200302867 玖、發明說明 【發明所屬之技術領域】 本發明係關於供從塑膠採集油的塑膠之油化方法及油 化設備。 【先前技術】 供從廢棄塑膠採集油的油化設備雖有各種提案，但是均 未執行充分的分解，實際上並未存在實用操作的設備。 所以，本案申請人之前便有開發如日本專利特開2 0 0 0 -1 6 774號公報中所揭示的小型且簡單構造的逆熱梯度方式 (r e v e r s e t h e rm a 1 g r a d i e n t t y p e )的油化設備。 但是，在此油化設備中，卻存在有下述問題點：1)雖在塑 膠處理量較少時可確實的將塑膠進行油化，但是若塑膠處 理變多的話，則頗難進行完全的塑膠油化；2)在融解 PVC(polyvinylchlorid)塑膠之際，於融解部中將產生氯化 氫氣體，但是對此氯化氫氣體的處理則尙未充分的實施； 3)未被油化之廢氣（off-gas)的處理尙未充分的實施等問 題。 【發明內容】 因此本發明主要乃有鑒於該等問題點，其主要目的在於 提供一種可將大量塑膠進行油化，並可進行氯化氫氣體的 處理，且可完全處理廢氣的油化方法、及油化設備。 緣是，本發明的油化方法，係將塑膠加熱融解而產生起 泡狀塑膠，取出此起泡狀塑膠並經加熱、解聚合之後，再 經冷卻而產生油。此時可將起泡狀塑膠朝斜上方（最好相對 6 312/發明說明書(補件)/92-〇4/92101606 200302867 於水平爲2 5〜3 0 °的角度）拉上取出。此外，亦可將起泡狀 塑膠一邊朝斜上方拉上一邊進行加熱，且對起泡狀塑膠依 越上方位置使用越高的溫度進行加熱。此外，亦可在經融 解的塑膠中添加食物油、動物油、或礦物油並加熱，而產 生由該等混合物所構成的起泡狀塑膠。 再者，本發明的油化方法，亦可在將融解塑膠之際所產 生的氯化氫氣體，與其他分解氣體進行分離之後，再與消 石灰進行反應而形成氯化銘並回收。此外，亦可將未被油 化的廢氣利用高溫陶瓷進行接觸分解的處理。 再者，本發明的油化設備係具備有：將塑膠予以加熱並融 解而產生起泡狀塑膠的融解部；以及取出起泡狀塑膠並經 加熱、解聚合後，再經冷卻而產生油的分解部。在此油化 設備中，分解部亦可具備有：將起泡狀塑膠朝斜上方（最好 依相對於水平爲25〜30°的角度）拉上取出的取出機構。分 解部亦可具備有：將起泡狀塑膠一邊朝斜上方拉上一邊進 行加熱，且對起泡狀塑膠依越上方位置使用越高的溫度進 行加熱的加熱機構。在融解部與分解部的銜接部處，亦可 具備有：供注入食物油、動物油、或礦物油用的油注入機 構。此外，融解部亦可由具不同溫度分布的複數融解筒所 形成；分解部亦可由具不同溫度分布的複數傾斜分解筒所 形成。 再者，本發明的油化設備亦可具備有：供將在融解部所產 生的氯化氫氣體進行處理用的脫氯裝置；此脫氯裝置亦可 具備有：供將氯化氫氣體與其他分解氣體進行分離用的分 312/發明說明書(補件)/92·04/92101606 200302867 離器；以及將分離器進行分離後的氯化氫氣體與消石灰進 行反應而形成氯化鈣的反應器。此外，亦可具備有：將在分 解部中經冷卻後而未形成油的廢氣，利用高溫陶瓷進行接 觸分解而處理的廢氣處理裝置。 再者，本發明的油化設備，亦可在設置多段的分解筒 中，於最終段的分解筒上端處設置殘渣回收機構；此殘渣 回收機構亦可使上方開口位於最終段的分解筒上端位置 處’而使下方開口位於較重於空氣的非活性氣體環境內之 筒而形成。 再者’本發明的油化亦可設備：供儲存塑膠並供應給融解 部用的漏斗；此漏斗係具備有：具螺旋狀葉片的導螺桿 (lead screw)。此外，亦可在漏斗與融解部之間，具備著由 既定長度之未加熱區域所形成的非加熱部。複數的融解筒 係具備有：具有供搬送塑膠用之螺旋狀葉片的導螺桿，且位 於前頭之融解筒的導螺桿葉片間距，大於其他融解筒的導 螺桿葉片間距。 再者’本發明的油化設備乃融解部與分解部係具備有： 內筒；形成於內筒外圍的外筒；形成於內筒與外筒間之循 環著熱風的熱風空間；以及檢測出融解部與分解部之溫度 的溫度偵測器；此外，亦可尙具備有：當溫度偵測器檢測出 達到既定溫度以上的異常溫度之時，便對熱風空間送入二 氧化碳的二氧化碳供應裝置。 再者，本發明的油化設備乃融解部與分解部係具備有： 內筒；形成於內筒外圍的外筒；以及形成於內筒與外筒間 312/發明說明書(補件)/92-04/92101606 8 200302867 之循環著熱風的熱風空間；此外，亦可尙具備有：供對熱風 空間供應經燃燒所產生之熱風的熱風產生裝置；以及使供 應給融解爐之塑膠進行乾燥的乾燥裝置；亦可將此乾燥裝 置內的空氣供應給熱風產生裝置並經燃燒而進行脫臭。此 外，亦可將乾燥裝置內的空氣供應給廢氣處理裝置，並利 用高溫陶瓷進行接觸分解而脫臭。 再者，本發明的油化設備係融解筒的其中一部份採用伸 縮自如所形成的伸縮筒，且此伸縮筒係由內筒、蛇腹管、 及外筒所形成，而該蛇腹管係配置於內筒外圍處，其中一 端固定於內筒上，而另一端則可對內筒進行滑動；該外筒 係固定於蛇腹管的另一端，並在內部可自由滑動的收容著 內筒。 再者，本發明的油化設備乃融解部係具備有：內筒；形成 於內筒外圍的外筒；以及形成於內筒與外筒之間，並使液 體之熱媒進行循環的熱媒空間；亦可更具備有供對此熱媒 空間供應著液體熱媒用的熱媒供應裝置。 【實施方式】 以下，參照圖式，針對本發明實施態樣進行說明。 圖1所示係供說明相關本發明塑膠之油化方法的基本原 理之槪念圖。原料的塑膠係在20〇°C〜3 5 0 °C之溫度下進行 融解，並儲存於儲存部1中。經融解過的塑膠（融解塑膠） 便利用分解筒1 3而朝斜上方拉上。 其中，分解筒13係具備有：內筒2;在內筒2周圍形成 熱風空間4的外筒6、以及導螺桿7。導螺桿7係由旋轉軸 9 312/發明說明書(補件)/92-04/92101606 200302867 1 4與螺旋葉片8所構成，並利用馬達1 2依4〜5轉/分的速 度進行旋轉。對熱風空間4從配管1 〇供應著熱風。內筒2 內的溫度在爲將塑膠予以氣化並解聚合，而維持於 350 〜620 〇C ° 利用導螺桿7在內筒2內進行搬送的融解塑膠，於分解 筒1 3下方進行一次分解（從融解狀態到氣化的最初較重氣 體狀態），而形成一次分解氣體。一次分解氣體便利用導螺 桿7而依低速度被送往分解筒1 3上方，並利用從配管1 5 所供應的熱風，在維持於3 5 0 t〜62 0 °C的內筒2內進行二 次分解（若塑膠被解聚合並經冷卻的話，便呈油化狀態）’ 而形成較輕的二次分解氣體。 、 再者，若原料的塑膠中所含之所有油成分的二次分解， 均在分解筒上半部進行的話，則分解筒僅要一個便已足 夠，亦可採用二個分解筒，並將連接於儲存部1者當作第 1段分解筒，且將第2段分解筒連接於此第1段分解筒上。 再者，在儲存部1外側設有供形成熱風空間3用的外箱 5，俾對熱風空間3送入熱風。供應給儲存部1的塑膠經加 熱至200〜3 5 (TC而形成融解塑膠mp，同時在表面部形成起 泡狀的塑膠（起泡狀塑膠）f。此泡沬狀塑膠f利用軸前端14a 浸漬於融解塑膠mp內的導螺桿7，而被一邊斜向拉上一邊 進行加熱，此時因爲與熱之間的接觸面積將變大，因此將 確實的進行分解（解聚合）而形成二次分解氣體。二次分解 氣體便從配管9中進行收集，經冷卻而油化，然後回收於 儲油槽中。 312/發明說明書(補件)/92-〇4/92 ΚΠ 6〇6 10 200302867 再者，泡沫狀塑膠f的拉上速度可爲3 0〜6 0 c m /分，若低 於此的話，搬送效率將惡化，反之，若超過此的話，將無 法充分的分解。譬如，泡沫狀塑膠f利用圖1 5所示導螺桿 7而被螺旋狀拉起。此時的螺旋狀移動速度最好爲 3 0〜6 Ocm/分。此速度乃譬如利用導螺桿7的間距P而進行 調節。如此的話，泡沬狀塑膠f便將被依上述速度在內筒 2內進行搬送’並經緩慢的加熱，而在一次分解溫度區域 與二次分解溫度區域中充分的被分解（解聚合）。泡沫狀塑 膠f截至完全二次分解爲止，可在600 °C附近加熱14〜15 分鐘程度。 雖原料的塑膠種類之不同而處理溫度亦將各自不同，但 是最好將儲存部1的溫度設定爲融解塑膠mp形成起泡狀. 的溫度（2 00〜3 5 0 °C )，此外，爲獲得良好的分解，而設定較 緩和的溫度梯度，並維持較久的起泡狀態，且增加與熱之 間的接觸面積之事乃屬重要的。爲此，可將分解筒1 3設計 呈傾斜於水平的狀態。此外，傾斜的分解筒1 3內將藉由使 熱風朝上半部吹入之後再從上半部朝向下半部循環，而使 從下半部到上半部逐漸溫度上升。此方式便是所謂的「逆 熱梯度方式（reverse thermal gradient type)」。 在爲將泡沬狀塑膠f良好的長時間保持，最好如圖2所 示，將分解筒2 7的傾斜角度0設定爲2 5 °〜3 0。。若分解 筒2 7的傾斜角度0低於2 5 °的話，泡沬狀塑膠f將快速的 朝橫向流動並在短時間內消失，反之，若傾斜角度β設定 爲超過3 0 °的話，隨與重力間的關係，便頗難從融解塑膠 11 312/發明說明書(補件)/92-04/92101606 200302867 m p表面將泡沬狀塑膠f朝上方長距離的拉起，在此情況 下，泡沫狀塑膠f亦將在短時間內消失。 在圖2中’融解塑膠mp的儲存部2 9係形成於將供應筒 2 8與分解筒2 7連接呈v字形的連接部處。供應筒2 8係由 內筒20與外筒21所構成，並在其間介設著配管22且供應 著熱風。內筒2 0內維持於2 0 0〜3 5 0 °C。 分解筒2 7係由內筒2 5、外筒1 7、及導螺桿2 4所構成。 導螺桿24係依軸23下端可自由旋轉的支撐於儲存部29 下壁之方式進行安裝。對內筒2 5與外筒1 7之間，從熱風 產生爐透過配管26c供應著450〜620 °C的加熱空氣。然後， 此加熱空氣係依在分解筒2 7內下降並從分解筒下半部的 配管26b抽出，然後再從上半部的配管26a流入之方式進 行循環。如此的話，高溫空氣若在分解筒2 7內從上半部朝 向下半部進行循環的話，分解筒27內的溫度分布便形成溫 度從下朝上變高的狀態。分解筒2 7的下半部乃爲執行一次 分解而維持於3 00〜4 5(TC，而分解筒27的上半部則爲執行 二次分解而加熱至6 00 °C附近。 在儲存部2 9中產生泡沬狀塑膠f，此泡沬狀塑膠f便於 良好狀態下，依在傾斜的分解筒27內上升之方式進行搬 送，並在搬送途中便被加熱而形成分解氣體。分解筒27 與供應筒2 8呈V字形連接狀態，因爲融解塑膠mp完全封 閉於儲存部2 9中，因此分解氣體不致從分解筒2 7逆流回 供應筒2 8而呈安全狀態，而且防止空氣從外部通過儲存部 2 9進入分解筒2 7內’亦毫無爆炸的危險性。 12 312/發明說明書(補件)/92-04/92101606 200302867 其次，針對採用此塑膠油化方法的油化設備進行說明。 在圖3至圖7中，本發明的油化設備3 0係具備有：將如 原料的廢塑膠予以融解的融解部3 1 ;將在此融解部3 1中 所融解的塑膠施行一次分解與二次分解的分解部3 2 ;在處 理含氯之P V C時，施行脫氯處理的脫氯處理部3 3 ;供將 塑膠進行融解、分解時所產生的廢氣施行處理用的廢氣處 理部3 4 ;以及產生屬於融解與分解時之熱源的熱風的第 1、第2熱風爐35,36。 融解部3 1係如圖6所示，具備有：透過非加熱部4 1 0而 連接於投入原料塑膠之漏斗4 1上的第1融解筒3 1 a ;前端 連接於第1融解筒3 1 a前端下方，並垂直於第1融解筒3 1 a 的第2融解筒3 1 b ;後端連接於第2融解筒3 1 b前端下方， 並垂直於第2融解筒3 1 b的第3融解筒3 1 c ;以及後端連 接於第3融解筒3 1 c前端下方，並垂直於第3融解筒3 i c 的第4融解筒3 1 d。如此的話，第1〜第4融解筒3 1 a，3 1 b ,…，3 1 d整體便配置呈矩形，而融解塑膠將依序從分解筒前 端朝接著下一個融解筒後端落下並進行傳送。該等融解筒 3 1 a〜3 1 d亦可水平連接。 漏斗4 1係如圖1 6所示，乃由下述構件所形成：漏斗狀殼 體411;覆蓋著殻體411上面的蓋體412;配置於蓋體412 中心部的馬達4 1 3 ;以及連接於馬達4〗3並貫穿且延伸於 殻體4 1 1內，由旋轉軸4 1 4a與旋轉軸4丨4a上所安裝螺旋 葉片4 1 4b所組成的導螺桿4 1 4。導螺桿4 i 4之螺旋葉片 41朴係整體呈沿導螺桿414形狀的漏斗狀。在導螺桿414 312/發明說明書(補件)/92-04/92101606 13 200302867 內壁與螺旋葉片414b外圍之間設計著2〜5cm程度的間隔 W。導螺桿4 1 4乃利用馬達4 ! 3而依既定速度進行旋轉， 俾防止較輕的塑膠阻塞於漏斗4 1內。較重的塑膠將通過導 螺桿4 1 4內壁與螺旋葉片4〗4b外圍間的間隔w而掉下， 較輕的塑膠碎片則將隨導螺桿414而確實的被送入非加熱 部410內。 非加熱部4 1 0係形成圓筒狀，並連接於漏斗4 2下半部（參 照圖1 7)。在非加熱部4 1 〇端部處設置馬達* 2，在此馬達 4 2上連接者與後述之配置於融解筒3 1 a內的導螺桿1 3 7共 通的導螺桿1 3 7。導螺桿1 3 7利用馬達4 2而旋轉，俾將從 漏斗4 1所送至的塑膠碎片緩慢的送往前方，並供應給融解 筒 3 1 a ° 再者，非加熱部4 1 0係不同於後述的融解筒3 1，並未施 行利用熱風的加熱。所以，因爲漏斗4 1之安裝部與融解筒 3 1呈分離狀態，因此塑膠便不致在漏斗4 1安裝部附近便 開始融解，可防止隨已融解塑膠的黏性阻抗而導致導螺桿 1 3 7旋轉的停止現象發生。換句話說，藉由使塑膠的融解 部分遠離漏斗4 1安裝部’便可加長未融解塑膠部分，並利 用此未融解塑膠擠推融解塑膠而前進。 融解部3 1係由矩形外箱1 3 6、與外箱1 3 6內所設置的內 筒1 3 1所構成（第8圖）。在內筒1 3 1內設置著導螺桿1 3 7 ; 此導螺桿1 3 7係具備有：旋轉軸1 3 3、以及設置於旋轉軸1 3 3 周圍的螺旋葉片1 3 2。此外’第1融解筒3 1 a的導螺桿1 3 7 的間距係設定爲大於其他融解筒3 1 b，3 1 c，3 1 d的導螺桿 14 312/發明說明書(補件)/92-〇4/921()16()6 200302867 1 3 7之間距。此乃如後述因爲融解部3 1的設定溫度較低於 其他融解筒，因此塑膠的滯留密度較低且阻抗較小的緣 故。導螺桿1 3 7利用馬達而旋轉（譬如，第1融解筒3 1 a利 用馬達4 2 (圖4、圖5)而旋轉，而第2融解筒3 1 b利用馬 達5 5而旋轉）。 再者’內筒1 3 1係在外圍設置複數個吸熱葉片丨3 4。在 內筒1 3 1與外箱1 3 6之間形成熱風空間丨3 5。第1融解筒 31a控制於190〜2 00。(：，第2融解筒31b內控制在210〜230 °C ’第3融解筒3 1 c控制在2 3 0〜2 6 0。(：，第4融解筒3 1 d 控制在3 0 0〜34CTC。如此將四個融解筒31a，31b，…，31d配 設呈矩形狀，並將各融解筒溫度逐漸提高的理由，如下所 述：a)爲確實執行氯乙烯等含氯塑膠的脫氯，而確保充分的 滯留時間（約20分鐘）；b)利用多段化而緩和溫度分布便可 輕易的進行溫度控制；c)降低第1融解筒3 i a的溫度，乃 爲防止在漏斗4 1附近產生塑膠融附於旋轉軸1 3 3上的現 象；以及d)爲縮短設備整體的配設長度。 再者’對各融解筒3 1內從第1熱風爐3 5經由配管7 0 而供應熱風’此熱風將從傳送塑膠的下游端朝向上游端吹 送。所以’各融解部3 1內將呈逆熱梯度狀態。各融解部 3 1內的熱風循環乃利用鼓風機5 6，5 7，5 8 (圖4 )、6 0而執行 的。另外，在第1、第2熱風產生爐35，36上連接著煙囪 59。煙囪59具有分管59a，59b與排放口 59c，並形成倒u 字形（圖4)。 分解部3 2係由控制在3 5 〇〜4 2 〇的第！段分解筒4 7、 15 312/發明說明書(補件)/92-04/92101606 200302867 以及鄰接於第1段分解筒47並控制在4 5 0〜5 8(TC的第2段 分解筒4 8 (圖7 )。分解筒4 7，4 8係配置呈傾斜於水平面 2 5〜30 °的狀態。第4融解筒31d前端部係連接於第1段分 解筒4 7內，且此連結部將形成融解塑膠的儲存部。 第1段分解筒4 7係由利用隔板2 5 6而進行隔間，而形 成被隔開爲左右二列的二個單位分解筒47 a，47b所構成（圖 9)。單位分解筒47 a，4 7b係具備有：內筒2 5 5 ;設置於內筒 2 5 5外圍的複數個吸熱風扇2 5 3 ;導螺桿1 5 0 ;以及送入熱 風的熱空間2 5 4。各導螺桿1 5 0係由旋轉軸2 5 1與螺旋葉 片2 5 2所構成，並利用馬達51，52(圖5)而進行旋轉。 第2段分解筒48大致如同第1段分解筒47的構造，在 單位分解筒48 a，4 8b(圖6)中分別設置著內筒148。在內筒 1 4 8內設置有導螺桿1 4 9，而導螺桿1 4 9則利用馬達 53，54(圖5、圖7)而緩慢的（4〜5轉/分）進行旋轉。 在第1段分解筒47的內筒2 5 5上端，設置著供將通過 的分解氣體加熱至580〜620 °C的過熱器151(圖7)。在第1 段分解筒47內經二次分解的分解氣體，通過過熱器1 5 1 與配管49而被抽出，並透過鹼洗淨用洗滌器（ScrUbbe〇61 而傳送至冷凝器37a(圖5)。然後，分解氣體便利用冷凝器 3 7 a而冷卻並油化，此油便通過配管4 6而儲存於儲油槽3 8 a 中。儲油槽38a中所儲存的油，部份將經由供給油槽（server tank)STl而供應給熱風產生爐35,36。 再者，在配管49中途安裝著供調整配管49內所流通分 解氣體之流量用的閥49a。雖對冷凝器37a必須僅送在第1 16 312/發明說明書(補件)/92-04/92101606 200302867 段分解筒4 7中完全被二次分解的較輕分解氣體，但是從配 管4 9所導出的分解氣體中’多少含有未完全執行二次分解 的稍重之不完全分解氣體。所以’雖然當來自配管4 9的分 解氣體導出量較少時，不完全分解氣體將無法超越配管4 9 的直立部，而將返回第1段分解筒4 7並經由落下筒1 2 0 而被送往第2段分解筒4 8 ’但是若來自配管4 9的分解氣 體導出量較多的話’分解氣體的導出流勢將增加’導致不 完全分解氣體亦將超越配管4 9的直立部而被送往冷凝器 3 7a。所以，利用閥49a而調整從配管49所導出分解氣體 的導出量，俾防止不完全分解氣體被送往冷凝器3 7 a。 第1段分解筒47乃如前述，因爲被控制於3 5 0〜4 2 0°C ’ 因此在第1段分解筒4 7中相當於分解溫度較低之汽油的油 成分、燈油及輕油的成分，將部分經一次分解後再被二次 分解。其中，未充分分解狀態的氣體將利用過熱器1 5 1而 完全的二次分解。所以如此的話，經二次分解的分解氣體 將被冷凝器3 7 a所冷卻並油化。未被冷凝器3 7 a充分油化 的氣體將被具有泵P的配管46所吸取，而當作廢氣被回 收於儲油槽3 8 a中。 在第1段分解筒47內未被完全二次分解的起泡狀塑膠 成分，將經由落下筒120而供應給第2段分解筒48下端 部，並利用第2段分解筒48內的導螺桿1 49而朝斜上方傳 送。因爲第2段分解筒48內被控制於45 0〜5 8 0 °C溫度’因 此在第2段分解筒4 8中，相當於燈油、輕油之成分的殘留 部分及重油成分，亦將被完全的二次分解。與塑膠—胃辛皮 17 312/發明說明書(補件)/92-〇4/92101606 200302867 投入的金屬、泥等殘渣，將經由污泥管40a而被回收於污 泥槽40中。 污泥槽40係如圖i 8所示，儲存著水40b，並在水40b 中設置金屬網40c，而殘渣則將被回收於此金屬網40c上。 藉由從污泥槽4 0中取出金屬網4 0 c，便可將殘渣從污泥槽 4 〇中取出。污泥槽4 0上面由其中一部份設有開口 4 0 e的 蓋體40d所覆蓋著。在污泥槽40中較水40b更上方處，塡 充入如二氧化碳等重於空氣的非活性氣體4〇f，而污泥管 4 〇 a下端則位於非活性氣體4 〇 f內。在污泥槽4 0上連接著 氣體高壓瓶4 0 g，俾從氣體高壓瓶4 0 g對污泥槽4 0內供應 著非活性氣體4 0 f。從氣體高壓瓶4 〇 g所供應的非活性氣 體4 0 f，將部分溢出於開口 4 0 e。如此的話，藉由使污泥管 4 〇 a下端位於非活性氣體4 〇 f中，便可有效的防止從污泥 管40a朝第2段分解筒48內流入空氣，而消除爆炸的危險 性。此外，當使污泥管40a下端位於水40b中的情況時， 雖較輕的殘渣將隨水的浮力而浮起，而阻塞污泥管4 0 a的 下端部分，但是藉由使污泥管40a下端位於非活性氣體40f 中，便可防止此現象的發生，殘渣將掉入於水40b中。 對第1段、第2段分解筒4 7，4 8的上半部，從第2熱風 產生爐36經由配管71，71a，71b(圖5)而供應熱風，此熱風 將依從分解筒4 7，4 8下半部脫出並返回上半部的方式，利 用鼓風機1 7 0,1 7 1,1 72進行循環。如此的話，分解筒47，4 8 將形成從上半部朝向下半部變爲低溫的逆熱梯度狀態。此 外，對融解部3 1供應著來自第1熱風產生爐3 5的熱風， 18 312/發明說明書(補件)/92-04/92101606 200302867 此熱風譬如將在第4融解筒3 1 d中’利用鼓風機ό 0而進行 循環（圖7)。 在第2段分解筒4 8之內筒1 4 8上端配置著透過鹼洗淨 用洗滌器6 1而連接於冷凝器3 7 b上的配管5 0 (圖5 )。被第 2段分解筒4 8所分解的分解氣體’經通過配管5 0而被送 入洗條器6 1中’然後再送往冷凝益3 7 b中。被迭；住冷丨规益 3 7 b中的分解氣體將經冷卻而油化。經油化的油將經配管 8 6而被送入儲油槽3 8 b中，且此油將部分利用供給油槽 ST2而被送往上述第1、第2熱風產生爐35,36中。另外， 上述冷凝器37a，37b係利用冷卻塔CT而冷卻（圖3)。 在第1段、第2段分解筒4 7，4 8上將連接著銜接於收集 排氣管1〇〇上的配管1〇1，1〇2。所以，第1段、第2段分 解筒4 7,4 8的排氣便經由配管101，102而從收集排氣管100 排放出於外部。此外，未被連接於上述第2段分解筒4 8 上之冷凝器3 7b所油化的氣體，則將利用泵P並經由配管 8 6而回收於儲油槽3 8 b中。 在上述所說明的融解部31與分解筒47，48中，部分採用 伸縮筒700。伸縮筒700係由蛇腹管部701與滑動部702 所形成（圖19)。蛇腹管部701係由蛇腹管7 0 3、及配置於 其內部的蛇腹管內筒704所構成，蛇腹管內筒704總長度 係較長於蛇腹管703總長度。蛇腹管7 03與蛇腹管內筒704 係設置呈其中一端切齊，而蛇腹管內筒704則突出於蛇腹 管7 0 3另一端的狀態。然後，在突出的蛇腹管內筒7 04外 圍上配置著支撐筒705，俾由此蛇腹管內筒704與支撐筒 19 312/發明說明書(補件)/92-04/92101606 200302867 7 0 5構成滑動部7 02。支撐筒7 0 5內徑係形成略大於蛇腹管 內筒704外型，且支撐筒7 0 5內周面與蛇腹管內筒704外 周面形成滑動面。另外，在圖1 9所示中，在支撐筒7 0 5 未位於蛇腹管內筒704上的部分，配置著由與蛇腹管內筒 704相同直徑而所形成的內筒706，並在蛇腹管內筒704 與內筒7 06相突接端處形成相對應的楔形部7 04a，7 06 a。 此情況下，二楔形部7 04 a，7 06 a的相對向面便形成滑動面。 如此的話，當在融解部3 1與段分解筒4 7,4 8之其中一部 份上所配置的伸縮筒7 0 0，被融解部3 1與段分解筒4 7,4 8 所加熱而熱膨脹的情況時，便具有吸收此熱膨脹量的作 用。換句話說，譬如當第1融解筒3 1 a被從常溫加熱至200 °C前後，並隨熱膨脹而使總長延伸的情況時，在第1融解 筒3 1 a其中一部份上所配置的伸縮筒7 0 0，便依收縮蛇腹 管7 0 3而使蛇腹管內筒7〇4朝滑動部7 02側移動之方式進 行收縮，俾吸收第1融解筒3 i a的膨脹量。 再者，圖19中所示的伸縮筒700，因爲將蛇腹管內筒 7 0 4的滑動位置設計於蛇腹管部7 0 1外部，並採用較蛇腹 管內筒704更大徑的支撐筒7 0 5形成滑動部702，因此便 可不致使蛇腹管內筒7 0 4內徑變小，且可使蛇腹管內筒7 0 4 形成厚壁狀態。藉此便可防止伸縮筒7 0 0產生變形現象， 甚至可消除隨伸縮筒7 0 0變形而所產生的蛇腹管7 0 3損壞 情形，便可防止因從蛇腹管703損壞處洩漏出分解氣體等 而釀成火災的情形發生。 其次，針對脫氯處理部3 3的細部進行說明。 20 312/發明說明書(補件)/92-04/92101606 200302867 從融解部3 1之融解筒3 1 a，3 1 b，3 1 c上面所延伸出的配管 7 5，7 6，7 7係連接於配管7 8 (圖5 )，而配管7 8則連接於第1 分離器3 9 a (圖1 0)。第1分離器3 9 a係供將融解筒 31a，31b，31c中所產生的氯化氫氣體，與其中所含的若干分 解氣體予以分離用。第1分離器3 9 a在上半部設有冷卻盤 管3 0 1。在配管7 8中流動的氯化氣氣體’在通過冷卻盤管 3 0 1之際將被冷卻，並被排放於位於較冷卻盤管3 0 1更下 方位置處的第1分離器3 9 a下半部中。所排放出的氯化氫 氣體，更將通過冷卻盤管301而從第1分離器39a上半部 經由配管7 9，被送往與第1分離器具相同構造的第2分離 器3 9b中。經第2分離器39b所分離的氯化氫氣體將被送 往與第1、第2分離器39a，3 9b具相同構造的第3分離器 3 9c中，並在利用第3分離器39c而與分解氣體完全分離 之後，便經由配管8 1而被送往反應器3 0 0的下半部中。藉 由配置著該等複數個分離器39a，39b，39c，便可將氯化氫氣 體從分解氣體中完全的分離。 反應器3 0 0係具有攪拌棒3 0 6，並在此攪拌棒3 0 6上安 裝著葉片308。反應器300的上半部連接於消石灰槽83。 爲將消石灰槽8 3內的消石灰予以乾燥，便在消石灰槽8 3 周圍設置加熱筒3 05。在消石灰槽83下半部設有導螺桿 3 0 3，此導螺桿3 0 3利用馬達3 04而進行旋轉。 再者，在反應器3 03下端設有導螺桿3 09，此導螺桿309 利用馬達3 1 0而進行旋轉。在導螺桿3 09周圍，爲將經反 應器之反應而所產生的水予以乾燥去除，便利用加熱筒 21 312/發明說明書(補件)/92-04/92101606 200302867 3 1 3進行加熱。在反應器3 0 0內之反應而所產生的氯化鈣， 將被收容於氯化鈣槽3 1 2中。此外，在反應器3 0 0的高度 方向上適當位置處，設有溫度偵測計S 1，S 2，S 3，利用溫度 偵測計S 1，S 2，S 3而檢測出反應熱，並藉由此反應熱檢測信 號控制著消石灰槽8 3的馬達3 04、與反應器3 00之排放用 導螺桿3 0 9的馬達310轉動。換句話說，反應器3 00的攪 拌棒3 06經常進行旋轉，若氯化氫氣體大量的進入反應器 3 0 0內的話，反應將便激烈而產生大量反應熱。所以，當 最高位置的溫度偵測計S 3檢測出一定以上的反應熱之 時，便依大量送入消石灰之方式，使消石灰槽8 3的導螺桿 3 〇 3進行旋轉。然後，在隨反應之進行，反應熱產生減少 而溫度略爲下降，且位於中間位置的溫度偵測計S2檢測 出一定範圍的溫度期間，便配合此而供應消石灰。然後， 當反應變遲緩且最高位置的溫度偵測計S 1檢測出既定溫 度的話，便判斷反應已結束，而使反應器3 00的排放用導 螺桿3 09進行旋轉，俾將所產生的氯化鈣回收於氯化鈣槽 3 1 2中。在回收所產生的氯化鈣之後，若再度開始反應的 話，溫度偵測計S 1便感測此反應的開始，並使導螺桿3 03 產生旋轉而從消石灰槽8 3中將消石灰送入反應器3 0 0內， 隨溫度偵測計S 2，S 3依序檢測出反應熱，增加消石灰的供 應，並依循反應熱的下降而減少消石灰的供應量，且重複 著上述動作。 通常，氯化氫氣體可謂若無溶劑的話，將無法在乾體的 中和劑中進行反應，在此便利用氯化氫氣體與消石灰進行 22 312/發明說明書(補件)/92-04/92101606 200302867 反應時所產生的水當作溶劑使用，而促進中和反應。此反 應式如下所示： 2HCl + Ca(0H)2 = CaCl2 + 2H20 另外，在此反應中，爲將以水蒸氣狀態所產生的水予以 去除，以及爲將氯化氫氣體抽入反應器300中，而設置真 空泵3 1 4。爲將此真空泵3 1 4的吸取負載設爲一定，而在 真空泵314的進口側設置供流入空氣用的放洩閥（relief valve)315。此外，爲將反應器300中未充分反應的氯化氫 氣體予以去除，而設置鹼洗淨用洗滌器3 1 7。 其次，針對廢氣處理部34進行說明。 圖1 1所示係廢氣處理部3 4的槪略構造圖。如圖1 1所 示，廢氣處理部3 4係具有殼體2 3 6。在油化設備動作中， 殼體2 3 6經常連結於燃燒器2 3 4，並將殼體2 3 6內加熱至 約 1 2 00 °C。 再者，在上述殼體2 3 6內，立設複數個陶瓷角柱 2 3 8，2 3 8，…，2 3 8。此陶瓷角柱係將從銜接於上述儲油槽 38 a，38b的入口 2 3 5所流入的廢氣，在1/100秒〜2/100秒 內進行接觸分解，而變化爲C02、NOx、H20等單純氧化 物。此時，所產生的熱能便通過出口 2 3 7而被導入於第1、 第2熱風產生爐35,36中。 廢氣係未被冷凝器37a，3 7b所油化的乙醛等環境激素 (e n v i r 〇 m e n t h 〇 r m ο n e)，在本實施例中，利用儲油槽3 8 a，3 8 b 先暫時回收之後，在從該等儲油槽38a，3 8b送往廢氣處理 部34。此外，廢氣亦可從冷凝器37a，3 7b直接送往廢氣處 23 312/發明說明書(補件)/92-04/92101606 200302867 理部3 4。 其次’針對傾斜管內的安全系統及脫臭系統進行說明。 如圖2 0所示，在融解部3 1的各融解管、及分解部3 2 的各傾斜管上設置著多數個溫度偵測計S，S，…，S。該等溫 度偵測計S連接於控制器5 1 1，而此控制器5 1 1則控制著 連接於二氧化碳高壓瓶5 1 2上之閥5 1 3的開關。此二氧化 碳高壓瓶5 1 2係連接於將來自第卜第2熱風產生爐3 5，3 6 的熱風，送入融解部3 1與分解部3 2內的熱風循環路Q上。 所以，控制器5 11在當溫度偵測計S檢測出如意外等異常 溫度之情況時，便開啓閥5 1 3，而將二氧化碳經由熱風循 環路Q內而供應給融解部3 1與分解部3 2內。藉此融解部 3 1與分解部3 2內便被冷卻，而使油化設備3 〇的運轉停止。 在所處理的塑膠囤積場A中’於上方設置具吸取風扇 5 1 4 a的吸取裝置5 1 4。所以，特別係指從廢塑膠所產生的 惡臭空氣，將被吸取裝置5 1 4所吸取，並被送往熱風產生 爐3 6中進行燃燒而脫臭。 再者，利用粉碎機5 1 5而粉碎的塑膠碎片p，利用乾燥 機5 1 6並使用來自熱風產生爐3 6的熱風而進行乾燥，經乾 燥後的塑膠碎片P便被送往漏斗4 1。在此若在乾燥機5 i 6 內利用熱風將塑膠碎片P進行乾燥的話，將有可能使附近 充滿惡臭的情形發生。其中，乾燥機5 1 6內具惡臭的空氣， 便在利用風扇516a而由旋風器（Cyclone)517將混入空氣中 的細小粒子予以去除之後，再送往熱風產生爐3 5中進行處 理。藉由該等系統便可期待充分的除臭效果。 24 312/發明說明書(補件)/92-04/92101606 200302867 再者，具惡臭的空氣亦可利用供處理廢氣用的廢氣處理 部3 4進行分解。換句話說，具惡臭的空氣將利用熱風產生 爐3 5，3 6或廢氣處理部3 4進行處理。 在上述實施例中，雖將分解筒設計呈二段，但是亦可設 置如圖1 2所示的融解部2 0 0，該融解部2 0 0係在第2段分 解筒4 8之後，設置著與第2段分解筒4 8具相同構造且依 相同角度傾斜的第3段分解筒2 1 0，各個溫度分布則設計 爲：第1段分解筒爲3 5 0〜4 00°C、第2段分解筒爲400〜4 80 °C、第3段分解筒爲4 8 0〜5 8 0 °C。如此的話’藉由將分解 筒設定爲三段，因爲可將分解溫度分布更加緩和，且分解 時間亦將變長，因此便可對應隨原料塑膠比重等的分解條 件變化，而保證確實的二次分解。 換句話說，第2段分解筒4 8上端透過落下筒2 1 8而銜 接於相同傾斜角度的第3段分解筒2 1 0下端，而未被第2 段分解筒4 8所抽取出的未分解起泡狀塑膠及分解氣體’將 經由落下筒2 1 8而被送往第3段分解筒2 1 0內。經送入第 3段分解筒2 1 0內的未分解起泡狀塑膠及分解氣體’將由 第3段分解筒2 1 0進行二次分解’經二次分解過的分解氣 體便經由鹼洗淨的洗滌器2 1 6且被冷凝器3 7 c所冷卻油 化，而形成相當A重油的油。此油便經由配管2 1 4而被回 收於儲油槽2 1 5中。在第3段分解筒2 1 0中銜接著鼓風機 2 2 1，藉此便形成加熱空氣從分解筒的上朝下的逆熱梯度狀 態並進行循環。此外，殘澄將通過污泥管2 1 9而被回收於 經注入水的污泥槽2 2 0中。未被上述第3段分解筒2 1 0之 25 312/發明說明書(補件)/92-〇4/921016〇6 200302867 冷凝器3 7 c所油化的分解氣體，將利用泵P而被吸取並通 過配管2 1 4而回收於儲油槽2 1 5中。將在第1段、第2段 分解筒47，48中經二次分解過的分解氣體，從上端部抽取 出並油化，而此時尙未完全二次分解的氣體將利用過熱器 1 5 1，1 5 2而分解。在第2段分解筒中將獲得如輕油、燈油、 部分相當於重油成分的分解氣體，剩餘的相當於A重油之 成分便利用第3段分解筒進行分解。此外，更可將分解筒 設定爲四段以上。 再者，在圖12所示實施例中，融解部200係形成型（垂 直型）。β卩，第1、第2、第3融解筒201，202,203係在垂 直方向上’分別透過銜接部204,2 05而連結在一起，從漏 斗4 1所送至的塑膠便在第1融解筒20 1中被朝右方向移 送，在第2融解筒2 02中則被朝左方向移送，在第3融解 筒中被朝右方向移送，然後再供應給第1段分解筒4 7的下 端部。最下段的第3融解筒203之導螺桿2 07將利用馬達 2 0 8而旋轉，此馬達2 0 8的旋轉係利用鏈2 0 9而使第1融 解筒2 0 1的導螺桿2 0 6進行旋轉，此導螺桿2 0 6的旋轉則 透過齒輪G 1，G 2而使第2融解筒2 0 2的導螺桿2 2 1進行旋 轉。熱風係利用鼓風機2 1 3而從融解部2 0 0中溫度較低的. 上側被抽取出，然後經由配管2 2 2而被送往下側，而在融 解部內朝上方進行循環。 在圖2 1所示實施例中，第1〜第4融解筒3 1 a，3 1 b，…，3 1 d 係利用從熱媒加熱裝置600所供應的熱媒進行加熱。此處 所謂的熱媒係指液體的熱媒，譬如採用各種熱媒油。此熱 26 312/發明說明書(補件)/92-04/92101606 200302867 媒利用熱媒加熱裝置6 0 0加熱至既定溫度’並經由熱媒配 管60 1而供應給融解筒3 1的熱媒空間1 3 5 熱媒空間1 3 5 ’ 係如同前述之熱風空間1 3 5般，形成於內筒1 3 1與外箱1 3 6 之間。所以，熱媒便在熱媒空間1 3 5 ’中依從下游側朝上游 側流動之方式，利用循環泵602進行循環。相關在第1融 解筒3 1 a內控制於1 90〜2 00 °C，在第2融解筒3 lb內控制 於210〜2 3 0 °C，在第3融解筒31c內控制於2 3 0〜2 60 °C， 在第4融解筒31d內控制於3 00〜340 °C的情況，上述之各 別的控制則如同上述利用熱風進行加熱的情況相同。 如此的話，藉由改變熱風並採用熱媒，便可達下述效果：a) 可大幅改善熱傳效率；b)相較於熱風之下，因爲熱媒較不 易冷卻，因此即便設備停止時，融解筒3 1內的溫度亦較不 易下降’當啓動設備之際便可在短時間內啓動，以及c)即 便融解筒3 1的內筒1 3 1產生破損的情況時，仍可防止釀成 火災意外。 再者，因爲一般熱媒的動作溫度在3 5 0 °C以下，因此雖 僅融解筒3 1加熱採用熱媒，但是藉由選擇適當的熱媒，亦 可使分解筒47，48的加熱亦採用熱媒進行。此外，亦可隨 所採用熱媒的動作溫度’而在融解筒3 1中僅被控制於低溫 的融解筒31(譬如：第1、第2、第3融解筒31a，31b，31c) 利用熱媒進行加熱。 在圖1 3所示實施例中，第4融解筒3〗d與第〗段分解 筒47下半部乃利用銜接部5 00而相銜接，並經由此銜接部 5 〇〇而將經融解過的起泡狀塑膠供應給第1段分解筒47內 312/發明說明書(補件)/92-04/92101606 200302867 的內筒2 5 5下端。此外，對上述銜接部5 ο 〇供應 內所儲存的植物性或動物性食用油或該等使用後 等，該等油與起泡狀塑膠的混合物，便利用各分 行1次、2次分解。藉此，便可將經改質過的油） 分解反應進行回收。 一般乃如圖1 4所示，將如聚乙烯、聚丙烯、聚 A B S樹脂、丙烯酸樹脂等塑膠，進行熱分解並有 生成油而被收集，其餘的則當作廢氣（7〜8%)使用 氣處理部34進行處理，碳化物（2〜3%)則當作殘達 集於殘渣槽4 〇中。聚氯乙烯則利用石灰進行中和 5 8 %變成氯化鈣，約4 2 %則將被熱分解，經油化ϋ 的部分約3 0 %程度。 再者，在2〇〇2年1月25日所提出申請之包括 申請專利範圍、圖式、摘要在內的日本專利申請 (Νο.2002-017650 號）、及在 2002 年 10 月 16 日所 之包括說明書、申請專利範圍、圖式、摘要在內 利申請案（No .2002-3 0 1 8 95號）中的所有揭示內容 照全部而被組合於本說明書中。 再者，本發明並不僅限定於上述實施形態。上 態僅爲例示而已，舉凡與本發明申請專利範圍中 術思想具有實質相同的構造，並達相同作用功效 於涵蓋在本發明的技術範疇之內。 【產業上可利用性】 如上述，相關本發明的塑膠油化方法及油化設 312/發明說明書(補件)/92-04/92101606 著槽5 0 2 的廢油等 解筒而施 W用化學 苯乙烯、 9 0 %當作 並利用廢 i而被收 ]而有約 Ϊ被收集 說明書、 案 提出申請 的曰本專 ，經由參 述實施形 所記載技 者，均屬 備，乃屬 28 200302867 於可有效當作供從廢氣塑膠採收油之用的塑膠油化方法及 油化設備。 【圖式簡單說明】 圖1爲本發明基本原理的構造圖。 圖2爲根據本發明基本原理之實施例的構造圖。 圖3爲本發明一實施例的油化設備之立體示意圖° 圖4爲本發明一實施例的油化設備之正視圖。 圖5爲本發明一實施例的油化設備之平面圖。 圖6爲圖5之槪略構造說明圖。 圖7爲圖4之槪略構造說明圖。 圖8爲融解筒之橫切剖圖。 圖9爲分解筒之橫切剖圖。 圖1 〇爲脫氯處理部的構造圖。 圖11爲廢氣處理部的構造圖。 圖1 2爲其他實施例的槪略構造說明圖。 圖1 3爲融解部與分解部間之銜接部的構造圖。 圖1 4爲對應所處理塑膠的回收率圖。 圖1 5爲起泡狀塑膠之拉上狀態說明圖。 圖1 6爲漏斗之橫切剖圖。 圖1 7爲非加熱部的立體示意圖。 圖1 8爲污泥槽之構造圖。 圖19爲伸縮筒之構造圖。 圖20爲防止意外系統與脫臭系統的槪略構造圖° 圖2 1爲其他實施例的槪略構造圖。 312/發明說明書(補件)/92-04/92101606 29 200302867 (元件符號說明） 1 儲存部 2 內筒 3 熱風空間 4 熱風空間 5 外箱 6 外筒 7 導螺桿 8 螺旋葉片 9 配管 10 配管 12 馬達 13 分解筒 14 旋轉軸 14a 軸前端 15 配管 17 外筒 20 內筒 2 1 外筒 22 配管 24 導螺桿 25 內筒 26a 配管 26b 配管 312/發明說明書(補件)/92-04/92101606200302867 发明 Description of the invention [Technical field to which the invention belongs] The present invention relates to a method and a device for oiling a plastic for collecting oil from plastic. [Prior Art] Although various proposals have been made for oiling equipment for collecting oil from waste plastics, they have not been sufficiently decomposed, and practically no equipment exists. Therefore, the applicant of the present case has previously developed a small and simple structure inverse thermal gradient method (reve v er s e t h e rm a 1 g r a d i en t t y p e) as disclosed in Japanese Patent Laid-Open No. 2000-0-16774. However, in this oiling equipment, there are the following problems: 1) Although the plastic can be reliably oiled when the amount of plastic processing is small, but if the plastic processing becomes more, it is difficult to completely Plasticization of plastics; 2) When melting PVC (polyvinylchlorid) plastics, hydrogen chloride gas will be generated in the melting section, but the treatment of hydrogen chloride gas is not fully implemented; 3) off-gas that is not oilized (off- gas), and insufficient implementation. [Summary of the Invention] Therefore, the present invention is mainly in view of these problems, and its main object is to provide an oiling method capable of oiling a large amount of plastics, processing hydrogen chloride gas, and completely treating exhaust gas, and oil.化 设备。 Equipment. The reason is that in the oiling method of the present invention, the plastic is heated and melted to produce a foamed plastic. The foamed plastic is taken out, heated and depolymerized, and then cooled to produce oil. At this time, the blister-like plastic can be pulled upward obliquely (preferably relative to 6 312 / Invention Specification (Supplement) / 92-〇4 / 92101606 200302867 at an angle of 25 to 30 ° horizontally) and taken out. In addition, the foamed plastic can be heated while being pulled upward obliquely, and the foamed plastic can be heated at a higher temperature from the upper position. In addition, food oil, animal oil, or mineral oil can be added to the melted plastic and heated to produce a blistering plastic composed of these mixtures. Furthermore, in the oiling method of the present invention, the hydrogen chloride gas generated during the melting of the plastic can be separated from other decomposed gases, and then reacted with slaked lime to form a chloride salt and recovered. In addition, the non-oiled exhaust gas may be subjected to a contact decomposition treatment using a high-temperature ceramic. Furthermore, the oiling equipment of the present invention is provided with: a melting part that heats and melts plastic to generate foamed plastic; and takes out the foamed plastic, heats, depolymerizes, and cools to produce oil. Decomposition department. In this oiling equipment, the disassembling section may also be provided with a take-out mechanism for pulling out the blister-like plastic obliquely upward (preferably at an angle of 25 to 30 ° with respect to the horizontal). The decomposing unit may be provided with a heating mechanism that heats the foamed plastic while pulling it upward obliquely, and heats the foamed plastic at a higher temperature from the upper position. The connecting portion of the melting portion and the dissolving portion may be provided with an oil injection mechanism for injecting food oil, animal oil, or mineral oil. In addition, the melting section may be formed of a plurality of melting tubes having different temperature distributions; the dissolving section may also be formed of a plurality of inclined decomposition tubes having different temperature distributions. Furthermore, the oiling equipment of the present invention may be provided with a dechlorination device for processing the hydrogen chloride gas generated in the melting section; the dechlorination device may also be provided with: Separator 312 / Invention Specification (Supplement) / 92 · 04/92101606 200302867 separator; and a reactor in which hydrogen chloride gas separated by the separator is reacted with slaked lime to form calcium chloride. In addition, an exhaust gas treatment device may be provided which treats the exhaust gas that has not been oil-formed after being cooled in the decomposition unit, and is subjected to contact decomposition using a high-temperature ceramic. Furthermore, in the oiling equipment of the present invention, a residue recovery mechanism may be provided at the upper end of the decomposition tank in the final stage in the multi-stage decomposition tank; the residue recovery mechanism may also place the upper opening at the upper end position of the decomposition cylinder in the final stage. 'And the lower opening is formed in a cylinder in an inert gas environment that is heavier than air. Furthermore, the oiling device of the present invention is also a device: a funnel for storing plastic and supplying it to a melting section; the funnel is provided with a lead screw having a spiral blade. In addition, a non-heating portion formed by an unheated area of a predetermined length may be provided between the funnel and the melting portion. The plurality of melting cylinders are provided with a lead screw having helical blades for conveying plastic, and the lead screw blade pitch of the leading melting tube is larger than the lead screw blade pitch of other melting tubes. Furthermore, the melting unit and the disintegrating unit of the present invention are provided with: an inner cylinder; an outer cylinder formed on the periphery of the inner cylinder; a hot air space formed by circulating hot air between the inner cylinder and the outer cylinder; A temperature detector for the temperature of the melting section and the decomposition section. In addition, it may be provided with a carbon dioxide supply device that sends carbon dioxide to the hot air space when the temperature detector detects an abnormal temperature above a predetermined temperature. Furthermore, the melting unit and the disintegrating unit of the present invention are provided with: an inner cylinder; an outer cylinder formed at the periphery of the inner cylinder; and an inner cylinder and an outer cylinder 312 / Invention Specification (Supplement) / 92 -04/92101606 8 200302867 hot air space circulating hot air; in addition, it can be equipped with: a hot air generating device for supplying hot air generated by combustion to the hot air space; and drying and drying the plastic supplied to the melting furnace Device; the air in this drying device can also be supplied to the hot air generating device and deodorized by burning. In addition, the air in the drying device can be supplied to the exhaust gas treatment device, and the high-temperature ceramics can be used to decompose and deodorize. Furthermore, a part of the melting barrel of the oiling equipment of the present invention is a telescopic barrel formed by telescoping, and the telescopic barrel is formed by an inner tube, a bellows tube, and an outer tube, and the bellows tube system is configured At the periphery of the inner tube, one end is fixed to the inner tube, and the other end can slide the inner tube; the outer tube is fixed to the other end of the bellows tube, and the inner tube is slidably received in the inner tube. Furthermore, the melting unit of the present invention is provided with a melting unit including: an inner cylinder; an outer cylinder formed on the periphery of the inner cylinder; and a heat medium formed between the inner cylinder and the outer cylinder to circulate a liquid heat medium Space; and a heat medium supply device for supplying a liquid heat medium to the heat medium space may be further provided. [Embodiment] Hereinafter, embodiments of the present invention will be described with reference to the drawings. Fig. 1 is a schematic diagram for explaining the basic principle of the method for oiling a plastic according to the present invention. The raw plastic is thawed at a temperature of 20 ° C to 350 ° C and stored in the storage unit 1. The melted plastic (melt plastic) is conveniently pulled up obliquely with the disassembly cylinder 1 3. Among them, the decomposition cylinder 13 includes: an inner cylinder 2; an outer cylinder 6 forming a hot air space 4 around the inner cylinder 2; and a lead screw 7. The lead screw 7 is composed of a rotating shaft 9 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867 1 4 and a spiral blade 8 and is rotated by a motor 12 at a speed of 4 to 5 rpm. Hot air is supplied to the hot air space 4 from the pipe 100. The temperature in the inner cylinder 2 is maintained at 350 to 620 ° C in order to vaporize and depolymerize the plastic. The melted plastic transported in the inner cylinder 2 by the lead screw 7 is decomposed once under the decomposition cylinder 13 (From the melting state to the initial heavier gas state of gasification), and a primary decomposition gas is formed. The primary decomposition gas is conveniently sent to the decomposition cylinder 1 3 at a low speed using the lead screw 7 and is performed in the inner cylinder 2 maintained at 3 50 0 to 62 0 ° C using hot air supplied from the pipe 15. Secondary decomposition (if the plastic is depolymerized and cooled, it will be in an oily state) 'to form a lighter secondary decomposition gas. Moreover, if the secondary decomposition of all the oil components contained in the plastic of the raw material is performed in the upper part of the decomposition cylinder, only one decomposition cylinder is sufficient, and two decomposition cylinders can also be used, and The person connected to the storage unit 1 is regarded as the first-stage disintegrating cylinder, and the second-stage dissolving cylinder is connected to the first-stage dissolving cylinder. Further, an outer box 5 for forming the hot air space 3 is provided on the outside of the storage unit 1, and hot air is fed into the hot air space 3. The plastic supplied to the storage unit 1 is heated to 200 ~ 3 5 (TC to form a melted plastic mp, and at the same time, a foamed plastic (foamed plastic) f is formed on the surface portion. This foamed plastic f uses the shaft front end 14a The lead screw 7 immersed in the melted plastic mp is heated obliquely while being pulled upward. At this time, the contact area with heat will increase, so it will be decomposed (depolymerized) surely to form a secondary Decomposed gas. Secondary decomposed gas is collected from piping 9, cooled and oiled, and then recovered in the oil storage tank. 312 / Invention Specification (Supplement) / 92-〇4 / 92 ΚΠ 6〇6 10 200302867 Again The drawing speed of the foamed plastic f can be 30 to 60 cm / min. If it is lower than this, the conveying efficiency will be deteriorated. On the contrary, if it exceeds this, it will not be able to be fully decomposed. For example, foamed plastic f f It is pulled up spirally by the lead screw 7 shown in FIG. 15. The spiral-shaped moving speed at this time is preferably 30 to 6 cm / min. This speed is adjusted by using the pitch P of the lead screw 7, for example. In this case, the foam-like plastic f will be included at the above speed. It is transported in 2 and slowly heated, and is fully decomposed (depolymerized) in the primary decomposition temperature region and the secondary decomposition temperature region. The foamed plastic f can be around 600 ° C until the secondary decomposition is completed. Heating for about 14 ~ 15 minutes. Although the raw materials are different in plastic type and the processing temperature will be different, it is best to set the temperature of the storage unit 1 to melt the plastic mp to form a bubble. Temperature (2 00 ~ 3 50 ° C), in addition, in order to obtain a good decomposition, set a milder temperature gradient and maintain a longer foaming state, and increase the contact area with heat is It's important. For this reason, the decomposition tube 1 3 can be designed to be inclined to the horizontal state. In addition, in the inclined decomposition tube 13, the temperature is gradually increased from the lower half to the upper half by blowing hot air into the upper half and then circulating from the upper half to the lower half. This method is the so-called "reverse thermal gradient type". In order to maintain the foam-like plastic f for a good long time, it is preferable to set the inclination angle 0 of the decomposition tube 27 to 25 ° to 30, as shown in FIG. . If the inclination angle 0 of the decomposition tube 27 is lower than 25 °, the bubble-shaped plastic f will flow quickly in the lateral direction and disappear in a short time. On the contrary, if the inclination angle β is set to exceed 30 °, it will follow The relationship between gravity is quite difficult to melt plastic 11 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867 mp surface will pull up the foam-like plastic f long distance upward, in this case, the foam-like Plastic f will also disappear in a short time. In FIG. 2, the storage portion 29 of the melted plastic mp is formed at a connecting portion connecting the supply cylinder 28 and the disassembly cylinder 27 in a V-shape. The supply cylinder 28 is composed of an inner cylinder 20 and an outer cylinder 21, and a pipe 22 is interposed therebetween to supply hot air. The inner cylinder is maintained at 2 0 ~ 3 5 0 ° C. The decomposition tube 27 is composed of an inner tube 25, an outer tube 17 and a lead screw 24. The lead screw 24 is installed in such a manner that the lower end of the shaft 23 is rotatably supported on the lower wall of the storage portion 29. Between the inner tube 25 and the outer tube 17, heated air of 450 to 620 ° C is supplied from the hot-air generating furnace through a pipe 26c. Then, the heated air is circulated by descending inside the decomposition tube 27 and withdrawing from the pipe 26b in the lower half of the decomposition tube, and then flowing in through the pipe 26a in the upper half. In this way, if high-temperature air is circulated from the upper half to the lower half in the decomposition cylinder 27, the temperature distribution in the decomposition cylinder 27 becomes a state where the temperature becomes higher from the bottom to the top. The lower half of the decomposition tube 27 is maintained at 3 00 ~ 4 5 (TC for the first decomposition, and the upper half of the decomposition tube 27 is heated to approximately 600 ° C for the second decomposition. In the storage section A bubble-shaped plastic f is generated in 29, and the bubble-shaped plastic f is conveniently transported in a good state by rising in the inclined decomposition tube 27, and is heated to form decomposition gas during the transportation. The decomposition tube 27 It is in a V-shaped connection state with the supply cylinder 28, because the melted plastic mp is completely enclosed in the storage portion 29, so the decomposed gas does not flow back from the decomposition cylinder 27 to the supply cylinder 28 and is in a safe state, and prevents air from passing through from the outside The storage section 2 9 enters the decomposition tube 2 7 'and there is no danger of explosion. 12 312 / Invention Manual (Supplement) / 92-04 / 92101606 200302867 Next, the oiling equipment using this plastic oiling method will be described. In FIGS. 3 to 7, the oiling device 30 of the present invention is provided with a melting section 3 1 that melts waste plastic such as raw materials, and performs one-time decomposition of the plastic melted in the melting section 31. With secondary decomposition of the decomposition section 3 2; In the case of PVC, a dechlorination treatment section 3 3 that performs a dechlorination treatment; an exhaust gas treatment section 3 4 for the treatment of the waste gas generated when the plastic is melted and decomposed; and a hot air that generates a heat source that is a heat source during the melting and decomposition The first and second hot-air stoves 35 and 36. As shown in FIG. 6, the melting section 31 is provided with a first melting tube 3 1 connected to a funnel 41 for feeding raw materials through a non-heating section 4 1 0. a; the front end is connected below the front end of the first melting tube 3 1 a and perpendicular to the second melting pot 3 1 b of the first melting tube 3 1 a; the rear end is connected below the front end of the second melting tube 3 1 b and is vertical The third melting tube 3 1 c is located on the second melting tube 3 1 b; and the rear end is connected below the front end of the third melting tube 3 1 c and is perpendicular to the fourth melting tube 3 1 d of the third melting tube 3 ic. In this case, the first to fourth melting cylinders 3 1 a, 3 1 b, ..., 3 1 d are arranged in a rectangular shape as a whole, and the melting plastic will sequentially fall from the front of the decomposition cylinder toward the rear of the next melting cylinder and proceed. Conveying. The melting tubes 3 1 a ~ 3 1 d can also be connected horizontally. The funnel 4 1 is shown in Figure 16 and is formed by the following components: funnel-shaped shell A body 411; a cover body 412 covering the upper surface of the housing 411; a motor 4 1 3 arranged at the center of the cover body 412; and a motor 4 connected to the motor 4 and extending through the housing 4 1 1 by a rotating shaft 4 A lead screw 4 1 4 composed of a spiral blade 4 1 4b mounted on a rotating shaft 4 丨 4a. The spiral blade 41 of the lead screw 4 i 4 has a funnel shape along the shape of a lead screw 414. 414 312 / Invention Specification (Supplement) / 92-04 / 92101606 13 200302867 The space W between the inner wall and the periphery of the spiral blade 414b is designed to be about 2 to 5 cm. The lead screw 4 1 4 is rotated at a predetermined speed by using a motor 4! 3 to prevent lighter plastic from being blocked in the funnel 41. The heavier plastic will fall through the space w between the inner wall of the lead screw 4 1 4 and the periphery of the spiral blade 4b. The lighter plastic pieces will be surely sent into the non-heating part 410 with the lead screw 414. . The non-heating section 4 10 is formed in a cylindrical shape and is connected to the lower half of the funnel 42 (see FIG. 17). A motor * 2 is provided at the end of the non-heating section 4 10, and the motor 4 2 is connected to a lead screw 1 3 7 which is common to a lead screw 1 3 7 arranged in the melting cylinder 3 1 a described later. The lead screw 1 3 7 is rotated by the motor 4 2, and the plastic chips sent from the funnel 41 1 are slowly forwarded and supplied to the melting barrel 3 1 a ° Furthermore, the non-heating part 4 1 0 is different In the melting tube 31 described later, heating by hot air is not performed. Therefore, because the mounting part of the funnel 41 and the melting tube 31 are separated, the plastic will not start to melt near the mounting part of the funnel 41, which can prevent the lead screw 1 3 7 from being caused by the viscous impedance of the melted plastic. The rotation stops. In other words, the unmelted plastic portion can be lengthened by keeping the melted portion of the plastic away from the funnel 41 1 mounting portion, and the unmelted plastic can be pushed forward to squeeze the melted plastic. The melting section 3 1 is composed of a rectangular outer box 1 3 6 and an inner tube 1 3 1 provided in the outer box 1 3 6 (Fig. 8). A lead screw 1 3 7 is provided in the inner cylinder 1 3 1; the lead screw 1 37 includes a rotation shaft 1 3 3 and a spiral blade 1 3 2 provided around the rotation shaft 1 3 3. In addition, the pitch of the lead screws 1 3 7 of the first melting tube 3 1 a is set to be larger than the lead screws 14 of the other melting tubes 3 1 b, 3 1 c, 3 1 d / Instruction Manual (Supplement) / 92- 〇4 / 921 () 16 () 6 200302867 1 3 7 This is because the set temperature of the melting section 31 is lower than that of other melting barrels, as described later, so the retention density of the plastic is low and the impedance is small. The lead screw 1 3 7 is rotated by a motor (for example, the first melting cylinder 3 1 a is rotated by a motor 4 2 (FIG. 4 and FIG. 5), and the second melting cylinder 3 1 b is rotated by a motor 55). Furthermore, the inner tube 1 3 1 is provided with a plurality of heat absorbing blades 3 4 at the periphery. A hot air space is formed between the inner cylinder 1 3 1 and the outer box 1 3 6. The first melting tube 31a is controlled from 190 to 200. (: The second melting tube 31b is controlled at 210 ~ 230 ° C 'The third melting tube 3 1 c is controlled at 2 3 0 ~ 2 6 0. (: The fourth melting tube 3 1 d is controlled at 3 0 0 ~ 34CTC. In this way, the four melting cylinders 31a, 31b, ..., 31d are arranged in a rectangular shape, and the reason for gradually increasing the temperature of each melting cylinder is as follows: a) In order to implement the dechlorination of chlorine-containing plastics such as vinyl chloride, etc. To ensure a sufficient residence time (about 20 minutes); b) the temperature distribution can be easily controlled by using multiple stages to ease the temperature distribution; c) the temperature of the first melting tube 3 ia is reduced to prevent it from being in the vicinity of the funnel 41 1 The phenomenon that plastic is fused on the rotating shaft 1 3 3 is generated; and d) the length of the equipment is shortened. Furthermore, 'the hot air is supplied from each of the melting tubes 31 to the first hot blast stove 35 through the pipe 70' and this hot air is blown from the downstream end toward the upstream end of the conveyed plastic. Therefore, the inside of each melting section 31 is in a state of reverse thermal gradient. The hot air circulation in each melting section 31 is performed using blowers 5 6, 5 7, 5 8 (Fig. 4), and 60. A chimney 59 is connected to the first and second hot-air generating furnaces 35 and 36. The chimney 59 has branch pipes 59a, 59b and a discharge port 59c, and is formed in an inverted U shape (Fig. 4). The decomposition unit 3 2 is controlled by 3 5 0 ~ 4 2 0! Segment decomposition tube 4 7, 15 312 / Invention specification (Supplement) / 92-04 / 92101606 200302867, and adjacent to the first stage decomposition tube 47 and controlled to 4 5 0 ~ 5 8 (TC second stage decomposition tube 4 8 (Figure 7). The disassembling cylinders 4, 7 and 8 are arranged in a state inclined from the horizontal plane 25 to 30 °. The front end of the fourth melting cylinder 31d is connected to the first stage of dissolving cylinder 4 7 and this connecting portion will The storage section of the melted plastic is formed. The first section of the decomposition tube 4 7 is composed of two unit decomposition tubes 47 a and 47 b which are partitioned by a partition 2 5 6 to form a left and a right column (FIG. 9). The unit disassembling cylinders 47 a and 4 7b are provided with: an inner cylinder 2 5 5; a plurality of heat absorbing fans 2 5 3 provided on the periphery of the inner cylinder 2 5 5; a lead screw 1 50; Space 2 5 4. Each lead screw 150 is composed of a rotating shaft 2 51 and a spiral blade 2 5 2 and is rotated by motors 51 and 52 (FIG. 5). The second stage disassembling cylinder 48 is substantially the same as the first The structure of the one-stage decomposition cylinder 47 includes an inner cylinder 148 in each of the unit decomposition cylinders 48 a and 4 8 b (FIG. 6). A lead screw 1 4 9 is provided in the inner cylinder 1 4 8 and a lead screw 1 4 9 Then use motors 53, 54 ( (5, Figure 7) Rotate slowly (4 to 5 rpm). The upper end of the inner tube 2 5 5 of the first stage decomposition tube 47 is provided with a heating device for heating the passing decomposition gas to 580 to 620 ° C. Superheater 151 (Fig. 7). The decomposed gas that has undergone secondary decomposition in the first-stage decomposition tube 47 is extracted through the superheater 1 5 1 and the piping 49 and transmitted through the scrubber for scrubbing (ScrUbbe〇61). To the condenser 37a (Fig. 5). Then, the decomposed gas is conveniently cooled and oiled by the condenser 37a, and this oil is stored in the oil storage tank 38a through the pipe 46. The oil stored in the oil storage tank 38a Part of the oil will be supplied to the hot-air generating furnaces 35 and 36 via a server tank ST1. In addition, a valve 49a for adjusting the flow rate of the decomposed gas flowing in the pipe 49 is installed in the pipe 49. The condenser 37a must only be sent to the lighter decomposition gas completely decomposed in the secondary decomposition tube 4 7 in Section 1 16 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867, but it is derived from the pipe 4 9 The decomposition gas 'how much contains a slightly heavier incompletely decomposed gas that has not been completely subjected to secondary decomposition. So' though However, when the amount of the decomposed gas discharged from the piping 49 is small, the incompletely decomposed gas cannot exceed the upright portion of the piping 49, and will return to the first stage decomposition tube 47 and be sent to the drop tube 1 2 0. The second stage decomposition tube 4 8 'But if the amount of the decomposed gas discharged from the piping 49 is large, the' exhaust potential of the decomposed gas will increase ', so that the incompletely decomposed gas will also exceed the upright portion of the piping 4 9 and be sent to Condenser 3 7a. Therefore, the amount of the decomposed gas discharged from the piping 49 is adjusted by the valve 49a to prevent the incompletely decomposed gas from being sent to the condenser 37a. The first stage decomposition tube 47 is the same as above, because it is controlled at 3 50 ~ 4 2 0 ° C. Therefore, in the first stage decomposition tube 47, it is equivalent to the oil composition, kerosene and light oil of gasoline with lower decomposition temperature. The components of the component are decomposed once and then decomposed twice. Among them, the gas in an insufficiently decomposed state will be completely decomposed by the superheater 151. So in this case, the decomposed gas after secondary decomposition will be cooled and oiled by the condenser 37a. The gas that has not been sufficiently oiled by the condenser 37a is sucked up by the pipe 46 having the pump P, and is recovered as the exhaust gas in the oil storage tank 38a. The blister-like plastic component in the first stage disintegrating cylinder 47 that has not been completely decomposed is supplied to the lower end of the second stage dissolving cylinder 48 through the drop cylinder 120, and the lead screw in the second stage dissolving cylinder 48 is used. 1 49 while transmitting diagonally upward. The temperature in the second stage of the decomposition tube 48 is controlled to 45 0 ~ 5 8 0 ° C. Therefore, in the second stage of the decomposition tube 48, the remaining portion of the component equivalent to the light oil and light oil and the heavy oil component will also be Complete secondary decomposition. And plastic-stomach rind 17 312 / Invention specification (Supplement) / 92-〇4 / 92101606 200302867 Residues such as metal and mud put in will be collected in the sludge tank 40 through the sludge pipe 40a. The sludge tank 40 is shown in Fig. I8. Water 40b is stored, and a metal mesh 40c is provided in the water 40b. The residue will be recovered on the metal mesh 40c. By taking out the metal mesh 40 c from the sludge tank 40, the residue can be taken out from the sludge tank 40. The upper surface of the sludge tank 40 is covered by a cover 40d having an opening 40e in one part. Above the water 40b in the sludge tank 40, 塡 is filled with an inactive gas 40f that is heavier than air, such as carbon dioxide, and the lower end of the sludge pipe 40a is located in the inert gas 40f. A gas high-pressure bottle 40 g is connected to the sludge tank 40, and an inert gas 40 f is supplied from the gas high-pressure bottle 40 g to the sludge tank 40. A portion of the inert gas 40 f supplied from 40 g of the gas autoclave will overflow into the opening 40 e. In this way, by placing the lower end of the sludge pipe 40a in the inert gas 40f, it is possible to effectively prevent air from flowing into the second stage decomposition tube 48 from the sludge pipe 40a, thereby eliminating the danger of explosion. In addition, when the lower end of the sludge pipe 40a is located in the water 40b, although the lighter residue will float with the buoyancy of water and block the lower end portion of the sludge pipe 40a, but by making the sludge pipe 40a The lower end of 40a is located in the inert gas 40f, which can prevent this phenomenon, and the residue will fall into the water 40b. Hot air is supplied from the second hot-air generating furnace 36 through the pipes 71, 71a, 71b (Fig. 5) to the upper half of the first and second stages of the decomposing tubes 4 7, 4 8 and this hot air will follow the decomposing tubes 4 7 In the manner that the lower half comes out and returns to the upper half, the circulation is performed by using a blower 1 7 0, 1 7 1, 1 72. In this way, the decomposition tubes 47, 4 8 will form a reverse thermal gradient state that becomes low temperature from the upper half toward the lower half. In addition, the melting section 31 is supplied with hot air from the first hot-air generating furnace 35, 18 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867 This hot air will be, for example, in the fourth melting tube 3 1 d. The blower is used for circulation (Figure 7). A pipe 50 (FIG. 5) connected to the condenser 3 7 b through the scrubber 6 1 for alkaline washing is disposed on the upper end of the inner tube 1 4 8 of the second-stage decomposition tube 4 8. The decomposed gas' decomposed by the second-stage decomposing cylinder 48 is sent to the strip washer 61 by passing through the pipe 50, and then sent to the condensate 3 7b. The decomposed gas in the cooling 丨 benefit 3 7 b will be cooled and oiled. The oiled oil will be sent to the oil storage tank 3 8 b through the pipe 86, and this oil will be partly sent to the first and second hot air generating furnaces 35 and 36 by using the oil supply tank ST2. The condensers 37a and 37b are cooled by a cooling tower CT (Fig. 3). Pipes 10, 10 connected to the collection exhaust pipe 100 are connected to the decomposition tubes 4 7, 4 8 in the first and second stages. Therefore, the exhaust gas in the first and second stages of the separators 4, 7, 4 and 8 is discharged from the collection exhaust pipe 100 through the pipes 101 and 102 to the outside. In addition, the gas that has not been liquefied by the condenser 3 7b connected to the above-mentioned second stage decomposing cylinder 4 8 will be recovered in the oil storage tank 3 8 b by the pump P through the pipe 8 6. Of the melting section 31 and the disassembling tubes 47 and 48 described above, the telescoping tube 700 is partially used. The telescopic tube 700 is formed by a bellows tube portion 701 and a sliding portion 702 (FIG. 19). The bellows tube portion 701 is composed of a bellows tube 703 and a bellows tube inner tube 704 arranged inside the bellows tube portion 701. The total length of the bellows tube 704 is longer than the total length of the bellows tube 703. The bellows tube 703 and the bellows tube 704 are arranged with one end aligned, and the bellows tube 704 protrudes from the other end of the bellows tube 703. Then, a support cylinder 705 is arranged on the periphery of the protruding inner tube inner tube 7 04, so that the inner tube inner tube 704 and the support tube 19 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867 7 0 5 constitute Slide section 02. The inner diameter of the support tube 705 is slightly larger than that of the inner tube 704, and the inner surface of the support tube 705 and the outer surface of the inner tube 704 of the bellows form a sliding surface. In addition, as shown in FIG. 19, an inner tube 706 having the same diameter as the inner tube 704 of the bellows tube is disposed on a portion of the support tube 7 0 5 which is not located on the inner tube 704 of the bellows tube, and is placed on the bellows tube. Corresponding wedge-shaped portions 7 04a and 7 06 a are formed at the protruding ends of the inner cylinder 704 and the inner cylinder 70 06. In this case, the facing surfaces of the two wedge portions 7 04 a and 7 06 a form a sliding surface. In this case, when the telescopic cylinder 7 0 0 disposed on one of the melting section 31 and the segment dissolving tube 4 7, 4 8 is heated by the melting section 31 and the segment dissolving tube 4 7, 4 8 In the case of thermal expansion, it has the effect of absorbing this amount of thermal expansion. In other words, for example, when the first melting tube 3 1 a is heated from normal temperature to about 200 ° C, and the total length is extended by thermal expansion, the first melting tube 3 1 a is disposed on a part of the first melting tube 3 1 a. The telescopic tube 7 0 0 is contracted in such a manner that the inner tube 7 0 of the bellows tube is moved toward the sliding portion 7 02 side by contracting the bellows tube 7 0 3 and absorbs the expansion amount of the first melting tube 3 ia. Furthermore, the telescopic tube 700 shown in FIG. 19 is designed because the sliding position of the inner tube 704 of the bellows tube is designed outside the bellows tube portion 701, and a support tube 7 having a larger diameter than the inner tube 704 of the bellows tube is used. 0 5 forms the sliding portion 702, so that the inner diameter of the inner tube 7 0 4 of the bellows tube is not reduced, and the inner tube 7 0 4 of the bellows tube can be formed into a thick wall state. This can prevent the deformation of the telescopic tube 700, and even eliminate the damage of the bellows tube 70 caused by the deformation of the telescopic tube 700, and prevent the decomposition gas from leaking from the damaged portion of the bellows tube 703. Waiting for a fire to happen. Next, details of the dechlorination treatment section 33 will be described. 20 312 / Invention Manual (Supplement) / 92-04 / 92101606 200302867 The melting tube 3 1 a, 3 1 b, 3 1 c from the melting part 3 1 7 5、7 6,7 7 series The pipe 7 8 is connected to the pipe 7 8 (FIG. 5), and the pipe 7 8 is connected to the first separator 3 9 a (FIG. 10). The first separator 3 9 a is used to separate the hydrogen chloride gas generated in the melting cylinders 31 a, 31 b, and 31 c from the decomposed gases contained therein. The first separator 3 9 a is provided with a cooling coil 3 0 1 in the upper half. The chlorinated gas gas flowing in the pipe 7 8 will be cooled as it passes through the cooling coil 3 0 1 and will be discharged to the first separator 3 9 a located below the cooling coil 3 0 1. In the lower half. The discharged hydrogen chloride gas will be sent from the upper half of the first separator 39a through the cooling coil 301 to the second separator 3 9b having the same structure as the first separator through the pipe 79. The hydrogen chloride gas separated by the second separator 39b is sent to a third separator 39c having the same structure as the first and second separators 39a and 39b, and is decomposed by the third separator 39c. After the gas is completely separated, it is sent to the lower half of the reactor 300 through the pipe 81. By disposing these separators 39a, 39b, 39c, the hydrogen chloride gas can be completely separated from the decomposed gas. The reactor 300 has a stirring rod 3 06, and a blade 308 is mounted on the stirring rod 3 06. The upper half of the reactor 300 is connected to the slaked lime tank 83. In order to dry the slaked lime in the slaked lime tank 8 3, a heating cylinder 305 is set around the slaked lime tank 8 3. A lead screw 303 is provided in the lower half of the slaked lime tank 83. This lead screw 303 is rotated by a motor 304. Furthermore, a lead screw 309 is provided at the lower end of the reactor 303, and the lead screw 309 is rotated by a motor 3 10. In order to dry and remove the water generated by the reaction of the reactor around the lead screw 3 09, it is convenient to use a heating cylinder 21 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867 3 1 3 for heating. The calcium chloride produced by the reaction in the reactor 300 will be contained in the calcium chloride tank 3 1 2. In addition, at appropriate positions in the height direction of the reactor 300, temperature detectors S1, S2, and S3 are provided. The temperature detectors S1, S2, and S3 are used to detect the heat of reaction. Based on the reaction heat detection signal, the motor 3 04 of the slaked lime tank 83 and the motor 310 of the lead screw 309 for the discharge of the reactor 3 00 are controlled to rotate. In other words, the stirring rod 3 06 of the reactor 300 is often rotated. If a large amount of hydrogen chloride gas enters the reactor 300, the reaction will be intense and a large amount of reaction heat will be generated. Therefore, when the temperature detector S 3 at the highest position detects more than a certain amount of reaction heat, the lead screw 3 03 of the slaked lime tank 83 is rotated by feeding a large amount of slaked lime. Then, as the reaction progresses, the heat of reaction decreases and the temperature slightly decreases, and the temperature detector S2 located at the middle position detects a certain range of temperature, and supplies hydrated lime in accordance with this. Then, when the reaction becomes slow and the temperature detector S 1 at the highest position detects a predetermined temperature, the reaction is judged to be complete, and the lead screw 3 09 of the reactor 3 00 is rotated to rotate the generated chlorine Calcium was recovered in the calcium chloride tank 3 1 2. After recovering the generated calcium chloride, if the reaction starts again, the temperature detector S 1 senses the start of the reaction, and causes the lead screw 3 03 to rotate to send the slaked lime from the slaked lime tank 8 3 to the reaction. In the device 300, the reaction heat is sequentially detected with the temperature detectors S2 and S3, the supply of slaked lime is increased, and the supply of slaked lime is decreased in accordance with the decrease of the reaction heat, and the above action is repeated. In general, hydrogen chloride gas can be said to be unable to carry out the reaction in the neutralizer of the dry body without a solvent. Here, it is convenient to use hydrogen chloride gas and slaked lime to perform the reaction. The generated water is used as a solvent to promote the neutralization reaction. The reaction formula is as follows: 2HCl + Ca (0H) 2 = CaCl2 + 2H20 In addition, in this reaction, in order to remove water generated in a water vapor state, and to draw hydrogen chloride gas into the reactor 300, And a vacuum pump 3 1 4 is provided. In order to keep the suction load of this vacuum pump 3 1 4 constant, a relief valve 315 for inflow air is provided on the inlet side of the vacuum pump 314. In order to remove the insufficiently reacted hydrogen chloride gas in the reactor 300, a scrubber 3 1 7 for alkali cleaning is provided. Next, the exhaust gas treatment unit 34 will be described. FIG. 11 is a schematic structural view of the exhaust gas treatment section 34. As shown in FIG. 11, the exhaust gas treatment section 34 has a housing 2 3 6. In the operation of the oiling equipment, the case 2 3 6 is often connected to the burner 2 3 4 and the inside of the case 2 3 6 is heated to about 1 200 ° C. Furthermore, a plurality of ceramic corner posts 2 3 8, 2 3 8,..., 2 3 8 are erected in the casing 2 3 6. This ceramic corner post system will contact and decompose the exhaust gas flowing from the inlets 2 3 5 connected to the oil storage tanks 38 a and 38 b in the range of 1/100 second to 2/100 second, and change to C02, NOx, H20, etc. Oxide. At this time, the generated heat energy is introduced into the first and second hot air generating furnaces 35 and 36 through the outlets 2 37. The exhaust gas is not environmental hormones (environment 〇rm ο ne), such as acetaldehyde, which has not been oiled by the condensers 37a, 37b. In this embodiment, the oil storage tanks 3 8a, 3 8b are temporarily recovered, These oil storage tanks 38a, 38b are sent to the exhaust gas treatment unit 34. In addition, the exhaust gas can also be sent directly to the exhaust gas from the condensers 37a, 37b. 23 312 / Invention Specification (Supplement) / 92-04 / 92101606 200302867 Management Department 34. Next, the safety system and deodorization system in the inclined pipe will be described. As shown in FIG. 20, a plurality of temperature detectors S, S, ..., S are provided on each of the melting tubes of the melting section 31 and each of the inclined tubes of the disassembling section 32. The temperature detectors S are connected to the controller 5 1 1, and the controller 5 1 1 controls the switch of the valve 5 1 3 connected to the carbon dioxide high pressure bottle 5 1 2. This carbon dioxide high-pressure bottle 5 1 2 is connected to the hot air circulation path Q in which the hot air from the second hot air generating furnace 3 5 and 3 6 is sent to the melting section 31 and the decomposing section 32. Therefore, the controller 5 11 opens the valve 5 1 3 when the temperature detector S detects an abnormal temperature such as an accident, and supplies carbon dioxide to the melting section 31 and the decomposition section through the hot air circulation path Q. 3 2 within. As a result, the inside of the melting section 31 and the disassembling section 32 are cooled, and the operation of the oiling equipment 30 is stopped. A suction device 5 1 4 with a suction fan 5 1 4 a is provided above the plastic storage site A to be processed. Therefore, it particularly means that the malodorous air generated from waste plastic will be sucked by the suction device 5 1 4 and sent to the hot air generating furnace 36 for combustion and deodorization. Furthermore, the plastic fragments p pulverized by the pulverizer 5 1 5 are dried by the dryer 5 1 6 and hot air from the hot air generation furnace 36, and the dried plastic fragments P are sent to the hopper 4 1 . Here, if the plastic chips P are dried by hot air in the dryers 5 i 6, there is a possibility that the vicinity will be filled with malodor. Among them, the odorous air in the dryer 5 1 6 is removed by a cyclone 517 using a fan 516a, and then sent to a hot air generating furnace 35 for processing. With these systems, a sufficient deodorizing effect can be expected. 24 312 / Invention Manual (Supplement) / 92-04 / 92101606 200302867 Furthermore, the foul air can also be decomposed by the exhaust gas treatment unit 34 for treating exhaust gas. In other words, the malodorous air is processed by the hot-air generating furnaces 35, 36, or the exhaust gas treatment unit 34. In the above embodiment, although the decomposition tube is designed in two stages, a melting section 2 0 0 as shown in FIG. 12 may be provided. The melting section 2 0 0 is provided after the second stage of the decomposition tube 4 8. The third stage decomposition tube 2 1 0 has the same structure as the second stage decomposition tube 4 8 and is inclined at the same angle. The temperature distribution is designed as follows: the first stage decomposition tube is 3 5 0 ~ 400 ° C, The two-stage decomposition tank is 400 ~ 4 80 ° C, and the third-stage decomposition tank is 4 800 ~ 5 80 ° C. In this case, 'by setting the decomposition tube to three stages, because the decomposition temperature distribution can be more relaxed, and the decomposition time will be longer, so it can respond to the changes in the decomposition conditions such as the specific gravity of the raw material plastic, and ensure a reliable break down. In other words, the upper end of the second stage decomposition tube 4 8 is connected to the lower end of the third stage decomposition tube 2 1 0 through the drop cylinder 2 1 8 and is not extracted by the second stage decomposition tube 4 8 The decomposed foamed plastic and decomposed gas' will be sent to the third decomposing cylinder 2 1 0 through the dropping cylinder 2 1 8. The undecomposed blistering plastic and decomposed gas in the 3rd stage decomposition tank 2 1 0 will be decomposed by the 3rd stage decomposition tank 2 1 0. The decomposed gas after the second decomposition will be washed by alkali. The scrubber 2 1 6 is cooled and oiled by the condenser 3 7 c to form an oil equivalent to A heavy oil. This oil is recovered in the oil storage tank 2 1 5 through a pipe 2 1 4. A blower 2 2 1 is connected to the decomposition tank 2 10 in the third stage, whereby a reverse thermal gradient state of heated air from the top of the decomposition tank is formed and circulated. In addition, the residue is recovered through the sludge pipe 2 19 in the sludge tank 2 2 0 which has been filled with water. The decomposition gas that has not been decomposed in the above-mentioned third stage 2 1 0-25 25 312 / Invention Specification (Supplement) / 92-〇4 / 921016〇6 200302867 Condenser 3 7 c will be sucked up by the pump P Then, it is recovered in the oil storage tank 2 1 5 through a pipe 2 1 4. The decomposed gas that has undergone the secondary decomposition in the first and second decomposing cylinders 47 and 48 is extracted from the upper end and oiled. At this time, the gas that has not been completely decomposed will use the superheater 1 5 1,1 5 2 and decomposed. Decomposition cylinders such as light oil, kerosene, and some heavy oil components will be obtained in the second stage decomposition cylinder, and the remaining components equivalent to A heavy oil will be decomposed by the third stage decomposition cylinder. In addition, you can set the decomposition tube to four or more stages. Further, in the embodiment shown in Fig. 12, the melting section 200 is of a forming type (vertical type). β 卩, the first, second, and third melting tubes 201, 202, and 203 are connected in a vertical direction through the connecting portions 204, 2 05, respectively, and the plastic sent from the funnel 4 1 is in the first melting tube. It was moved to the right in 20 1 and to the left in the second melting tube 202 and to the right in the third melting tube. Then it was supplied to the lower end of the first dissolving tube 4 7. The lead screw 2 07 of the third melting tube 203 in the lowermost stage is rotated by a motor 2 0 8. The rotation system of this motor 2 08 uses a chain 2 0 9 to make the lead screw 2 0 1 of the first melting tube 2 0 6 When rotating, the rotation of the lead screw 206 passes through the gears G 1 and G 2 to rotate the lead screw 2 2 1 of the second melting cylinder 2 0 2. The hot air system uses the blower 2 1 3 and the temperature is lower from the melting part 2000. The upper side is drawn out, and then sent to the lower side through the pipe 2 2 2 and circulated upward in the melting section. In the embodiment shown in FIG. 21, the first to fourth melting cylinders 3 1 a, 3 1 b,..., 3 1 d are heated by a heating medium supplied from a heating medium heating device 600. Here, the heat medium refers to a liquid heat medium, and various heat medium oils are used, for example. This heat 26 312 / Invention specification (Supplement) / 92-04 / 92101606 200302867 The medium is heated to a predetermined temperature by a heating medium heating device 6 0 0 and supplied to the heating medium space of the melting tube 3 1 through the heating medium pipe 60 1 1 3 5 The heat medium space 1 3 5 ′ is formed between the inner tube 1 3 1 and the outer box 1 3 6 like the hot air space 1 3 5 described above. Therefore, the heat medium is circulated in the heat medium space 1 3 5 'by flowing from the downstream side to the upstream side with the circulation pump 602. Correlation is controlled at 1 90 ~ 2 00 ° C in the first melting tube 3 1 a, 210 ~ 2 3 0 ° C in the 3 lb of the second melting tube, and 2 3 0 in the 3rd melting tube 31c. In the case where the temperature is controlled to ∼2 60 ° C and the temperature is controlled within the range of 300 to 340 ° C in the fourth melting cylinder 31d, the above-mentioned respective controls are the same as those in the case of heating by hot air. In this case, by changing the hot air and using a heat medium, the following effects can be achieved: a) the heat transfer efficiency can be greatly improved; b) compared with the hot air, because the heat medium is less likely to cool, so even when the equipment is stopped, The temperature in the melting cylinder 31 is also less likely to drop. 'When the equipment is started, it can be started in a short time, and c) Even if the inner cylinder 1 31 of the melting cylinder 3 1 is damaged, it can still prevent the brewing. Fire accident. In addition, because the operating temperature of the general heating medium is below 350 ° C, although only the heating cylinder 3 1 is used as the heating medium, the heating of the decomposition cylinders 47 and 48 can also be performed by selecting an appropriate heating medium. Use heat medium. In addition, according to the operating temperature of the heat medium used, the melting tube 31 (for example, the first, second, and third melting tubes 31a, 31b, and 31c) in the melting tube 31 which is controlled only at a low temperature may use heat. The medium is heated. In the embodiment shown in FIG. 13, the fourth melting tube 3 d and the lower half of the disassembling tube 47 are connected by the connecting portion 5000, and the molten portion is melted through the connecting portion 500. The blister-like plastic is supplied to the lower end of the inner tube 2 3 5 in the first step decomposition tube 47 312 / Instruction Manual (Supplement) / 92-04 / 92101606 200302867. In addition, for the plant or animal edible oils stored in the supply section of the aforementioned connection section or after use, the mixture of these oils and blistering plastics can be decomposed once or twice by each branch. Thereby, the reformed oil) decomposition reaction can be recovered. Generally, as shown in Figure 14, plastics such as polyethylene, polypropylene, poly ABS resin, and acrylic resin are thermally decomposed and collected as oil, and the rest are used as exhaust gas (7-8%) The gas processing unit 34 performs processing, and carbides (2 to 3%) are collected as residues in the residue tank 40. Polyvinyl chloride uses lime to neutralize 58% of calcium chloride, and about 42% of it will be thermally decomposed, and the oiled part will be about 30%. In addition, the Japanese patent application filed on January 25, 2002, including the scope, drawings, and abstract of the patent application (No. No. 2002-017650), and the patent application (No. All the disclosures in 2002-3 0 1 8 95) are combined in this specification in their entirety. The present invention is not limited to the embodiments described above. The above description is only an example. For example, it has substantially the same structure as the technical idea in the patent application scope of the present invention, and achieves the same function and effect. It is included in the technical scope of the present invention. [Industrial Applicability] As mentioned above, the plastic oiling method and oiling equipment 312 / Invention Specification (Supplement) / 92-04 / 92101606 of the present invention are unwound and used to dispose of waste oil such as 5 0 2 Chemical styrene and 90% were collected and used as waste]], and some of the applicants who have been applied for collection instructions and applications, are described in the description of the implementation, are 28, 28 200302867 It is a plastic oiling method and oiling equipment that can be effectively used for oil recovery from waste plastic. [Brief description of the drawings] FIG. 1 is a structural diagram of the basic principle of the present invention. FIG. 2 is a configuration diagram of an embodiment according to the basic principle of the present invention. FIG. 3 is a schematic perspective view of a petrochemical equipment according to an embodiment of the present invention. FIG. 4 is a front view of a petrochemical equipment according to an embodiment of the present invention. FIG. 5 is a plan view of an oiling apparatus according to an embodiment of the present invention. FIG. 6 is a diagram illustrating a schematic structure of FIG. 5. FIG. 7 is an explanatory diagram of a schematic structure of FIG. 4. Fig. 8 is a cross-sectional view of a melting tube. Fig. 9 is a cross-sectional view of an exploded tube. FIG. 10 is a structural diagram of a dechlorination treatment unit. Fig. 11 is a configuration diagram of an exhaust gas treatment unit. FIG. 12 is a diagram illustrating a schematic structure of another embodiment. FIG. 13 is a structural diagram of an interface between a melting section and a disassembling section. Figure 14 is a graph of the recovery rate for the treated plastic. Fig. 15 is an explanatory view of the pulled-up state of the foamed plastic. Figure 16 is a cross-sectional view of the funnel. FIG. 17 is a schematic perspective view of a non-heating portion. Figure 18 is a structural diagram of a sludge tank. Fig. 19 is a structural diagram of a telescopic cylinder. FIG. 20 is a schematic structural diagram of an accident prevention system and a deodorizing system. FIG. 21 is a schematic structural diagram of another embodiment. 312 / Invention Manual (Supplement) / 92-04 / 92101606 29 200302867 (Description of component symbols) 1 Storage section 2 Inner tube 3 Hot air space 4 Hot air space 5 Outer box 6 Outer tube 7 Lead screw 8 Spiral blade 9 Piping 10 Piping 12 Motor 13 Disassembly tube 14 Rotary shaft 14a Shaft front end 15 Piping 17 Outer tube 20 Inner tube 2 1 Outer tube 22 Piping 24 Lead screw 25 Inner tube 26a Piping 26b Piping 312 / Invention Manual (Supplement) / 92-04 / 92101606
30 200302867 26c 配 27 分 28 供 29 儲 30 油 3 1 融 3 1a 第 31b 第 3 1c 第 3 1 d 第 32 分 33 脫 34 廢 35 第 36 第 37a,37b,37c 38a 儲 38b 儲 39a 第 39b 第 39c 第 40 污 4 0a 污 40b 水 管 解筒 應筒 存部 化設備 解部 1融解筒 2融解筒 3融解筒 4融解筒 解部 氯處理部 氣處理部 1熱風產生爐 2熱風產生爐 冷凝器 油槽 油槽 1分離器 2分離器 3分離器 泥槽 泥管30 200302867 26c with 27 points 28 for 29 storage 30 oil 3 1 melting 3 1a section 31b section 3 1c section 3 1 d section 32 points 33 off 34 waste 35 section 36 section 37a, 37b, 37c 38a store 38b store 39a section 39b section 39c No. 40 Pollution 4 0a Pollution 40b Water tube dissolving tube should be stored in storage unit dissolving unit 1 dissolving tube 2 dissolving tube 3 dissolving tube 4 dissolving tube dissolving section chlorine treatment section gas treatment section 1 hot air generator 2 hot air generator condenser oil tank Oil tank 1 separator 2 separator 3 separator mud tank mud pipe
312/發明說明書(補件)/92-04/92101606 31 200302867 4 0c 金 屬 網 40d 蓋 體 40e 開 □ 40f 非 活 性 氣 體 40g 氣 體 局 壓 瓶 4 1 漏 斗 42 馬 達 43 儲 油 槽 46 配 管 47 第 1 段 分 解筒 47a,47b 單 位 分 解 筒 48 第 2 段 分 解筒 48a,48b 單 位 分 解 筒 49 配 管 49a 閥 50 配 管 51,52 馬 達 53,54 馬 達 55 馬 達 5 6,5 7,5 8, 60 鼓風機 59 煙 囪 59a,59b 分 管 5 9c 排 放 □ 60 洗 滌 312/發明說明書(補件)/92-(M/92101606312 / Invention Manual (Supplement) / 92-04 / 92101606 31 200302867 4 0c Metal mesh 40d Cover 40e Open 40f Inert gas 40g Gas pressure bottle 4 1 Funnel 42 Motor 43 Oil storage tank 46 Piping 47 First stage disassembly Tubes 47a, 47b Unit disintegration tube 48 Second stage disassembly tube 48a, 48b Unit disassembly tube 49 Pipe 49a Valve 50 Pipe 51, 52 Motor 53, 54 Motor 55 Motor 5 6,5 7,5 8, 60 Blower 59 Chimney 59a, 59b Manifold 5 9c Discharge □ 60 Washing 312 / Invention Manual (Supplement) / 92- (M / 92101606
32 200302867 61 洗滌器 70 配管 71,71a,71b 配管 75,76,77 配管 78 配管 8 1 配管 83 消石灰槽 86 配管 100 收集排氣管 101,102 配管 120 落下筒 13 1 內筒 132 螺旋葉片 133 旋轉軸 134 吸熱葉片 135 熱風空間 135' 熱媒空間 136 外箱 137 導螺桿 148 內筒 149 導螺桿 150 導螺桿 15 1 過熱器 170,171 鼓風機 33 312/發明說明書(補件)/92-04/92101606 200302867 200 融 20 1 〜203 第 204,205 銜 206 導 207 導 208 馬 209 鏈 2 10 第 2 13 鼓 2 14 配 2 15 儲 2 16 洗 218 落 2 19 污 220 污 22 1 導 222 配 234 燃 235 入 236 殼 237 出 238 陶 25 1 旋 252 螺 解部 1〜第3融解筒 接部 螺桿 螺桿 達 3段分解筒 風機 管 油槽 滌器 下筒 泥管 泥槽 螺桿 管 燒器 □ 體 □ 瓷角柱 轉軸 旋葉片32 200302867 61 Scrubber 70 Piping 71, 71a, 71b Piping 75, 76, 77 Piping 78 Piping 8 1 Piping 83 Lime tank 86 Piping 100 Collection exhaust pipe 101, 102 Piping 120 Drop tube 13 1 Inner tube 132 Spiral blade 133 Rotary shaft 134 Heat-absorbing blade 135 Hot air space 135 'Heat medium space 136 Outer box 137 Lead screw 148 Inner tube 149 Lead screw 150 Lead screw 15 1 Superheater 170,171 Blower 33 312 / Invention Manual (Supplement) / 92-04 / 92101606 200302867 200 Melt 20 1 ~ 203 No. 204,205 No. 206 No. 207 No. 208 No. 208 Horse 209 Chain 2 10 No. 2 13 Drum 2 14 Match 2 15 Storage 2 16 Wash 218 Drop 2 19 Sew 220 Sew 22 1 Guide 222 Match 234 Burn 235 Into 236 Shell 237 Out 238 Pottery 25 1 Rotary 252 Screwing part 1 ~ 3 melting tube joint part screw screw up to 3 stages decomposition tube fan tube oil tank scrubber lower tube mud tube mud tank screw tube burner □ body □ porcelain angle column rotating shaft rotary blade
312/發明說明書(補件)/92-04/92101606 34 200302867 253 吸熱風扇 254 熱空間 255 內筒 256 隔板 300 反應器 301 冷卻盤管 303 導螺桿 304 馬達 305 加熱筒 306 攪拌棒 308 葉片 309 導螺桿 3 10 馬達 3 12 氯化鈣槽 3 13 加熱筒 3 14 真空泵 3 15 放洩閥 3 17 鹼洗淨用洗滌器 410 非加熱部 4 11 殼體 4 12 Tifir Η®! 盍體 4 1 3 馬達 414 導螺桿 4 14a 旋轉軸 312/發明說明書(補件)/92-04/92101606312 / Invention Manual (Supplement) / 92-04 / 92101606 34 200302867 253 Heat absorption fan 254 Hot space 255 Inner tube 256 Partition 300 Reactor 301 Cooling coil 303 Lead screw 304 Motor 305 Heating tube 306 Stir rod 308 Blade 309 Guide Screw 3 10 Motor 3 12 Calcium Chloride Tank 3 13 Heating Cartridge 3 14 Vacuum Pump 3 15 Drain Valve 3 17 Washer for Alkaline Washing 410 Non-Heating Section 4 11 Housing 4 12 Tifir Η®! Carcass 4 1 3 Motor 414 Lead screw 4 14a Rotary shaft 312 / Invention manual (Supplement) / 92-04 / 92101606
35 200302867 4 14b 螺旋葉片 500 銜接部 502 槽 5 11 控制器 5 12 二氧化碳高壓 5 13 閥 514 吸取裝置 5 14a 吸取風扇 5 15 粉碎機 516 乾燥機 5 16a 風扇 517 旋風器 600 熱媒加熱裝置 601 熱媒配管 602 循環泵 700 伸縮筒 701 蛇腹管部 702 滑動部 703 蛇腹管 704 蛇腹管內筒 704a,706a 楔形部 705 支撐筒 706 內筒 A 塑膠囤積場 312/發明說明書(補件)/92-04/9210160635 200302867 4 14b Spiral blade 500 Adapter 502 Slot 5 11 Controller 5 12 High pressure carbon dioxide 5 13 Valve 514 Suction device 5 14a Suction fan 5 15 Crusher 516 Dryer 5 16a Fan 517 Cyclone 600 Heat medium heating device 601 Heat medium Piping 602 Circulation pump 700 Telescopic tube 701 Corrugated tube portion 702 Sliding portion 703 Corrugated tube 704 Corrugated tube inner tube 704a, 706a Wedge-shaped portion 705 Support tube 706 Inner tube A Plastic hoarding yard 312 / Instruction manual (Supplement) / 92-04 / 92101606
36 200302867 CT 冷 卻 塔 f 泡 沬 狀 塑 膠 G1 ,G2 齒 輪 mp 融 解 塑 膠 P 塑 膠 碎 片 Q 熱 風 循 環 路 S 溫 度 偵 測 計 SI，S2，S3 溫 度 偵 測 計 ST1，ST2 供 給 油 槽 312/發明說明書(補件)/92-04/9210160636 200302867 CT Cooling tower f Foam-like plastic G1, G2 Gear mp Melt plastic P Plastic fragments Q Hot air circulation path S Temperature detector SI, S2, S3 Temperature detector ST1, ST2 Supply oil tank 312 / Invention manual (Supplements) ) / 92-04 / 92101606