chemical flow control device linked metering pump for extraction processing
5 Vacuum pump for extraction process
6 Digital vacuum constant device for extraction processing
7 Water-cooling jacket for extraction processing
8 Water cooling device for extraction process
9 Cooling water circulation pump for extraction treatment
10 Water storage tank for extraction treatment
11 Ultrasonic oscillator for extraction processing
12 Ultrasonic generator for extraction process
13 Ultrasonic power meter for extraction process
14 Solvent discharge solenoid valve for extraction process
90 Temperature controller for extraction process
Ultrasonic decomposition processing equipment
15 Transfer pump for ultrasonic decomposition
16 Ultrasonic decomposition tank
17 Chemical storage tank for ultrasonic decomposition treatment
18 Chemical flow control device linked metering pump for ultrasonic decomposition treatment
19 Vacuum pump for ultrasonic decomposition
20 Digital vacuum constant apparatus for ultrasonic decomposition treatment
21 Water-cooled jacket for ultrasonic decomposition treatment
22 Water cooling device for ultrasonic decomposition treatment
23 Cooling water circulation pump for ultrasonic decomposition treatment
24 Water storage tank for ultrasonic decomposition
25 Processed liquid circulation pump for ultrasonic decomposition treatment
26 Ultrasonic decomposition processing unit for ultrasonic decomposition processing
27 Ultrasonic oscillator for ultrasonic decomposition treatment
28 Ultrasonic generator for ultrasonic decomposition treatment
29 Ultrasonic power meter for ultrasonic decomposition treatment
30 Solenoid discharge solenoid valve for ultrasonic decomposition treatment
91 Temperature controller for ultrasonic decomposition treatment
UV decomposition treatment equipment
31 Transfer pump for UV decomposition treatment
32 UV decomposition tank
33 First chemical storage tank for UV decomposition treatment
34 Flow rate control device linked metering pump for the first chemical for UV decomposition treatment
35 Second chemical storage tank for UV decomposition treatment
36 Additive control device for second chemical for UV decomposition treatment Interlocked screw quantitative supply device
37 Vacuum pump for UV decomposition
38 Digital vacuum constant apparatus for UV decomposition treatment
39 Water-cooled jacket for UV decomposition treatment
40 Water cooling device for UV decomposition treatment
92 Temperature controller for UV decomposition treatment
41 Cooling water circulation pump for UV decomposition treatment
42 Water storage tank for UV decomposition
43 Ultrasonic oscillator for UV decomposition
44 Ultrasonic generator for UV decomposition
45 Ultrasonic power meter for UV decomposition treatment
46 Lamphouse unit for UV decomposition treatment
47 High-pressure mercury lamp or high-pressure xenon lamp
48 Air cooling jacket for lamp cooling treatment
49 Air pump for lamp cooling treatment
50 Water cooling jacket for lamp cooling treatment
51 Pure water cooling device for lamp cooling treatment
52 Ion exchanger for lamp cooling treatment
53 Pure water storage tank for lamp cooling treatment
54 Solenoid discharge solenoid valve for UV decomposition
Vacuum distillation processing equipment
55 Transfer pump for vacuum distillation treatment
56 Vacuum distillation tank
57 Vacuum pump for vacuum distillation
58 Digital vacuum constant apparatus for vacuum distillation treatment
59 Heating device for vacuum distillation treatment
60 First temperature controller for vacuum distillation treatment
61 Solvent vapor condensing part for vacuum distillation treatment
62 Cooling serpentine for vacuum distillation treatment
63 Cooling section for vacuum distillation
64 Water cooling device for vacuum distillation treatment
65 Cooling water circulation pump for vacuum distillation treatment
66 Water storage tank for vacuum distillation treatment
67 Second temperature controller for vacuum distillation treatment
68 Receiving and collecting the condensed droplets for vacuum distillation treatment
69 First solenoid valve for vacuum distillation treatment
70 Recovered solvent storage tank for vacuum distillation treatment
71 Second solenoid valve for vacuum distillation treatment
Separation processing equipment
72 Separation treatment tank
73 First chemical storage tank for separation process
74 Flow rate control device linked metering pump for the first chemical for separation treatment
75 Upper plate for separation process
76 Vacuum pump for separation process
77 Digital vacuum constant apparatus for separation process
78 Water-cooled jacket for separation
79 Water cooling device for separation treatment
80 Cooling water circulation pump for separation treatment
81 Water storage tank for separation treatment
82 Ultrasonic oscillator for separation process
83 Ultrasonic generator for separation process
84 Ultrasonic wattmeter for separation process
85 Second chemical storage tank for separation process
86 Flow rate control device linked metering pump for second chemical for separation treatment
87 Boundary surface detection device for separation processing
88 Solvent discharge solenoid valve for separation process
89 Temperature controller for separation process

Claims (7)

A method for decomposing a polychlorinated biphenyl compound comprising the following treatment steps (A) to (E).
(A) From various products containing polychlorinated biphenyl compounds that are environmental pollutants, polychlorinated biphenyl compounds are extracted by an extraction treatment device,
(B) Sodium required for chemical reaction to completely decompose the polychlorinated biphenyl compounds in the extraction treatment liquid extracted from the polychlorinated biphenyl compounds introduced into the ultrasonic decomposition tank made of titanium Sodium alcoholate or metallic sodium in an amount of 2/3 to the total amount of alcoholate or metallic sodium is added, and the inside of the ultrasonic decomposition treatment tank is covered from the ultrasonic decomposition treatment tank according to the treatment conditions in a high vacuum and cooling state. The treatment liquid is transferred at a low flow rate by a circulation pump, introduced into the ultrasonic decomposition processing unit at a low flow rate, and an ultrasonic oscillation device is mounted in the ultrasonic decomposition processing unit, and the ultrasonic generator and ultrasonic power are installed. The ultrasonic oscillation output is adjusted by a meter to oscillate stronger ultrasonic waves than the ultrasonic oscillation device, making the liquid to be processed powerful. A large amount of cavitation is generated by vigorous vibration by sound waves, so that the main chain and side chain in the binding molecular chain of the polychlorinated biphenyl compound are cut by the action of frictional force and cavitation caused by the ultrasonic wave, and further the benzene ring Also, the polychlorinated biphenyl compounds are decomposed by being cleaved, and the treatment liquid is circulated again at a low flow rate in the ultrasonic decomposition treatment tank, so that the treatment liquid is circulated and subjected to ultrasonic decomposition treatment. An ultrasonic decomposition treatment step in which sodium alcoholate added to sodium chloride or metallic sodium is combined with a chlorine molecule released into the polychlorinated biphenyl compound by the ultrasonic decomposition treatment;
(C) In the liquid to be treated introduced into the ultraviolet decomposition tank made of titanium, the total amount of sodium alcoholate or sodium metal required for the chemical reaction to completely decompose the polychlorinated biphenyl compound is The remaining amount of the sonication treatment is added with sodium alcoholate or metal sodium of a fixed amount by 1/3, and further added with a fixed amount of titanium dioxide possessing photoconductivity. An ultrasonic oscillator is placed in contact with the lower part of the UV decomposition treatment tank under the processing conditions in a high vacuum and low temperature state for the liquid to be processed in the tank, and the ultrasonic wave is generated by the ultrasonic generator and ultrasonic power meter. Adjust the oscillation output to oscillate powerful ultrasonic waves from the ultrasonic oscillating device, and apply strong ultrasonic waves to the liquid to be processed in the UV decomposition treatment tank. It vibrates more and adds a violent microscopic stirring action by ultrasonic waves to promote chemical reaction. Under these processing conditions, a quartz glass lamphouse unit is cooled by a double tube jacket cooling method. In the lamp cooling process, the innermost part is ventilated by the outside air, and the pure water that has been cooled is circulated outside the lamp to forcibly cool the heat generated by the high-pressure mercury lamp or high-pressure xenon lamp and the generated heat rays. Since the rise is suppressed, ultraviolet rays with less heat rays than the lamp house unit can be generated, and the lamp house unit is fixedly mounted above the surface of the liquid to be treated or in the liquid to be treated and sealed with a sealing material. Using a high-pressure mercury lamp or high-pressure xenon lamp against the liquid to be treated in the UV decomposition bath UV decomposition treatment tank accelerates the decomposition rate in the UV decomposition process by the catalytic action of the photoconductive property possessed by the titanium dioxide added by irradiation with the generated UV light, and increases the acceleration in the photochemical reaction. The polychlorinated biphenyl compounds are decomposed by photochemical reaction by irradiating the solution to be treated with ultraviolet rays, so that the released chlorine molecules are combined with the sodium alcoholate added or sodium molecules with metallic sodium. Therefore, an ultraviolet decomposition process that completes the decomposition process by subjecting the polychlorinated biphenyl compound to an ultraviolet decomposition process,
(D) Solvent recovery treatment by subjecting the liquid to be treated introduced into the vacuum distillation treatment tank to a high vacuum state, indirect heating, the boiling point of the solvent, and the processing conditions in the condensation of the solvent vapor, vacuum distillation treatment of the contained solvent The liquid to be treated is separated into a solvent and a decomposition residue, and a vacuum distillation treatment step for removing the decomposition residue remaining in the vacuum distillation treatment tank outside the system of the vacuum distillation treatment device,
(E) Further, when the decomposition residue extracted in the vacuum distillation process contains oil, the decomposition residue extracted outside the system of the vacuum distillation apparatus is introduced into the separation tank. , Normal hexane is injected and added to the decomposition residue introduced into the separation tank, and an ultrasonic oscillator is contacted to the lower part of the separation tank under high vacuum and cooling conditions at low temperatures. In addition, the ultrasonic oscillation output is adjusted by the ultrasonic generator and the ultrasonic wattmeter, and a strong ultrasonic wave is oscillated and vibrated from the ultrasonic oscillator to the liquid to be processed. After microscopic stirring with strong ultrasonic waves and sufficiently extracting oil from the decomposition residue, all the equipment was stopped, and furfural was injected and added again. After the apparatus is operated and the liquid to be treated is sufficiently stirred, all the apparatuses are stopped and the separation apparatus is allowed to stand, so that the separated treatment liquid is separated into two layers. The upper layer is separated into a mixture of normal hexane and oil, and the lower layer is separated into a mixture of furfural and decomposition residue, and at the interface with both mixtures. The position is measured, and the vacuum distillation process is performed again in order to extract the oil and the decomposition residue separately contained in both the mixed liquids separately. The treatment liquid in the lower layer in the separation treatment tank is separated by the transfer pump for vacuum distillation at the same time that the treatment liquid discharge solenoid valve attached to the lower part of the separation treatment tank is opened in the tank. Is introduced into one of the tank by the vacuum distillation process chamber, oil is further introducing treatment liquid in the upper portion to the other of the tank and decomposition residue and the separation process.   In the extraction process step (A), isopropyl alcohol is injected and added to the transformer oil containing the polychlorinated biphenyl compounds extracted from the transformer, and ultrasonic waves are applied depending on the treatment conditions in a high vacuum and cooling state. 2. The method for decomposing a polychlorinated biphenyl compound according to claim 1, wherein the polychlorinated biphenyl compound is extracted by oscillating and vibrating with ultrasonic waves.   In the extraction treatment step (A), a condenser containing a polychlorinated biphenyl compound extracted by removing the exterior portion of the condenser is pulverized into a fine powder by a crusher, and isopropyl alcohol is injected and added thereto. A process for extracting a polychlorinated biphenyl compound by oscillating ultrasonic waves under a processing condition in a vacuum / cooling state and performing extraction processing by vibration of ultrasonic waves, followed by filtering with a vacuum filtration device. A method for decomposing a polychlorinated biphenyl compound according to 1.   In the extraction treatment step (A), carbonless paper (pressure-sensitive paper) and paper products containing a polychlorinated biphenyl compound are cut into thin lines with a shredder, and isopropyl alcohol or acetone is added and immersed therein. This is a step of extracting polychlorinated biphenyl compounds by oscillating ultrasonic waves under the processing conditions in a high vacuum / cooling state, extracting them by ultrasonic vibrations, and filtering them with a vacuum filtration device. Item 4. A method for decomposing a polychlorinated biphenyl compound according to Item 1.   In the extraction treatment step (A), normal hexane is added and immersed in the soil and sediment containing the polychlorinated biphenyl compound, and ultrasonic waves are oscillated under the treatment conditions in a high vacuum and cooling state. The method for decomposing a polychlorinated biphenyl compound according to claim 1, wherein the polychlorinated biphenyl compound is subjected to an extraction treatment by vibration of a sonic wave and subjected to a filtration treatment by a vacuum filtration device to extract the polychlorinated biphenyl compound.   In the extraction treatment step (A), the insulation portion of the insulated wire containing the polychlorinated biphenyl compound is immersed in dimethylformamide, which is an amide solvent, in a state of high vacuum and cooling. Under the treatment conditions, ultrasonic waves are oscillated and vibrated to dissolve the coated part, filtered with a vacuum filtration device, further injected with normal hexane, further vibrated with ultrasonic waves, and polychlorinated biphenyl compounds. The polychlorinated biphenyl compound according to claim 1, which is a step of subjecting the polychlorinated biphenyl compound to extraction treatment by dissolving in normal hexane, allowing the ultrasonic vibration to stop and allowing to stand, and separating and removing the dissolved portion of the coated portion. A method for decomposing biphenyl compounds. A polychlorinated biphenyl compound decomposition treatment apparatus comprising the following treatment apparatuses (F) to (J).
(F) The extraction object is introduced into the titanium extraction processing tank (1), the inside of the tank is sealed with the titanium upper plate (2), and the chemical storage tank for extraction processing (3) The extraction solvent is injected and added to the extraction target with the extraction solvent quantified pump (4) linked to the chemical flow rate controller for extraction processing, and then the inside of the tank is vacuumed with the extraction processing vacuum pump (5). The high vacuum state is further maintained by the digital vacuum constant device (6) for the extraction process, and the water cooling jacket (7) for the extraction process is contacted and attached to the outside of the extraction processing tank. The water is cooled by the extraction water cooling device (8) outside the system, and the cooling water is introduced into the water cooling jacket by the cooling water circulation pump (9) for extraction processing, Let the liquid cool down A low temperature state is maintained by the temperature controller (90) for the extraction process, the treated water after the cooling process is stored in the water tank (10) for the extraction process, and the cooling water is introduced again into the water cooling device. Further, the ultrasonic wave oscillating device (11) for extraction processing is attached to the lower part of the extraction processing tank in contact with the ultrasonic generator (12) for extraction processing and the ultrasonic power meter (13) for extraction processing. ) Adjusts the oscillation output of the ultrasonic wave, oscillates the ultrasonic wave from the ultrasonic wave oscillating device, vibrates the liquid to be processed in the extraction processing tank by the ultrasonic wave, and extracts the polychlorinated biphenyl compounds by the extraction processing device. Next, the extraction processing solution discharge electromagnetic valve (14) mounted at the bottom of the extraction processing tank is opened to extract the extraction processing solution out of the system for ultrasonic decomposition processing. Titanium by transfer pump An extraction processing unit for the introduction into sonication processing tank,
(G) The treatment liquid in which the extraction process of the polychlorinated biphenyl compound is completed is introduced into the ultrasonic decomposition tank (16) made of titanium by a transfer pump (15) for ultrasonic decomposition treatment. In addition, the sodium alcoholate or metallic sodium in the chemical storage tank (17) for ultrasonic decomposition treatment is stored in the ultrasonic decomposition treatment tank by the chemical flow control device linked quantitative pump (18) for ultrasonic decomposition treatment of sodium alcoholate or metallic sodium. A fixed amount is injected into the liquid to be processed, and the inside of the ultrasonic decomposition treatment tank is brought to a high vacuum state by a vacuum pump (19) for ultrasonic decomposition outside the system of the ultrasonic decomposition processing apparatus, for ultrasonic decomposition treatment. A water-cooled jacket for ultrasonic decomposition treatment is maintained outside the ultrasonic decomposition treatment tank by maintaining a high vacuum state with the digital vacuum constant device (20). A water cooling device (22) for ultrasonic decomposition treatment outside the system of the ultrasonic decomposition processing apparatus, and water is cooled, and the cooling water is a cooling water circulation pump for ultrasonic decomposition processing. (23) is introduced into the water-cooling jacket, the liquid to be treated in the ultrasonic decomposition treatment tank is cooled, and the temperature controller (91) for ultrasonic decomposition treatment is used to maintain the low temperature state. The treated water after the cooling treatment is stored in the treatment water storage tank (24), introduced again into the water cooling device, and the cooling water is circulated, which is higher than the liquid to be treated in the ultrasonic decomposition treatment tank. Under the processing conditions that maintain the low temperature state by the vacuum / cooling treatment, the liquid to be treated is transferred from the ultrasonic decomposition treatment tank at a low flow rate by the liquid circulation pump (25) for ultrasonic decomposition treatment. Sonication treatment The liquid to be treated is introduced into the unit (26), and an ultrasonic generator (27) for ultrasonic decomposition treatment is mounted in the ultrasonic decomposition processing unit, and an ultrasonic generator for ultrasonic decomposition processing is installed. (28) and the ultrasonic power meter (29) for ultrasonic decomposition treatment are used to adjust the oscillation output of the ultrasonic wave to oscillate strong ultrasonic waves from the ultrasonic oscillator, and the liquid to be processed is subjected to high vacuum and cooling. Depending on the processing conditions in the low temperature state due to the treatment, it is vibrated vigorously by powerful ultrasonic waves, cavitation due to a large amount is generated, polychlorinated biphenyl compounds are decomposed, and the liquid to be treated is again put in the ultrasonic decomposition treatment tank By introducing and circulating at a low flow rate, the liquid to be treated is circulated and subjected to ultrasonic decomposition treatment. In the treatment liquid that has completed ultrasonic decomposition treatment, ultrasonic decomposition treatment is performed. The processing liquid discharge solenoid valve (30) for ultrasonic decomposition processing attached to the lower part of the tank is opened, and the processing liquid that has been subjected to ultrasonic decomposition processing is discharged out of the system of the ultrasonic decomposition processing apparatus. In order to completely decompose the polychlorinated biphenyl compounds, an ultrasonic decomposition apparatus that introduces a treatment liquid that has been subjected to ultrasonic decomposition into a titanium ultraviolet decomposition tank by means of a transfer pump for ultraviolet decomposition. When,
(H) In the treatment liquid that has been subjected to ultrasonic decomposition treatment, the ultraviolet decomposition treatment transfer pump (31) introduces it into the titanium ultraviolet decomposition treatment tank (32), and with respect to the liquid to be treated in the ultraviolet decomposition treatment tank. The first chemical storage tank (33) for ultraviolet decomposition treatment with sodium alcoholate or sodium metal is used to decompose the sodium alcoholate or metal sodium into the ultraviolet decomposition treatment tank by the first chemical flow rate controller linked meter pump (34) for ultraviolet decomposition treatment. A fixed amount is supplied to the liquid to be treated, and the second chemical addition amount control device for the ultraviolet decomposition treatment of the titanium dioxide from the second chemical storage tank (35) for the ultraviolet decomposition treatment with titanium dioxide is connected to the screw quantitative supply device. (36) introduces and adds a fixed amount to the liquid to be treated in the ultraviolet decomposition treatment tank, A vacuum pump (37) for ultraviolet decomposition treatment outside the system is used to bring the inside of the ultraviolet decomposition treatment tank to a high vacuum state, and further, a high vacuum state is maintained by a digital vacuum constant device (38) for ultraviolet decomposition treatment, A water cooling jacket (39) for ultraviolet decomposition treatment is attached to the outside of the ultraviolet decomposition treatment tank, and water is cooled by the water cooling device (40) for ultraviolet decomposition treatment outside the system of the ultraviolet decomposition treatment device. Cooling water is introduced into the water cooling jacket by a cooling water circulation pump (41) for ultraviolet decomposition treatment, the liquid to be treated in the ultraviolet decomposition treatment tank is cooled, and the temperature controller (92) for ultraviolet decomposition treatment is in a low temperature state. The treated water after cooling treatment is stored in the water storage tank (42) for ultraviolet decomposition treatment, and is introduced into the water cooling device again to circulate the cooling water. Therefore, under the processing conditions in which the liquid to be processed in the ultraviolet decomposition treatment tank is maintained in a low temperature state by high vacuum and cooling treatment, an ultrasonic oscillation device for ultraviolet decomposition treatment (43) is provided below the ultraviolet decomposition treatment tank. The ultrasonic oscillation output is adjusted by the ultrasonic generator (44) for ultraviolet decomposition treatment and the ultrasonic power meter (45) for ultraviolet decomposition treatment, so that it is stronger than the ultrasonic oscillation device. The ultrasonic wave is oscillated and vibrations by ultrasonic waves are added to the liquid to be treated in the ultraviolet decomposition treatment tank to promote the photochemical reaction, and the quartz glass lamp house unit (46) is subjected to the ultraviolet decomposition treatment. It is fixed above the surface of the liquid to be treated in the tank or in the liquid to be treated, and sealed with a sealing material. A high-pressure mercury lamp or a high-pressure xenon lamp (47) is inserted in and fixed at both ends with quartz glass, and an air-cooling jacket (48) for lamp cooling treatment is provided around the lamp to The air pump (49) for the lamp cooling process outside the system introduces the outside air into the air cooling jacket for the lamp cooling process, forcibly cools the heat generated by the lamp, and exhausts the air outside the system. A water cooling jacket (50) made of quartz glass for cooling the lamp is provided outside the air cooling jacket for the lamp cooling treatment, and a pure water cooling device (51) for the lamp cooling treatment outside the system of the UV decomposition treatment apparatus. Pure water is cooled, and the cooled pure water is subjected to an ion exchanger (52 for lamp cooling). Cooled pure water that has been introduced into the pure water by removing the metal ions generated in the pure water through circulation of the purified pure water and made to be pure water with high purity discharged from the ion exchanger is used for lamp cooling treatment. In the pure water storage tank (53) for the lamp cooling treatment outside the system of the ultraviolet decomposition treatment apparatus, the heat generation by the lamp and the heat rays radiated by the lamp are forcibly cooled. High pressure mercury lamp or high pressure xenon against the liquid to be treated in the UV decomposition treatment tank by introducing the water again into the pure water cooling device for lamp cooling treatment and circulating the cooling pure water to forcibly cool the lamp. The lamp is irradiated with ultraviolet rays, and then the ultraviolet decomposition treatment is performed in a treatment solution in which the polychlorinated biphenyl compound is completely decomposed by completion of the ultraviolet decomposition treatment. Was treated liquid discharge solenoid valve for ultraviolet degradation process that is attached to the bottom of the bath (54) in the open state, an ultraviolet decomposition treating apparatus for introducing into the vacuum distillation tank by transfer pump for vacuum evaporation process,
(I) A treatment liquid obtained by completely decomposing a polychlorinated biphenyl compound is introduced into a vacuum distillation tank (56) by a transfer pump (55) for vacuum distillation, and vacuum outside the system of the vacuum distillation apparatus. A vacuum pump (57) for distillation treatment is used to bring the inside of the vacuum distillation treatment tank into a high vacuum state, and a high vacuum state is maintained using a digital vacuum constant device (58) for vacuum distillation treatment. A heating device (59) for vacuum distillation treatment is attached in contact with the lower portion, and the treatment liquid in the vacuum distillation treatment tank is indirectly heated by the heating device under high vacuum conditions under the treatment conditions, The temperature is adjusted by the first temperature controller (60) for vacuum distillation under a set temperature condition of the boiling point or higher with respect to the solvent contained, and the solvent is heated. It is vaporized by the heat treatment at a temperature above the point, becomes a solvent vapor state, rises, and is introduced into the solvent vapor condensing part (61) for vacuum distillation treatment by the upper part in the vacuum distillation treatment tank. A vacuum distillation processing cooling part (63) in which a cooling water serpentine tube (62) for vacuum distillation processing is provided to the surroundings, and water for vacuum distillation processing outside the system of the vacuum distillation processing apparatus. Water is cooled by the cooling device (64), and the cooling water is introduced into the cooling water snake pipe provided in the cooling unit by the cooling water circulation pump (65) for vacuum distillation processing, and the solvent vapor in the solvent vapor condensing unit is Then, the treated water after the cooling treatment is introduced into the water storage tank (66) for vacuum distillation treatment outside the system of the vacuum distillation treatment device, and again introduced into the water cooling device. The cooling water is circulated, and the temperature for the solvent vapor cooling treatment is controlled by the second temperature controller (67) for vacuum distillation under a set temperature condition of the solvent vapor below the boiling point temperature. The condensed and liquefied solvent is condensed by the condensate drop receiving and collecting device (68) for vacuum distillation, which is adjusted and condensed by the cooling process and is provided at the lower part of the cooling water serpentine in the cooling section. The recovered solvent is collected and stored, and the first electromagnetic valve (69) for vacuum distillation processing is automatically opened and closed to open the recovered solvent. The recovered solvent for vacuum distillation processing outside the system of the vacuum distillation processing apparatus The recovered solvent is introduced into the storage tank (70) and stored, and when the amount of the recovered solvent reaches a fixed amount, the recovered solvent is supplied to the second electromagnetic valve (71) for vacuum distillation treatment. It is opened by an automatic opening / closing operation, and is extracted outside the system of the vacuum distillation processing apparatus, and then the decomposition residue in the vacuum distillation processing tank is cooled and extracted outside the system of the vacuum distillation processing apparatus. A vacuum distillation processing device;
(J) Further, if the decomposition residue extracted by the vacuum distillation processing apparatus contains oil, the decomposition residue extracted outside the system of the vacuum distillation processing apparatus is separated into the separation processing tank (72). The first chemical flow control device interlocking metering pump (74) for separating the normal hexane from the first chemical storage tank (73) for separation processing outside the system of the separation processing device with respect to the decomposition residue. Then, a fixed amount of normal hexane is injected and added, and an upper plate (75) for separation treatment is set in the upper part of the separation treatment tank so that the inside of the separation treatment tank is sealed, and the separation treatment outside the system of the separation treatment apparatus. The inside of the separation processing tank is brought into a high vacuum state by a vacuum pump (76), and further maintained in a high vacuum state by a digital vacuum constant device (77) for separation processing, A water cooling jacket (78) for separation treatment is attached to the outside of the separation treatment tank, and water is cooled by a water cooling device (79) for separation treatment outside the system of the separation treatment device, thereby separating the cooling water. A cooling water circulation pump (80) for treatment is introduced into the water cooling jacket, the liquid to be treated in the separation treatment tank is cooled, and the low temperature state is maintained by the temperature controller (89) for separation treatment. The treated water after cooling treatment is stored in a water storage tank (81) for separation treatment outside the system of the separation treatment device, introduced again into the water cooling device and circulated through the cooling water, and further separated at the lower part of the separation treatment tank. The ultrasonic oscillation device (82) for contact is mounted in contact, and the ultrasonic oscillation output for the separation processing (83) and the ultrasonic power meter (84) for separation processing are adjusted, Super The liquid to be treated is oscillated with strong ultrasonic waves from the wave oscillation device to vibrate the liquid to be treated, and the liquid to be treated is subjected to microscopic stirring treatment with the powerful ultrasonic wave. After the oil is completely extracted from the decomposition residue by applying the stirring action, all the devices are stopped, and further, furfural is removed from the second chemical storage tank (85) for separation processing outside the system of the separation processing device. The second chemical flow control device linked metering pump (86) for separation treatment is used to inject and add the amount of furfural to the liquid to be treated, and all the devices are operated again to give sufficient stirring to the liquid to be treated. Then, all the devices are stopped and the separation processing device is allowed to stand, whereby the liquid to be treated is separated into two layers, and the upper layer contains normal hexane and oil. The mixed liquid and the lower layer are separated into a mixed liquid of furfural and decomposition residue. Next, the position of the boundary surface by both mixed liquids is detected by the boundary surface detection device (87) for separation processing. In order to extract the oil and decomposition residue separately contained in the two mixed liquids separately, the vacuum distillation tank is divided into two tanks in advance. The separation treatment liquid discharge solenoid valve (88) attached to the lower part of the separation treatment tank is operated to be opened, and at the same time, the inside of one of the vacuum distillation treatment tanks by the transfer pump for vacuum distillation treatment. Into the separation tank, the mixed liquid of the furfural and decomposition residue in the lower layer part is introduced, and in the other tank, the mixed liquid of normal hexane and oil in the upper layer part is introduced, and then both mixed liquids are introduced. of The solvent in rumal hexane and furfural is again subjected to vacuum distillation treatment due to the temperature difference of the boiling points, and after first recovering normal hexane and further furfural, oil components and decomposition residues remaining in the two vacuum distillation treatment tanks separately. Are separately separated from the system of the vacuum distillation processing apparatus, and the separation processing apparatus for oil and decomposition residue.

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