200304535 (1) 玖、發明說明 【發明所屬之技術領域】 本發明係關於一種改良燃燒工廠（尤其是將廢棄物轉 換成能源之工廠）產生之燃燒殘留物性質的方法，其中燃 料在一燃燒栅上燃燒，且在適當燃料控制下升高所產生的 燃燒殘留物溫度。 本發明亦關於一種燃燒工廠（尤其是廢棄物煅燒單位 )產生之殘留物的處理方法，其中燃料在一燃燒柵上燃燒 ，且所產生的燃燒殘留物在一濕式排放器中猝息，之後從 排放器送到外面。 另外，本發明亦關於一種燃燒工廠（尤其是將廢棄物 轉換成能源之工廠）產生之殘留物的處理方法，其中燃料 在一燃燒柵上燃燒，且在適當燃料控制下升高所產生的燃 燒殘留物溫度。 【先前技術】 在此種方法中，如歐洲專利EP 0 667 490 B1中所揭示 ，燃料在燃燒柵上加熱到燃燒產生的底灰溫度在燃燒柵外 面的熔化階段之前恰低於底灰熔點，此方法調節燃燒的方 式使得柵端部溫度儘可能高，以將下游熔化階段所需能量 保持儘可能地低。然而，在此點底灰不產生燒結或熔化， 但爲了達到所需底灰品質，需要下游熔化階段，此下游熔 化階段不僅需要相關設備，也需要增加能量源，即使下游 熔化階段有前述加熱作業。 - 8 - (2) (2)200304535 廢棄物的無機及有機汚染物成分對於所需底灰品質很 重要，進一步言之，重金屬及塩爲主要無機汚染物成分， 而無機汚染物則特別是因燃燒不完全而產生。另外，底灰 品質之評估主要是有多少汚染物在洗淨試驗期間被浸析出 來。另外，底灰機械性質對於評估是否適用於建築工程諸 如掩埋式垃圾處理場、土工、及舖路者很重要。 由於涉及燃燒殘留物處理之高溫在熔化階段，熔融燃 燒殘留物特徵在於有機化合物百分比低，將廢棄物轉換成 能源之工廠之典型底灰型式含有1〜5 %重量的未燃燒物 ，一般是判定爲燒蝕量，熔融燃燒殘留物燒蝕量重量低於 0.3 %。熔融燃燒殘留物另一特徵在於可出塩及重金屬百 分比低，因它們在熔融塊冷却時不是蒸發就是倂入所形成 的玻璃基體中。 另一方面，德國專利案DE 701 606 C中 揭示了一種技術，其中燃燒殘留物送到具有一入口段和有 一上升出口槽的一排放缸之排放器，並從該處以一排放柱 塞排到外面，這些燃燒殘留物稱爲底灰，將底灰猝息之水 供至排放缸，只需要足夠的新水導入缸內來抵消隨著濕底 灰排出之水量。黏附在殘留物上的許多物質和化合物（諸 如塩）的穩態濃度讓它本身內的這些濃度無法降低，造成 底灰在適用掩埋式垃圾處理場及再利用成爲建築材料方面 的品質無法令人滿意，此一缺點之原因是殘留物未分離（ 分類）成較佳品質分量和較佳品質分量’結果’無可避免 地整體燃燒殘留物品質無法令人滿意。 -9- (3) (3)200304535 德國專利案D E 4 4 2 3 9 2 7中也揭示了一 種技術，其中從爐來之殘留物直接輸送到水浴以在無先前 猝息之下進行粗洗，粗洗後的乾底灰分成至少二分量，小 於2 mm的所有粒子分配爲第一分量，而其他粒子分配爲第 二分量，此法繼續將第二分量以篩選步驟分成至少二分量 ，小於2 7〜3 5 mm的所有分配爲第三分量，剩下的粒子 分配爲第四分量，以此方式產生品質令人滿意的殘留物分 量，但是此法之缺點是大量灰塵飛揚和從爐進入的空氣造 成問題。 【發明內容】 本發明之產生係著眼於上述習用技術的各種問題。 本發明第一組發明目的在於提供一種方法，其中燃燒 程序可調節以得到具有所要品質之全燒結底灰而不需下游 融化或玻璃化單元。 本發明第二組發明目的也在於提供一種方法，其中分 離出好品質底灰分量，避免灰塵飛揚缺點以及從爐進入空 氣造成的問題，也減少水之進一步浪費。 另外，本發明第三組發明目的在於提供一種方法，其 中燃燒程序可調節以得到具有所要品質之全燒結底灰而不 需下游融化或玻璃化單元，在使用最少設備下避免灰麈飛 揚缺點以及從爐進入空氣造成的問題，也減少水之進一步 浪費。 接著將以所附圖式所示較佳實施例說明本發艮之改善 -10- (4) (4)200304535 燃燒工廠產生的燃燒殘留物品質之方法以及處理殘留物之 方法。 【實施方式】 第一組發明：改善燃燒工廠產生的燃燒殘留物性質之方法 第一組發明目的之達成係藉由運作一燃燒控制系統之 方式使得燃燒殘留物在主燃燒區燃料床上事先燒結及/或 熔入底灰內，而且尙未熔化或燒結的燃燒殘留物在燃燒程 序結束時排放，之後再一次回到燃燒程序。 第一組發明槪念第一係基於在柵上實施燃燒程序之方 式使得在主燃燒區燃料床上事先發生燒結或熔化，第二則 是將尙未燒結或熔化的燃燒殘留物回送，使得可在第二或 第三次嘗試下達到所需燒結或熔化的程度。 在第一組發明中，“完全燒結底灰”一詞係指由典型 上粒徑至少有例如8 inm之燒結及/或熔化塊體所組成之材 料，這些塊體由經過完全或表面熔化之後凝固的垃圾燃燒 殘留物所組成。 燒結及/或熔化塊體最好爲多孔構造，因在燒結熔化 期間釋出氣體，全燒結底灰可能之孔率歸因於燃料床上的 熔融底灰溫度不夠高而無法得到適當低孔率，且氣泡被類 似公知玻璃製造之氣泡移除程序驅出之後仍留下孔。全燒 結底灰與使用襯有耐火材料的坩堝式電爐或其他熔化單元 之下游高溫處理法得到的典型玻璃化底灰有所不同。 通過柵但最後未受影響之諸如玻璃或金屬的垃圾組成 -11 - (5) (5)200304535 物嚴格而言係在燃料床上既未熔化也未燒結者，然而，全 燒結底灰可包含這些玻璃或金屬，這些組成物有燒完和可 析出污染物適當性質。 “燒結”一言司依據 Hammerli ( Miill and Abfall 31， 底灰及其他殘留物棄置補充篇，第1 4 2頁，1 9 9 4年 出版）係指“熔化和固體化之特殊狀況”，因此下文中“ 燒結”所指“表面熔化或粒子一起熔化”意義往往超出其 一般科學上之用法。全燒結底灰燒結所產生的塊體可完全 或部分熔化。 未燒結及/或熔化的底灰組成物定義爲殘留底灰，與 全燒結底灰相比，殘留底灰特性爲粒徑小，燒蝕量高，而 且可析出污染物比率高。 第一組發明著眼於已然之殘留物的燒結及/或熔化以 及迄今尙未視爲可能之主燃燒區的燃料床。實際上，若液 態底灰在個別柵桿或柵的其他可動元件之間，對於機械燃 燒柵非常有害，爲此之故要避免底灰在柵上熔化，且要小 心處理使得在燃料床不會到達底灰之熔點。 藉由第一組發明，燒結及/或熔化程在上燃料床發生 ’其理由是最大熱衝擊從上方經由火焰體輻射發生，且直 接置於柵上的材料可藉由加入較冷（相對而言）的下部燃 燒空氣而保持在比從燃料床頂部相比是較低之溫度。由於 當以此方式調節燃燒時並非所有的燃燒殘留物能轉換成具 適當品質之全燒結底灰，未具全燒結性質的燃燒殘留物回 到燃燒程序。 -12- (6) (6)200304535 在燃料床上完成燒結及/或熔化程序不需額外外部能 源，所得到的底灰品質很像習於此技者熟悉之從已知下游 熔化及玻璃化高溫程序所得產品，使用的單元有諸如廻轉 審、坩堝式電爐、以及熔化室。然而這些習知方法的一項 主要缺點爲需要很複雜的額外單元，且所消耗的能源高。 第一組發明解決此問題，且能產生品質與習知方法得到的 底灰幾乎相同之底灰。 依據第一組發明的燃燒控制系統一顯著有利實施例， 下部燃燒空氣依要燃燒的廢棄物品質（垃圾品質）加入氧 氣，使得氧氣體積含量約2 5〜4 0%，最佳爲2 5〜 3 0 %，而且，依據另一有利實施例，下部燃燒空氣預熱 到約1 0 0〜4 0 0 °C，這些措施可單獨或一起使用，視 狀況而定。爲燃料特性函數之燃料床（一般爲垃圾層）溫 度最好設定在1 0 00〜1 40 0 °C。 達成所需狀況的所有燃燒控制措施以將燃燒殘留物轉 換成燒結及/或熔融底灰者係經選擇使得出現一特定比例 之全燒結底灰（例如重量佔整個燃燒殘留物量的2 5〜7 5 % )，依此方式確保主燃燒區燃料床上有足夠的未熔化 材料環繞熔化的灰，使得此措施不會對機械柵零件有不利 影響。 在本發明另一有利實施例中，飄塵回到燃燒程序，飄 塵與燃燒氣體一起離開燃料床，且經由鍋爐被導入下游烟 道氣體過濾器。 不完全及完全燒結底灰從燃燒系統排出後在一底灰篩 -13- (7) (7)200304535 選階段分開（通過粒徑例如2〜1 0 mm的篩子），超大尺 寸者爲完全燒結底灰，而過小尺寸者爲要回送之分量。習 於此技者知道有許多機械分離法來進行此分離程序。 分離可藉由篩選或結合篩選和洗滌步驟，如本發明其 他有利實施例所述。 當然也有在燃燒廠外進行底灰品質改進的其他措施， 尤其是具有以及沒有化學添加劑之特殊洗滌步驟。 粒徑由小於2〜1 0 mm的細分量回到燃燒程序，此可 藉由將細分量加入到要進給的燃料中或藉由將它直接進給 到燃料床而完成，爲了避免增加灰塵且爲了易於處理，細 分量在回送之前適當地粒化及塊化。 第二組發明：處理燃燒工廠產生的燃燒殘留物之方法 第二組發明係藉由以下述二個不同程序爲基礎之技術 特徵來達成。 第一程序係由一步驟組成，其中從一濕式排放器來的 燃燒殘留物機械地分成二分量，主分量主要由一粗分量和 超大尺寸分量組成，主分量以從濕式排放器來之水洗滌， 由是將黏在燃燒殘留物上的較細部分分離，而洗滌水與在 洗滌步驟中溶解的較細部分一起被帶到濕式排放器。 若是源自濕式排放器之水依此方式循環，可從較細部 分放出品質良好的主分量而不需大量的新水，不然它會黏 在燃燒殘留物，而這會對主分量品質有不利影響。結果， 較細部分已被洗滌的燃燒殘留物有良好品質，且可有效地 再利用例如做爲建築材料之底灰。 -14- (8) (8)200304535 第二程序係由一步驟組成，其中從一濕式排放器來的 燃燒殘留物機械地分成二分量，主分量主要由一粗分量和 超大尺寸分量組成，主分量先碾碎’再以從濕式排放器抽 來之水洗滌，由是將黏在碾碎燃燒殘留物上的較細部分分 離，而洗滌水與在洗條步驟中溶解的較細部分一起被帶到 濕式排放器。 第二程序優點爲在洗滌前放出包含在主分量中的污染 物，如此，所包含的污染物在洗條步驟中移除。另一優點 爲碾碎材料表面積較大，對於從主分量得到的材料多孔形 態非常重要。第二程序係用於需要品質很高的燃燒殘留物 或是主分量有很多污染物或燃燒殘留物孔度很重要之時， 第二程序亦用於底灰主分量在後續處理步驟中進一步碾碎 之場合，例如底灰主分量（最終產品）必須在浸析測試中 碾碎以便決定其品質時，使用第二程序較佳。碾碎及洗條 後的主分量不能與細分量混合，在多數場合中，由於主分 量已熔化或燒結，未燃燒或可浸析污染物含量低’使得這 些品質不會因碾碎而改變，因此，依據第二程序碾碎的主 分量與含有大量上述污染物之底灰細分量相比有很大不同 之品質。 依據第二組發明一實施例，在機械分離期間產生的最 細分量和細分量輸送（循環）到燃燒程序’這些分量再次 受到燃燒程序，因而使其能熔化和燒結。 藉由這些措施，先前第一種習用技術程序之缺點（所 有燃燒殘留物未再利用，即使含有少量較佳差品質殘留物 -15- (9) (9)200304535 )得以避免。與第二種習用技術相比’灰塵飄揚以及爐子 密封之問題得以避免。另外，藉由回送較差品質的最細分 量和細分量，更增加可回收的燃燒殘留物，因爲回送的細 部分有機會凝固成具有所需品質之燃燒殘留物，不管是第 一次回送或是重複回送之時。第二種習用方法並未有此優 點，因爲沒有回送到燃燒程序。 依據第二組發明的第一或第二程序之另一實施例，以 從濕式排放器來之水預洗之主分量新水淸洗’而攜有相當 大量污染物之排放水被洗出，造成燃燒殘留物及/或燒結 底灰品質更進一步提升。由於以新水淸洗粗分量，其優點 是從淸洗得到之水有一特定百分比可送到烟道氣體淸理系 統而不必預先淸理，因爲其所含有的污染物百分比相當低 。另外，本實施例提供一項優點，即從淸洗得到之水有一 特定百分比可供給濕式排放器，排放器中之水位可如此保 持，由於水持續地隨著排出的燃燒殘留物帶出，排放器中 之水位下降，因於從淸洗得到之水中的鈣和硫酸塩量可忽 略，管子和噴嘴不會阻塞。 依據第二組發明的第二程序，即使在第一分離步驟之 後主分量含有高百分比之超大尺寸分量（一般含有大量碎 金屬），超大尺寸粗分量在依據本發明又一實施例中的一 機械步驟做進一步的分離，金屬以一磁性分離器分離。 在第二組發明的一實施例中，其中一例爲粒徑加以區 別使得小於2 mm者爲最細分量，不小於2隨且小於8 mm者 爲細分量，而不小於8丨mn且小於3 2 nun者爲粗分量，而不 (10) (10)200304535 小於3 2画者爲超大尺寸。這些値提供做爲更了解本發明 之導引，明顯地，含有較細分量一定百分比之各分量附屬 於本身，只要此百分比可忽略。 一般而言，具粒徑小於約8 mm之細分量（直接從排放 器來者）較佳應回送到燃燒程序，因其品質不佳。在第二 程序中，產生了具粒徑與細分量者可相比之碾碎主分量， 碾碎主分量有較佳品質而能做爲建築材料。 舉例言之，在第二程序中，若第一粗分離步驟以3 2 mm爲截止點，亦即若是超大尺寸分量被分離，則建議提供 以例如8 imn爲截止點之第二機械步驟，使小於8 mm的所有 部分回到燃燒程序。 爲了得到儘可能多的可再利用分量，依據第二組發明 的又一實施例，合乎邏輯者爲從主分量分離出來的粗分量 與超大尺寸分量減小尺寸步驟（例如以碾碎機、碎岩機等 等）所產生的碾碎燃燒殘留物混合，此時建議使第一混合 分量受到機械分離，以將有不想要的粒徑粒子移除，因爲 在減小尺寸期間產生粒徑不合進一步再利用且要回到例如 燃燒程序者。 若是要製備燃燒殘留物以用於舖路製造基礎應用之特 別有興趣領域，材料必須是可壓實者，沒有細分量子（粒 徑例如不小於2 imn且小於8 mm，如上所述）的話是不可能 的。爲此之故，建議粗分量一部分必須有一尺寸減小步驟 以慎重地確保此必需之細分量之出現。由是，此粒徑發生 比率之機會充分不太可能。有利的是重量約3 0 %的粗分 -17- (11) (11)200304535 量接受此尺寸減小步驟，所形成的細分量和最細分量與粗 分量混合以形成一第二混合分量，最好用於舖路的混合分 量70%重量由粗分量形成。 在第二混合分量中，大多數的粒徑大於8腿，經驗顯 不這些成分有再利用所需品質，然而，粒徑不小於2醒且 小於8醒者佔一低比率有其必要，以確保上述舖路用之殘 留物之可壓實性。 依據第二組發明之再一實施例，第二混合分量以從濕 式排放器來之水洗滌，且第一混合分量分離，此時，粒徑 2 imn以下之部分（往往帶有特別嚴重污染物負擔）可確定 地從可回收殘留物分離。 此洗滌水可有利地送到濕式排放器，如前文所述，藉 由以此方式將水回送，新水之消耗可儘可能地低。 在此建議分離的金屬以從排放器來之水進行洗滌步驟 ，使黏附的任何燃燒殘留物得以洗掉，有利的是使用一篩 選步驟來機械地將分量分離。 添加可溶解重金屬沉澱劑到排放器水中對於改善回收 的燃燒殘留物品質相當有幫助，結果這些重金屬可藉由添 加沉澱劑而分離。 第三組發明：處理燃燒工廠產生的燃燒殘留物之方法 上述目的之達成係藉由基於二不同方法的下述第三組 發明之方法。 依據本發明，這些方法第一個係運轉燃燒控制系統之 方式使得燃燒殘留物在主燃燒區燃燒床上事先燒結及/或 -18- (12) (12)200304535 熔化到底灰中，在一濕式排放器內猝息所產生的燃燒殘留 物全部以及接著將之取出排放器，以一機械分離步驟將濕 式排放器來之濕燃燒殘留物先分離成二分量，接著以從濕 式排放器抽來之水洗滌主要由粗分量和超大尺寸分量組成 的主分量，因而將黏在燃燒殘留物上的較細部分分離，以 及將洗滌水和在洗滌步驟中溶解的較細部分輸送到濕式排 放器。 當假定可再利用主分量包含比率可忽略的可洗掉的污 染物（例如塩或重金屬）時，第一種方法有效。 第三組發明主要有二個技術特徵，第一個是包括一燃 燒控制系統，第二個是燃燒程序產生的殘留物之機械處理 ，其中第二個技術特徵包括取決於燃料成分之二個不同方 法。 包含在第一個技術特徵的燃燒控制系統在殘留物機械 處理方面對以下二方法而言是共用的，而且是依據柵上的 燃燒程序，其實施方式使燒結或熔化發生在主燃燒區的柵 上，而且依據尙未燒結或熔融的燃燒殘留物回送，使得可 在第二或第三次嘗試下達到所需燒結及/或熔化程度。 “全燒結底灰”一詞係指由典型上粒徑例如至少8 mm 的燒結及/或熔融塊所組成之材料，這些塊體由經過完全 或表面熔化之後凝固的垃圾燃燒殘留物所組成。 燒結及/或熔化塊體最好爲多孔構造，因在燒結熔化 期間釋出氣體，全燒結底灰可能之孔率歸因於燃料床上的 熔融底灰溫度不夠高而無法得到適當低孔率，且氣泡被類 -19- (13) (13)200304535 似公知玻璃製造之氣泡移除程序驅出之後仍留下孔。全燒 結底灰與使用襯有耐火材料的坩堝式電爐或其他熔化單元 之下游高溫處理法得到的典型玻璃化底灰有所不同。 通過柵但最後未受影響之諸如玻璃或金屬的垃圾組成 物嚴格而言係在燃料床上既未熔化也未燒結者，然而，全 燒結底灰可包含這些玻璃或金屬，這些組成物有燒完和可 析出污染物適當性質。 “燒結”一詞依據字義（見上述Hammerli )係指“ 熔化和固體化之特殊狀況”，因此下文中“燒結”所指“ 表面熔化或粒子一起熔化”意義往往超出其一般科學上之 用法。全燒結底灰燒結所產生的塊體可完全或部分熔化。 未燒結及/或熔化的底灰組成物定義爲殘留底灰，與 全燒結底灰相比，殘留底灰特性爲粒徑小，燒蝕量高，而 且可析出污染物比率高。 本發明著眼於已然之殘留物的燒結及/或熔化以及迄 今尙未視爲可能之主燃燒區的燃料床。實際上，若液態底 灰在個別柵桿或柵的其他可動元件之間，對於機械燃燒柵 非常有害，爲此之故要避免底灰在柵上熔化，且要小心處 理使得在燃料床不會到達底灰之熔點。 藉由第三組發明，燒結及/或熔化程在上燃料床發生 ，其理由是最大熱衝擊從上方經由火焰體輻射發生，且直 接置於柵上的材料可藉由加入較冷（相對而言）的下部燃 燒空氣而保持在比從燃料床頂部相比是較低之溫度。由於 當以此方式調節燃燒時並非所有的燃燒殘留物能轉換成具 -20- (14) (14)200304535 適當品質之全燒結底灰，未具全燒結性質的燃燒殘留物回 到燃燒程序。 在燃料床上完成燒結及/或熔化程序不需額外外部能 源，所得到的底灰品質很像習於此技者熟悉之從已知下游 熔化及玻璃化高溫程序所得產品，使用的單元有諸如廻轉 蜜、坩堝式電爐、以及熔化室。然而這些習知方法的一項 主要缺點爲需要很複雜的額外單元，且所消耗的能源高。 第三組發明解決此問題，且能產生品質與習知方法得到的 底灰幾乎相同之底灰。 在上述與機械處理相關之第一個方法中，若是源自濕 式排放器之水循環，可從細部分放出品質良好的主分量而 不需大量的新水，不然它會黏在燃燒殘留物，而這會對主 分量品質有不利影響。結果，較細部分已被洗滌的燃燒殘 留物有良好品質，且可有效地做爲可再利用之底灰。 在適合處理包含可洗掉的大量污染物（例如塩或重金 屬）之燃燒殘留物之第二種方法中，其目的之達成係運轉 燃燒控制系統之方式使得燃燒殘留物在主燃燒區燃燒床上 事先燒結及/或熔化到底灰中，在一濕式排放器內猝息所 產生的燃燒殘留物全部以及接著將之取出排放器，以一機 械分離步驟將濕式排放器來之濕燃燒殘留物先分離成二分 量（主要由一粗分量和超大尺寸分量所組成之分離的主分 量，其受到一尺寸減小步驟，接著以從濕式排放器抽來之 水洗滌），以及將洗滌水和在洗滌步驟中溶解的較細部分 輸送到濕式排放器。主分量碾碎之結果是卡在燃燒殘留物 -21 - (15) (15)200304535 內的較大粒子可在後續洗滌步驟中被洗出，因而從可再利 用主分量分離，如此，高百分比殘留物可回收成爲可再使 用的底灰，不管有很多污染物含在殘留物，無需期待稍後 大幅洗出污染物。 在上述第二種方法中，包含在本發明第一個技術特徵 內的燃燒控制也在機械處理之前進行。 依據本發明的燃燒控制系統一顯著有利實施例，下部 燃燒空氣依要燃燒的廢棄物品質（垃圾品質）加入氧氣， 使得氧氣體積含量約2 5〜4 0%，最佳爲2 5〜3 0% ，而且，依據另一有利實施例，下部燃燒空氣預熱到約 1 0 0〜4 0 0 °C，這些措施可單獨或一起使用，視狀況 而定。爲燃料特性函數之燃料床（一般爲垃圾層）溫度最 好設定在1 0 0 0〜1 4 0 0 °C。 達成所需狀況的所有燃燒控制措施以將燃燒殘留物轉 換成燒結及/或熔融底灰者係經選擇使得出現一特定比例 之全燒結底灰（例如重量佔整個燃燒殘留物量的2 5〜 7 5%)，依此方式確保主燃燒區燃料床上有足夠的未熔 化材料環繞熔化的灰，使得此措施不會對機械柵零件有不 利影響。 在本發明另一有利實施例中，飄塵回到燃燒程序，飄 塵與燃燒氣體一起離開燃料床，且經由鍋爐被導入下游烟 道氣體過濾器。 第三組發明的第二個特徵（亦即包含二方法之燃燒殘 留物機械處理）之進行說明如下。 -22- (16) (16)200304535 依據第三組發明一實施例，機械分離期間產生的最細 分量和細分量被送到燃燒程序，這些分量再次受到燃燒程 序，因而能熔化和燒結。 藉由這些措施，先前第一種習用技術程序之缺點（所 有燃燒殘留物未再利用，即使含有少量較佳差品質殘留物 )得以避免。與第二種習用技術相比，灰塵飄揚以及爐子 密封（導入空氣）之問題得以避免。另外，藉由回送較差 品質的最細分量和細分量，更增加可回收的燃燒殘留物， 因爲回送的細部分有機會凝固成具有所需品質之燃燒殘留 物，不管是第一次回送或是重複回送之時。第二種習用方 法並未有此優點，因爲沒有回送到燃燒程序。 依據第三組發明的另一實施例，以從濕式排放器來之 水預洗之主分量新水淸洗，而攜有相當大量污染物之排放 水被洗出，造成燃燒殘留物及/或燒結底灰品質更進一步 提升。由於以新水淸洗粗分量，其優點是從淸洗得到之水 有一特定百分比可送到烟道氣體淸理系統而不必預先淸理 ，因爲其所含有的污染物百分比相當低。另外，本實施例 提供一項優點，即從淸洗得到之水有一特定百分比可供給 濕式排放器，排放器中之水位可如此保持，由於水持續地 隨著排出的燃燒殘留物帶出，排放器中之水位下降，因於 從淸洗得到之水中的鈣和硫酸塩量可忽略，管子和噴嘴不 會阻塞。 依據本發明的機械處理第二種方法中’即使在第一分 離步驟之後主分量含有高百分比之超大尺寸分量子（一般 -23- (17) (17)200304535 含有大量碎金屬），超大尺寸粗分量在依據本發明又一實 施例中的一機械步驟做進一步的分離，金屬以一磁性分離 器分離。 在第三組發明的一實施例中，其中一例爲粒徑加以區 別使得小於2 mm者爲最細分量，不小於2 mm且小於8 mm者 爲細分量，而不小於8 mm且小於3 2 mm者爲粗分量，而不 小於3 2 min者爲超大尺寸。這些値提供做爲更了解本發明 之導引，明顯地，含有較細分量一定百分比之各分量附屬 於本身，只要此百分比可忽略。直接從排放器而來且粒徑 不小於2麵且小於8匪之細分量爲燃燒殘留物最好回到燃 燒程序之部分。另一方面，包含在依據第二種方法的碾碎 程序結果所得到之底灰粒徑分布之細部分粒徑等於直接由 排放器供應之細分量粒徑，且此細部分品質較佳利於再利 用，因此碾碎底灰的細部分稱爲高品質細分量。 舉例言之，在第二種方法中，若第一粗分離步驟以 3 2 mm爲截止點，亦即若是超大尺寸分量被分離，則建議 提供以例如8 mm爲截止點之第二機械步驟，使小於8 mm的 所有部分回到燃燒程序。 在此建議將金屬從主分量分離，以防止機械分離設備 被大塊碎金屬損壞。 不僅是大塊碎金屬，其他金屬也從含有過小分量之主 分量（亦即粗分量小於3 2 mm )釋出，這些金屬部分可做 爲分開的再利用程序。 將金屬分別從超大尺寸分量和粗分量移除比較便利， -24- (18) (18)200304535 視意欲用於所產生的燃燒殘留物之再利用程序及型式而定 〇 若燃燒殘留物要用來例如舖路，則建議超大尺寸分量 在較不適於此目的之大於3 2醒的金屬部分已移除之後受 到進一步尺寸減小步驟。 在第二種方法中，爲了得到儘可能多的可再利用分量 ，依據第三組發明又一實施例，合乎邏輯者爲從主分量分 離出來的粗分量與超大尺寸分量減小尺寸步驟所產生的碾 碎燃燒殘留物混合以形成第一混合分量，此時建議使第一 混合分量受到機械分離，以將有不想要的粒徑粒子移除’ 因爲在減小尺寸期間產生粒徑不合進一步再利用且要回到 例如燃燒程序者。 若是要製備燃燒殘留物以用於舖路製造基礎應用之特 別有興趣領域，材料必須是可壓實者，沒有細分量子（粒 徑例如不小於2 mm且小於8皿1，如上所述）的話是不可能 的。爲此之故，建議粗分量一部分必須有一尺寸減小步驟 以慎重地確保此必需之細分量之出現。由是，此粒徑發生 比率之機會充分不太可能。有利的是重量約3 〇 %的粗分 量接受此尺寸減小步驟，所形成的細分量和最細分量與粗 分量混合以形成一第二混合分量，最好用於舖路的混合分 量7 0%重量由粗分量形成。 在第二混合分量中，大多數的粒徑大於8顧’經驗顯 示這些成分有再利用所需品質，然而，粒徑不小於2 mi且 小於8腿者佔一低比率有其必要，以確保上述舖路用之殘 -25- (19) (19)200304535 留物之可壓實性。 依據第三組發明之再一實施例，第二混合分量以從濕 式排放器來之水洗滌，且第一混合分量分離，此時，粒徑 2匯以下之部分（往往帶有特別嚴重污染物負擔）可確定 地從可回收殘留物分離。 此洗滌水可有利地送到濕式排放器，如前文所述，藉 由以此方式將水回送，新水之消耗可儘可能地低。 在此建議分離的金屬以從排放器來之水進行洗滌步驟 ，使黏附的任何燃燒殘留物得以洗掉，有利的是使用一篩 選步驟來機械地將分量分離。 添加可溶解重金屬沉澱劑到排放器水中對於改善回收 的燃燒殘留物品質相當有幫助’結果這些重金屬可藉由添 加沉澱劑而分離。 接著將參照所附圖式進一步說明本發明之第一至第三 組發明實施例，下文中所用特定値（量）諸如重量和百分 比係解釋實施例之典型者，不應以這些値（量）來限制本 發明。 圖1和圖2爲第一組發明方法工作流程圖。第一組發 明將參照這些圖式詳細說明。 在圖1和圖2所示方法中，含有2 2 0公斤灰之 1 0 0 0公斤廢棄物（方塊1 0 0 )進給到一質量燃燒系 統並且其燃燒方式使得所產生的燃燒殘留物重量的2 5〜 7 5 %變成全燒結底灰（方塊1 0 2 )，總共得到3 0 0 公斤之燃燒殘留物，這些殘留物落入一濕式排放器（方塊 -26- (20) (20)200304535 10 4)，殘留物在該處被猝息，接著被排出（方塊 10 6)，經過一分離程序（包括篩選）以及可能之洗滌 (方塊1 0 8 )，分離出2 0 0公斤的全燒結底灰（方塊 110)，且將之再利用（方塊1 1 2 )。尙未燒結的 1 0 0公斤燃燒殘留物回送到燃燒程序（方塊1 1 4 )， 與烟道氣體一起離開的飄塵重量爲2 0公斤，且在一烟道 氣體過濾器內回收（方塊1 1 6 )以及經由淸洗鍋爐管而 回收（方塊1 1 8 )，所回收之飄塵送到一分開的棄置通 道路（方塊1 2 0 )。 在圖2所示方法中，3 1 0公斤之燃燒殘留物落入一 濕式排放器，而且1 0公斤的飄塵回送到燃燒程序，除此 之外圖2所示方法與圖1中所示者相同，因此以相同的標 號來標示與圖1中相同之方塊。 接著將參照圖3至圖6之工作流程圖來說明第二組發 明之方法實施例。 如圖3所示，含有2 2 0公斤灰之1 0 0 0公斤廢棄 物（方塊3 0 0 )供至一柵基系統（方塊3 0 2 )之後燃 燒，此燃燒程序產生8 0 0公斤的烟道氣體（方塊3 0 1 )和3 0 0公斤燃燒殘留物，這些殘留物前送到一濕式排 放器（方塊3 0 4 )，從該處，因爲濕了之故，3 1 5公 斤的燃燒殘留物或底灰（方塊3 0 6 )被取出，取出的殘 留物受到機械分離，此際係篩選8 mi粒徑（方塊3 0 8 ) 。此程序將2 1 5公斤之燃燒殘留物或底灰分成粒徑大於 8 iM之主分量（方塊3 1 0 )和粒徑小於8 uun之約1 〇 〇 -27- (21) (21)200304535 公斤之細分量和最細分量（方塊3 1 2 )。具有粒徑大於 8醒且由粗分量和超大尺寸分量所組成之底灰受到濕化處 理（方塊3 1 4 )，在此程序中，提供從濕式排放器取出 之1 0 0 0升之水來洗滌底灰，由是沖洗出粒徑小於8 min 之1 5公斤細組成。實際上，底灰在一篩上洗滌，該篩允 許8 mm或更小的分量通過。已用來洗滌底灰之水連同細分 量和最細分量回到濕式排放器，已洗滌底灰取出而可馬上 用於再利用程序，諸如舖路（方塊3 1 6 )，而且約 1 0 0公斤的被篩選移除的細分量一般是回到柵基系統以 進一步燒結。然而，細分量亦可用於其他目的（方塊 3 18) 。4 0升的補充水或新水被加入以補償濕式排放 器中水之損失，因爲燃燒殘留物在被取出濕式排放器之時 自然地會攜帶著水。 上述程序可變化成圖4所示，在此變化實施例中，粒 徑大於8醒的主分量之濕化處理之後以新水沖洗，特別言 之，爲了將以濕式排放器之水濕化處理而受混入的成分移 除，8 0升的新水（方塊3 2 0 )加入到2 0 0公斤主分 量（方塊3 2 2 ) 。4 0升的沖洗水被留住以刷洗烟道氣 體或用於其他棄置處理，而另外的4 0公斤回到濕式排放 器做爲補充水以補充水之損失。依此方式洗滌之底灰可導 入其他再利用程序。 圖5爲第二組發明之程序另一實施例，在此變化實施 例中，含有2 2 0公斤灰之1 0 〇 〇公斤廢棄物（方塊 5 0 0 )供至一柵基系統（方塊5 0 2 )之後燃燒，此燃 (22) (22)200304535 燒程序產生8 0 0公斤的烟道氣體（方塊5 0 4 )和 3 2 0公斤燃燒殘留物，這些殘留物前送到一濕式排放器 (方塊5 0 6 ) 。3 3 6公斤的燃燒殘留物從濕式排放器 取出，重量增加是因爲從底灰來之細粒子亦即含在底灰洗 滌水中之細粒子回到濕式排放器。4 0升的水加入濕式排 放器以補充水之損失，3 3 6公斤的底灰或燃燒殘留物前 送到一濾網，濾網允許粒徑3 2 imn之分量通過（方塊 5 0 8 )。粒徑大於3 2 min之超大尺寸分量先被送到一金 屬分離器（方塊5 1 0 )，金屬已分離之底灰輸送到一個 產生粒徑約8 mm之底灰的碾碎器（方塊5 1 2 )，碾碎的 底灰輸送到允許粒徑8 inm之分量通過的另一濾網（方塊 5 14)，具粒徑小於8 mm的1 0 0公斤底灰或燃燒殘留 物以此機械分離程序移除，而且最好回到柵基系統，底灰 被棄置或是受到進一步處理（方塊5 1 5 )，剩下的粗分 量送到一金屬分離器（方塊5 1 6 )。由金屬分離器移除 之金屬成分以及被上述金屬分離步驟分離之金屬成分被收 集且受到加濕處理，藉由加濕處理，黏附在金屬成分上之 底灰粒子被洗掉（方塊5 1 8 )，結果得到用於再利用程 序之2 0公斤的鐵及非鐡金屬（方塊5 2 0 )，金屬已移 除之底灰或粗分量（粒徑8〜3 2腿）重量爲2 1 5公斤 (方塊5 2 2 ) ，6 0公斤的粗分量送到一碾碎器（方塊 5 2 4 )，粒徑降低到小於2 min，碾碎之後，碾碎的分量 與1 5 5公斤的未碾碎粗分量混合，且混合物以一個允許 粒徑2醒之分量通過的一濾網進行加濕處理（方塊5 2 6 -29 - (23) (23)200304535 )’加濕處理需要的1 〇 〇 〇升洗滌水由濕式排放器供應 ，加濕處理產生粒徑爲8〜3 2匪之1 5 5公斤底灰以及 粒徑爲2〜8 inm之4 5公斤細分量，這兩種分量係用於再 利用程序’亦即做爲建築材料或馬路副底層（方塊5 2 8 )’另一方面，藉由加濕處理移除之粒徑小於2匪的細分 量回到濕式排放器。 圖6中之工作流程圖爲圖3中實施例之基本變化，其 中使用可溶解金屬之沉澱劑，沉澱劑注入濕式排放器以將 排放器中水中鉛濃度從2 m g / L降到〇 · 〇 5 m g / L (方塊3 2 6 ) ’此沉澱劑將溶解在將2 Ο 0公斤底灰加 濕的約2 0升的底灰水中之鉛減少到1 1T1 g，4 0 0公斤 的錯處於燃燒處理（方塊3 0 2 )所產生的烟道氣體中。 在以允許粒徑8 m的分量通過的篩子之機械分離程序中（ 方塊308)，在400公克的鉛中，200公克的鉛留 在在洗滌後送到再利用程序的2 0 0公斤底灰（方塊 3 1 0 )中，另一方面，2 0 0公克的鉛與粒徑小於8麵 的細分量（方塊3 1 2 ) —起回到柵基系統（方塊3 0 2 )〇 另外’接著將參照圖7 - 1 0說明第三組發明之方法 實施例。 如圖7中所示，含有2 2 0公斤灰之1 〇 〇 〇公斤廢 棄物（方塊7 0 0 )進給到一柵基系統（方塊7 〇 2 )並 且其燃燒方式使得所產生的燃燒殘留物重量的2 5〜7 5 %變成全燒結底灰，此燃燒產生8 0 0公斤的烟道氣體以 -30- (24) (24)200304535 及3 0 0公斤的燃燒殘留物，這些殘留物送到一濕式排放 器（方塊7 0 6 )，在加濕下，3 1 5公斤的殘留物或底 灰被取出（方塊7 0 8 )，被取出的殘留物此時受到機械 分離，篩選粒徑爲8 mm者（方塊7 1 0 )。此程序將 2 1 5公斤的燃燒殘留物分成粒徑大於8醒的主分量（方 塊7 1 2 )以及粒徑小於8 min的細分量和最細分量（方塊 7 14)。粒徑大於8 min的粗分量和超大尺寸分量所組成 之底灰受到加濕處理（方塊7 1 6 )，在此程序中，從濕 式排放器取出之1 0 0 0升水供應底灰之洗滌，由是洗出 粒徑小於8醒的1 5公斤細成分。實際上底灰係以允許8 mm或更小的分量通過之濾網洗滌，已用來洗滌底灰的水與 細分量和細分量回到濕式排放器，洗滌後的底灰被取出而 能馬上用於再利用程序，諸如舖路（方塊7 1 8 )。藉由 篩選移除的1 0 0公斤細分量一般是回到柵基系統以進一 步燒結，然而，細分量亦可用於其他程序（方塊7 2 0 ) 。4 0升的補充水或新水被加入以補充濕式排放器中水之 損失，因爲燃燒殘留物在其從濕式排放器被取出時自然地 將水攜出。 上述程序亦可修改成如圖8所示，在此實施例中，在 粒徑大於8醒的主分量加濕處理後爲以新水（方塊7 2 2 )沖洗（方塊7 2 4 )，特別言之，爲了移除以濕式排放 器來的水進行加濕處理形成的攜帶組成物，2 0 0公斤的 主分量加入8 0升的新水，4 0升的沖洗水用來進行烟道 氣體刷洗（方塊7 2 6 )或其他棄置處理，另外的4 0公 -31 - (25) (25)200304535 斤回到濕式排放器做爲水損失之補充水，依此方式洗滌的 底灰可導入其他再利用程序。 圖9爲第三組發明的程序另一實施例，在此實施例中 ，含有2 2 0公斤灰之1 0 0 0公斤廢棄物（方塊9 0 0 )前送至一柵基系統（方塊9 0 2 )，此燃燒程序產生 8 0 0公斤的烟道氣體（方塊9 0 4 )和3 2 0公斤燃燒 殘留物，這些殘留物前送到一濕式排放器（方塊9 0 6 ) 。3 3 6公斤的燃燒殘留物從濕式排放器取出，重量增加 是因爲含在底灰洗滌水中之細粒子回到濕式排放器。4 0 升的水加入濕式排放器以補充水之損失，3 3 6公斤的底 灰或燃燒殘留物前送到一濾網，濾網允許粒徑3 2 mm之分 量通過（方塊908)。粒徑大於32 imn之超大尺寸分量 先被送到一金屬分離器（方塊9 1 0 )，金屬已分離之底 灰輸送到一個產生粒徑約8 mm之底灰的碾碎器（方塊 9 12)，碾碎的底灰輸送到允許粒徑8 imn之分量通過的 另一濾網（方塊9 1 4 )，具粒徑小於8 mm的1 0 0公斤 底灰或燃燒殘留物以此機械分離程序移除，而且最好回到 柵基系統，底灰被棄置或是受到進一步處理（方塊9 1 5 )，剩下的粗分量送到一金屬分離器（方塊9 1 6 )。由 金屬分離器移除之金屬成分以及被上述金屬分離步驟分離 之金屬成分被收集且受到加濕處理（方塊9 1 8 )，藉由 加濕處理，黏附在金屬成分上之底灰粒子被洗掉，結果得 到用於再利用程序之2 0公斤的鐵及非鐵金屬（方塊 9 2 0 )，金屬已移除之底灰或粗分量（粒徑8〜3 2隨 -32- (26) (26)200304535 )重量爲2 1 5公斤（方塊9 2 2 ) ，6 0公斤的粗分量 送到一碾碎器（方塊9 2 4 )，粒徑降低到小於2 mm，碾 碎之後，碾碎的分量與1 5 5公斤的未碾碎粗分量混合， 且混合物以一個允許粒徑2 min之分量通過的一濾網進行加 濕處理（方塊9 2 6 )，加濕處理需要的1 0 0 0升洗滌 水由濕式排放器供應，加濕處理產生粒徑爲8〜3 2腿之 1 5 5公斤底灰以及粒徑爲2〜8mm之4 5公斤細分量， 這兩種分量係用於再利用程序（方塊9 2 8 )，另一方面 ，藉由加濕處理移除之粒徑小於2 mm的細分量回到濕式排 放器。 圖1 0中之工作流程圖爲圖7中實施例之基本變化， 其中使用可溶解金屬之沉澱劑，沉澱劑注入濕式排放器以 將排放器中水中鉛濃度從2 m g / L降到〇 . 〇 5 m g / L (方塊7 2 8 )，此沉澱劑將溶解在將2 0 0公斤 底灰加濕的約2 0升的底灰水中之鉛減少到1 m g， 4 0 0公斤的鉛處於燃燒處理（方塊7 0 2 )所產生的烟 道氣體中。在以允許粒徑8 nun的分量通過的篩子之機械分 離程序中（方塊7 1 〇 )，在4 0 0公克的鉛中，2 0 0 公克的鉛留在在洗滌後送到再利用程序的2 〇 〇公斤底灰 (方塊7 1 2 )中，另一方面，2 0 0公克的鉛與粒徑小 於8 mm的細分量（方塊7 1 4 ) —起回到柵基系統（方塊 7 0 6 ) 〇 如上所述，依據本發明第一組發明，其提供一種方法 ’其中可得到具所要品質之全燒結底灰而不需使用下游熔 -33- (27) (27)200304535 化或玻璃化單元。 而且，依據本發明第二組發明，其提供一種方法，其 中可分離出良好品質底灰分量，避免灰塵飄揚缺點以及從 爐進入空氣造成的問題，也減少水之進一步浪費。 另外，本發明第三組發明，其提供一種方法，其中燃 燒程序可調節以得到具有所要品質之全燒結底灰而不需下 游融化或玻璃化單元，在使用最少設備下避免避免灰塵飄 揚缺點以及從爐進入空氣造成的問題，也減少水之進一步 浪費。 雖然本發明已以實施例加以說明，但不限於此，對習 於此技人士而言，在不偏離本發明技術範圍之內仍可輕易 地進行所有修改，變化及增加。 〔圖式簡單說明〕 圖1爲第一組發明方法一實施例工作流程圖。 圖2爲第一組發明方法另一實施例工作流程圖。 圖3爲第二組發明方法一實施例工作流程圖。 圖4爲第二組發明方法另一實施例工作流程圖。 圖5爲第二組發明方法又一實施例工作流程圖。 圖6爲第二組發明方法更一實施例工作流程圖。 圖7爲第三組發明方法一實施例工作流程圖。 圖8爲第三組發明方法另一實施例工作流程圖。 圖9爲第三組發明方法又一實施例工作流程圖。 圖1 0爲第三組發明方法更一實施例工作流程圖。 -34-200304535 (1) Description of the invention [Technical field to which the invention belongs] The present invention relates to a method for improving the properties of combustion residues produced in a combustion plant (especially a plant that converts waste into energy), wherein the fuel is in a combustion grill Combustion, and raise the temperature of the combustion residues under appropriate fuel control. The invention also relates to a method for treating residues from a combustion plant (especially a waste calcining unit), in which fuel is burned on a combustion grid, and the combustion residues produced are quenched in a wet exhauster, and thereafter From the drain to the outside. In addition, the present invention also relates to a method for treating residues from a combustion plant (especially a plant that converts waste into energy), in which the fuel is burned on a combustion grid and the combustion produced is raised under proper fuel control. Residual temperature. [Prior art] In this method, as disclosed in European Patent EP 0 667 490 B1, the fuel is heated on the combustion grid until the temperature of the bottom ash generated by the combustion is just below the melting point of the bottom ash before the melting stage outside the combustion grill, This method regulates the combustion so that the temperature of the gate end is as high as possible to keep the energy required for the downstream melting stage as low as possible. However, the bottom ash does not sinter or melt at this point, but in order to achieve the required bottom ash quality, a downstream melting stage is required. This downstream melting stage requires not only related equipment, but also an increased energy source, even if the aforementioned heating operation is performed in the downstream melting stage. . -8-(2) (2) 200304535 Waste inorganic and organic pollutant components are important to the required bottom ash quality. Furthermore, heavy metals and plutonium are the main inorganic pollutant components, and inorganic pollutants are especially caused by It is generated by incomplete combustion. In addition, the evaluation of the bottom ash quality is mainly how much pollutants are leached out during the cleaning test. In addition, the mechanical properties of the bottom ash are important in assessing their suitability for construction works such as landfills, geotechnical, and pavers. Due to the high temperature involved in the treatment of combustion residues, the melting combustion residues are characterized by a low percentage of organic compounds. The typical bottom ash type of a plant that converts waste to energy contains 1 to 5% by weight of unburned materials, which is generally judged For the amount of ablation, the ablation amount of the melt combustion residue is less than 0. 3%. Melt combustion residue is also characterized by low plutonium emission and low percentage of heavy metals. This is because they either evaporate or pour into the formed glass matrix when the molten mass is cooled. on the other hand, German patent DE 701 606 C discloses a technology, The combustion residue is sent to a discharger of a discharge cylinder having an inlet section and a rising outlet slot, And from there, it is drained out with a drain plug, These combustion residues are called bottom ash, Supply the bottom ash's sudden water to the discharge tank, Only enough fresh water needs to be introduced into the tank to offset the amount of water discharged with the wet bottom ash. The steady-state concentrations of many substances and compounds (such as ravioli) that adhere to the residue make it impossible to reduce these concentrations within itself, As a result, the quality of the bottom ash is unsatisfactory in the application of landfill disposal sites and reuse as building materials. The reason for this disadvantage is that the residue is not separated (sorted) into a better quality component and a better quality component 'results' inevitably the overall combustion residue quality is not satisfactory. -9- (3) (3) 200304535 German patent case DE 4 4 2 3 9 2 7 also discloses a technology, The residue from the furnace is directly sent to the water bath for rough washing without previous suddenness, The dry bottom ash after rough washing is divided into at least two parts, All particles smaller than 2 mm are assigned as the first component, While the other particles are assigned the second component, This method continues to divide the second component into at least two components in a screening step, All less than 2 7 ~ 3 5 mm are assigned as the third component, The remaining particles are assigned as the fourth component, This yields a satisfactory residue content, However, the disadvantage of this method is that a large amount of dust flying and the air entering from the furnace cause problems. [Summary of the Invention] The production of the present invention focuses on various problems of the conventional techniques described above. The first group of inventions of the present invention aims to provide a method, The combustion process can be adjusted to obtain a fully sintered bottom ash of the desired quality without the need for a downstream melting or vitrification unit. The second group of invention aims to provide a method, Which separates out the good quality bottom ash content, Avoid the shortcomings of dust flying and problems caused by air entering from the furnace, It also reduces further waste of water. In addition, The third group of inventions aims to provide a method, The combustion process can be adjusted to obtain a fully sintered bottom ash of the desired quality without the need for a downstream melting or vitrification unit. Avoid the shortcomings of fly ash and the problems caused by air entering from the furnace with the least equipment, It also reduces further waste of water. Next, the method for improving the quality of the combustion residues produced by the combustion plant and the method for treating the residues will be described with the preferred embodiment shown in the accompanying drawings. [Embodiment] The first group of inventions: Methods for improving the properties of combustion residues produced by combustion plants The first set of inventions were achieved by operating a combustion control system to enable the combustion residues to be sintered and / or melted into the bottom ash on the fuel bed in the main combustion zone, And the unmelted or sintered combustion residues are discharged at the end of the combustion process, After that, return to the combustion program again. The first group of inventions is based on the idea that the combustion process is performed on the grid so that the fuel bed in the main combustion zone is sintered or melted in advance. The second is to return the unsintered or molten combustion residues of rhenium. This makes it possible to achieve the desired degree of sintering or melting in the second or third attempt. In the first group of inventions, The term "fully sintered bottom ash" refers to a material composed of sintered and / or melted masses typically having a particle size of at least, for example, 8 inm, These blocks are composed of solid waste burning residues that have solidified after being completely or surface melted. The sintered and / or melted mass is preferably porous, Because gas is released during sintering and melting, The possible porosity of the fully sintered bottom ash is due to the molten bottom ash temperature on the fuel bed being not high enough to obtain a suitably low porosity. Also, the bubbles remain behind after being driven out by a bubble removal procedure similar to that known in glass manufacturing. Fully sintered bottom ash is different from the typical vitrified bottom ash obtained by downstream high temperature processing using crucible electric furnaces or other melting units lined with refractory materials. Composition of garbage such as glass or metal that passes through the grid but is not affected in the end -11-(5) (5) 200304535 Strictly speaking, those that are neither melted nor sintered on the fuel bed, however, Fully sintered base ash can contain these glasses or metals, These compositions have the proper properties to burn out and precipitate pollutants. The word “sintering” is based on Hammerli (Miill and Abfall 31, Disposal of bottom ash and other residues, Page 1 4 2 Published 1984) means "the special condition of melting and solidification", Therefore, the meaning of “smelting the surface or melting the particles together” in the following “sintering” often goes beyond its general scientific usage. The mass produced by the sintering of the fully sintered bottom ash can be completely or partially melted. Unsintered and / or molten bottom ash composition is defined as residual bottom ash, Compared with fully sintered bottom ash, Residual bottom ash characteristics are small particle size, High ablation Moreover, the ratio of precipitated pollutants is high. The first group of inventions focused on the sintering and / or melting of already existing residues and the fuel beds of the main combustion zone that have not been considered as possible so far. Actually, If the liquid bottom ash is between individual bars or other movable elements of the grid, Very harmful to mechanical burner, For this reason, it is necessary to prevent the bottom ash from melting on the grid. Care must be taken so that the melting point of the bottom ash does not reach the fuel bed. With the first set of inventions, The reason for the sintering and / or melting process in the upper fuel bed is that the maximum thermal shock occurs from above through the flame body radiation, And the material placed directly on the grid can be kept at a lower temperature than from the top of the fuel bed by adding cooler (relatively speaking) lower combustion air. Since not all combustion residues can be converted into fully sintered bottom ash of appropriate quality when the combustion is regulated in this way, Combustion residues that are not fully sintered return to the combustion process. -12- (6) (6) 200304535 Completes the sintering and / or melting procedure on the fuel bed without additional external energy, The quality of the bottom ash obtained is very similar to the products familiar to those skilled in the art from known downstream melting and vitrification high temperature procedures. The units used are such as Crucible electric furnace, As well as the melting chamber. However, one of the major disadvantages of these conventional methods is that they require very complex additional units, And the energy consumed is high. The first set of inventions addresses this problem, And it can produce a bottom ash with almost the same quality as the bottom ash obtained by the conventional method. A significantly advantageous embodiment of the combustion control system according to the first group of inventions, The lower combustion air is added with oxygen according to the quality of the waste to be burned (garbage quality), So that the oxygen volume content is about 25 to 40%, The best is 2 5 ~ 30%, and, According to another advantageous embodiment, The lower combustion air is preheated to about 100 ~ 400 ° C. These measures can be used individually or together, It depends. The temperature of the fuel bed (usually the refuse layer), which is a function of fuel characteristics, is best set at 1000 ~ 140 ° C. All combustion control measures to achieve the required conditions to convert combustion residues into sintered and / or molten bottom ash are selected so that a specific proportion of fully sintered bottom ash occurs (e.g. 2 to 5 to 7 weight 5%), In this way, ensure that there is enough unmelted material on the fuel bed in the main combustion zone to surround the molten ash, So that this measure will not adversely affect the mechanical grid parts. In another advantageous embodiment of the invention, Dust returns to the burning process, Dust leaves the fuel bed with the combustion gases, It is introduced into the downstream flue gas filter via the boiler. After the incomplete and completely sintered bottom ash is discharged from the combustion system, it is separated in a bottom ash sieve (-13) The oversized ones are completely sintered bottom ash, If the size is too small, the weight will be returned. Those skilled in the art know that there are many mechanical separation methods to perform this separation procedure. Isolation can be through screening or a combination of screening and washing steps, As described in other advantageous embodiments of the invention. Of course, there are other measures to improve the bottom ash quality outside the combustion plant. Especially special washing steps with and without chemical additives. The particle size is returned to the combustion process from a subdivision of less than 2 to 10 mm. This can be done by adding the subdivided amount to the fuel to be fed or by feeding it directly into the fuel bed, To avoid adding dust and for ease of handling, Fines are properly granulated and lumped before being returned. The second group of inventions: Method for treating combustion residues generated by a combustion plant The second group of inventions is achieved through technical features based on two different procedures described below. The first procedure consists of one step, The combustion residue from a wet exhaust is mechanically divided into two components, The principal component is mainly composed of a coarse component and an oversized component. The main component is washed with water from the wet drain, By separating the thinner parts that stick to the combustion residue, The wash water is taken to the wet drain together with the finer part dissolved in the washing step. If water from a wet drain is circulated in this way, Good quality main components can be released from the finer parts without a lot of fresh water, Otherwise it will stick to the burning residue, This will adversely affect the quality of the principal components. result, The finer part of the combustion residue that has been washed is of good quality, And it can be effectively reused as a base ash for building materials, for example. -14- (8) (8) 200304535 The second program consists of one step, The combustion residue from a wet exhaust is mechanically divided into two components, The principal component is mainly composed of a coarse component and an oversized component. The main component is crushed ’and washed with water drawn from the wet drainer. By separating the finer part of the crushed combustion residue, Instead, the wash water is taken to the wet drain, along with the finer part dissolved during the washing step. The second procedure has the advantage of releasing the contaminants contained in the main component before washing, in this way, The contained contaminants are removed during the washing step. Another advantage is the larger surface area of the crushed material, It is important for the porous state of the material obtained from the principal component. The second procedure is used when a high-quality combustion residue is required, or when there are many pollutants in the main component, or when the porosity of the combustion residue is important, The second procedure is also used in the case where the main component of the bottom ash is further crushed in the subsequent processing step. For example, when the bottom ash main component (final product) must be crushed in a leaching test to determine its quality It is better to use the second procedure. The main component after crushing and washing the bar cannot be mixed with the subdivided amount. In most cases, Since the main component has been melted or sintered, Low levels of unburned or leachable pollutants ’so that these qualities will not change by crushing, therefore, The main component of the crushing according to the second procedure has a very different quality compared to the bottom ash subdivision containing a large amount of the above-mentioned pollutants. According to an embodiment of the second group of inventions, The most finely divided and produced fines during mechanical separation are conveyed (circulated) to the combustion program. These components are again subjected to the combustion program, This enables it to melt and sinter. With these measures, Disadvantages of the previous first conventional technical procedure (all combustion residues are not reused, Even if it contains a small amount of better quality residues -15- (9) (9) 200304535) can be avoided. Compared with the second conventional technique, the problems of dust flying and furnace sealing are avoided. In addition, By returning the lowest and lowest quality subdivisions, More recyclable combustion residues, Because the returned part has the opportunity to solidify into a combustion residue of the required quality, Whether it is the first loopback or a repeat loopback. The second conventional method does not have this advantage. Because there is no return to the combustion program. According to another embodiment of the first or second program of the second group of inventions, The pre-washed water with the main amount of fresh water from the wet-type drainer is used to wash it ’, and the discharged water carrying a considerable amount of pollutants is washed out. As a result, the quality of combustion residues and / or sintered bottom ash is further improved. Since the coarse portion is washed with fresh water, This has the advantage that a certain percentage of the water obtained from the scrubbing can be sent to the flue gas scrubbing system without having to be pretreated, Because the percentage of pollutants it contains is quite low. In addition, This embodiment provides an advantage, That is, a certain percentage of the water obtained from the washing can be supplied to the wet drain, The water level in the drain can be maintained in this way, Since water is continuously carried out with the exhausted combustion residue, The water level in the drain drops, Because the amount of calcium and thorium sulfate in the water obtained from the washing is negligible, The tubes and nozzles will not clog. According to the second procedure of the second group of inventions, Even after the first separation step, the main component contains a high percentage of oversized components (generally containing a large amount of broken metal), The extra-large size coarse component is further separated in a mechanical step according to another embodiment of the present invention. The metal is separated by a magnetic separator. In an embodiment of the second group of inventions, One example is to differentiate the particle size so that the less than 2 mm is the most subdivided amount. The number of subdivisions is not less than 2 and less than 8 mm. Coarse component is not less than 8 丨 mn and less than 3 2 nun, But (10) (10) 200304535 is less than 3 2 2 are oversized. These are provided as a guide to better understand the invention, obviously, Each component containing a certain percentage of the subdivision is attached to itself, As long as this percentage is negligible. Generally speaking, Subdivisions with a particle size of less than about 8 mm (directly from the emitter) should preferably be returned to the combustion process, Because of its poor quality. In the second procedure, Produced a crushed principal component with a particle size that is comparable to the finely divided amount The crushed main component has better quality and can be used as a building material. For example, In the second procedure, If the first coarse separation step takes 32 mm as the cutoff point, That is, if the oversized components are separated, It is recommended to provide a second mechanical step with, for example, 8 imn as the cut-off point, Return all parts smaller than 8 mm to the combustion procedure. To get as many reusable components as possible, According to yet another embodiment of the second group of inventions, It is logical to reduce the size of the coarse component and the oversized component from the main component (for example, by using a crusher, Crushing combustion residue from rock crushers, etc.), It is recommended that the first mixed component be mechanically separated, To remove unwanted particles, This is because particle size discrepancies are generated during size reduction and are reused and returned to, for example, a combustion program. For areas of special interest for the preparation of combustion residues for basic applications in paving, The material must be compactable, No subdivision quantum (particle diameter is, for example, not less than 2 imn and less than 8 mm, (As described above) is not possible. For this reason, It is recommended that a portion of the coarse component must have a size reduction step to carefully ensure that this necessary amount of subdivision occurs. By The chance of this particle size ratio occurring is sufficiently unlikely. It is advantageous that the coarse fraction of about 30% by weight -17- (11) (11) 200304535 is subjected to this size reduction step, The formed subdivision amount and the most subdivision amount are mixed with the coarse component to form a second mixed component, 70% by weight, preferably for paving, is made of coarse components. In the second mixed component, Most are larger than 8 legs, Experience has shown that these ingredients have the required quality for reuse, however, It is necessary that the particle size is not less than 2 and less than 8 to account for a low ratio. To ensure the compactability of the remnants used in the above paving. According to yet another embodiment of the second group of inventions, The second mixed component is washed with water from a wet drain, And the first mixed component is separated, at this time, Particle fractions below 2 imn, often with particularly severe pollutant burdens, can definitely be separated from recyclable residues. This wash water can advantageously be sent to a wet drain, as described above, By returning water in this way, The consumption of fresh water can be as low as possible. It is recommended that the separated metal be washed with water from the drain, Allowing any sticking combustion residue to be washed away, It is advantageous to use a sieving step to mechanically separate the components. Adding soluble heavy metal precipitants to the effluent water is quite helpful for improving the quality of the recovered combustion residues, As a result, these heavy metals can be separated by adding a precipitant. The third group of inventions: Method for treating combustion residues generated in a combustion plant The above object is achieved by a method of the third group of inventions described below based on two different methods. According to the invention, The first of these methods is to operate the combustion control system so that the combustion residues are pre-sintered and / or -18- (12) (12) 200304535 melted into the bottom ash on the main combustion zone combustion bed, All the combustion residues produced in a wet exhauster and then taken out of the exhauster, A mechanical separation step is used to separate the wet combustion residue from the wet discharger into two components, Then, the main component composed of the coarse component and the oversized component is washed with water drawn from the wet drainer. Thus separating the thinner part of the combustion residue, And the washing water and the finer part dissolved in the washing step are sent to the wet discharger. When it is assumed that the reusable principal component contains a negligible ratio of washable pollutants (such as plutonium or heavy metals), The first method works. The third group of inventions has two main technical features, The first is to include a combustion control system, The second is the mechanical treatment of residues from the combustion process, The second technical feature includes two different methods depending on the fuel composition. The combustion control system included in the first technical feature is common to the following two methods in the mechanical treatment of residues, And according to the burning process on the grid, It is implemented such that sintering or melting occurs on the grid of the main combustion zone, And based on the return of unsintered or molten combustion residue, This makes it possible to achieve the required degree of sintering and / or melting in the second or third attempt. The term "fully sintered bottom ash" means a material consisting of sintered and / or fused masses typically having a particle size of, for example, at least 8 mm, These blocks consist of solidified refuse burning residues that have completely or surface melted. The sintered and / or melted mass is preferably porous, Because gas is released during sintering and melting, The possible porosity of the fully sintered bottom ash is due to the molten bottom ash temperature on the fuel bed being not high enough to obtain a suitably low porosity. And the bubbles are still left behind after being driven out by a bubble removal procedure like -19- (13) (13) 200304535, which is similar to known glass manufacturing. Fully sintered bottom ash is different from the typical vitrified bottom ash obtained by downstream high temperature processing using crucible electric furnaces or other melting units lined with refractory materials. Garbage compositions such as glass or metal that pass through the grid but are not affected in the end are strictly neither melted nor sintered on the fuel bed, however, Fully sintered base ash can contain these glasses or metals, These compositions have the proper properties to burn out and precipitate pollutants. The word "sintering" means "special conditions of melting and solidification" according to the word meaning (see Hammerli above), Therefore, the meaning of “melting the surface or melting the particles together” in the following “sintering” often goes beyond its general scientific usage. The mass produced by the sintering of the fully sintered bottom ash can be completely or partially melted. Unsintered and / or molten bottom ash composition is defined as residual bottom ash, Compared with fully sintered bottom ash, Residual bottom ash characteristics are small particle size, High ablation Moreover, the ratio of precipitated pollutants is high. The present invention looks at the sintering and / or melting of already existing residues and the fuel bed in the main combustion zone which has so far not been considered possible. Actually, If the liquid bottom ash is between individual bars or other movable elements of the grid, Very harmful to mechanical combustion grids, For this reason, it is necessary to prevent the bottom ash from melting on the grid. Care must be taken so that the melting point of the bottom ash does not reach the fuel bed. With the third group of inventions, The sintering and / or melting process takes place in the upper fuel bed, The reason is that the maximum thermal shock occurs from above through the flame body radiation, And the material placed directly on the grid can be kept at a lower temperature than from the top of the fuel bed by adding cooler (relatively speaking) lower combustion air. Since not all combustion residues can be converted into fully sintered bottom ash with proper quality when adjusting the combustion in this way, Combustion residues that are not fully sintered return to the combustion process. No additional external energy is required to complete the sintering and / or melting process on the fuel bed, The quality of the bottom ash obtained is very similar to the products familiar to those skilled in the art from known downstream melting and vitrification high temperature procedures. The units used are such as Crucible electric furnace, As well as the melting chamber. However, one of the major disadvantages of these conventional methods is that they require very complex additional units, And the energy consumed is high. The third group of inventions addresses this issue, And it can produce a bottom ash with almost the same quality as the bottom ash obtained by the conventional method. In the above first method related to mechanical processing, If the water cycle originates from a wet drain, Can release good quality main components from detailed parts without large amount of fresh water, Otherwise it will stick to the burning residue, This will adversely affect the quality of the principal components. result, The finer part of the burned residue that has been washed has good quality, And can be effectively used as a recyclable bottom ash. In the second method, which is suitable for treating combustion residues that contain large amounts of pollutants that can be washed away, such as radon or heavy metals, The purpose is to operate the combustion control system in such a way that the combustion residues are sintered and / or melted in the bottom ash on the combustion bed in the main combustion zone in advance, All the combustion residues produced in a wet exhauster and then taken out of the exhauster, A mechanical separation step is used to separate the wet combustion residue from the wet exhauster into two components (the separated main component mainly composed of a coarse component and an oversized component, It undergoes a size reduction step, Then wash with water drawn from the wet drain), And the wash water and the finer part dissolved in the washing step are sent to the wet drain. As a result of the main component crushing, larger particles stuck in the combustion residue -21-(15) (15) 200304535 can be washed out in subsequent washing steps, So from the reusable principal component separation, in this way, A high percentage of residue can be recycled into a reusable bottom ash, Regardless of the many contaminants contained in the residue, There is no need to expect a significant washout of contaminants later. In the second method above, The combustion control included in the first technical feature of the present invention is also performed before the mechanical treatment. A significantly advantageous embodiment of the combustion control system according to the invention, The lower part of the combustion air is added with oxygen according to the quality of the waste to be burned (garbage quality), So that the oxygen volume content is about 25 to 40%, The best is 2 5 ~ 30%, and, According to another advantageous embodiment, The lower combustion air is preheated to about 100 ~ 400 ° C. These measures can be used individually or together, It depends. The temperature of the fuel bed (usually the refuse layer), which is a function of the fuel characteristics, is best set at 100 ° C to 140 ° C. All combustion control measures to achieve the required conditions to convert combustion residues to sintered and / or molten bottom ash are selected so that a specific proportion of fully sintered bottom ash occurs (e.g. 2 to 5 to 7 5%), In this way, ensure that there is enough unmelted material on the fuel bed in the main combustion zone to surround the molten ash, This will not adversely affect the mechanical grid parts. In another advantageous embodiment of the invention, Dust returns to the burning process, Dust leaves the fuel bed with the combustion gases, It is introduced into the downstream flue gas filter via the boiler. The second feature of the third group of inventions (that is, the mechanical treatment of combustion residues including the second method) is explained as follows. -22- (16) (16) 200304535 According to an embodiment of the third group of inventions, The finest components and subdivisions generated during mechanical separation are sent to the combustion program, These components are subject to the combustion process again, Therefore, it can be melted and sintered. With these measures, Disadvantages of the previous first conventional technical procedure (all combustion residues are not reused, Even if it contains a small amount of better poor quality residues) to avoid. Compared with the second conventional technology, Problems with dust flying and stove sealing (introduction of air) are avoided. In addition, By returning the most subdivided and subdivided quantities of poor quality, More recyclable combustion residues, Because the return detail has the opportunity to solidify into a combustion residue of the required quality, Whether it's the first loopback or a repeat loopback. The second conventional method does not have this advantage. Because there is no return to the combustion program. According to another embodiment of the third group of inventions, Rinse with fresh water pre-washed with fresh water from the wet drainer. The discharged water, which carries a considerable amount of pollutants, is washed out, As a result, the quality of combustion residues and / or sintered bottom ash is further improved. Since the coarse portion is washed with fresh water, The advantage is that a certain percentage of the water obtained from the scrubbing can be sent to the flue gas scrubbing system without having to be pretreated, Because the percentage of pollutants it contains is quite low. In addition, This embodiment provides an advantage, That is, a certain percentage of the water obtained from the washing can be supplied to the wet drain, The water level in the drain can be maintained in this way, Since water is continuously carried out with the exhausted combustion residue, The water level in the drain drops, Because the amount of calcium and thorium sulfate in the water obtained from washing is negligible, The tubes and nozzles will not block. In the second method of mechanical processing according to the present invention, 'even after the first separation step, the main component contains a high percentage of oversized components (generally -23- (17) (17) 200304535 contains a large amount of broken metal), The extra-large size coarse component is further separated in a mechanical step according to another embodiment of the present invention. The metal is separated by a magnetic separator. In an embodiment of the third group of inventions, One example is to differentiate the particle size so that the less than 2 mm is the most subdivided amount. Subdivision is not less than 2 mm and less than 8 mm. Coarse component is not less than 8 mm and less than 3 2 mm. Not less than 3 2 min is oversized. These are provided as a guide to better understand the invention, obviously, Each component containing a certain percentage of the subdivision is attached to itself, As long as this percentage is negligible. The amount of subdivision that comes directly from the emitter and has a particle size of not less than 2 sides and less than 8 bands is that the combustion residues are preferably returned to the part of the combustion process. on the other hand, The particle diameter of the fine part of the bottom ash particle size distribution included in the result of the crushing procedure according to the second method is equal to the particle size of the finely divided amount directly supplied by the discharger And the quality of this detail is better for reuse, Therefore, crushing the fine part of the bottom ash is called the high-quality subdivision. For example, In the second method, If the first coarse separation step is 32 mm as the cutoff point, That is, if the oversized components are separated, It is recommended to provide a second mechanical step with a cut-off point of, for example, 8 mm, Return all parts smaller than 8 mm to the burning procedure. It is recommended to separate the metal from the main component, To prevent mechanical separation equipment from being damaged by large pieces of shredded metal. Not just large pieces of broken metal, Other metals are also released from the main component that contains too little component (that is, the coarse component is less than 32 mm), These metal parts can be used as separate reuse programs. It is more convenient to remove the metal from the oversize component and the coarse component separately, -24- (18) (18) 200304535 Depending on the reuse procedure and type of combustion residues that are intended to be used 〇 If the combustion residues are to be used, for example, for paving, It is recommended that the oversize component undergo a further size reduction step after the metal parts larger than 32 mm which are less suitable for this purpose have been removed. In the second method, In order to get as many reusable components as possible, According to yet another embodiment of the third group of inventions, It is logical for the coarse component separated from the main component to be mixed with the crushed combustion residue produced by the oversize component downsizing step to form a first mixed component, It is recommended that the first mixed component be mechanically separated, To remove particles with unwanted particle sizes' because particle size discrepancies are generated during size reduction and further reused and returned to, for example, a combustion program. For areas of special interest for the preparation of combustion residues for basic applications in paving, The material must be compactable, There is no subdivided quantum (particle diameter, for example, not less than 2 mm and less than 8 dishes1, (As described above) is not possible. For this reason, It is recommended that a portion of the coarse component must have a size reduction step to carefully ensure that this necessary amount of subdivision occurs. By The chance of this particle size ratio occurring is sufficiently unlikely. It is advantageous to accept this size reduction step at a coarse content of about 30% by weight, The formed subdivision amount and the most subdivision amount are mixed with the coarse component to form a second mixed component, The blending content of 70%, preferably for paving, is formed by a coarse component. In the second mixed component, Most of the particle sizes are larger than 8 Gu ’experience shows that these components have the quality required for reuse, however, It is necessary to have a particle size of not less than 2 mi and less than 8 legs. In order to ensure the residue of the above paving -25- (19) (19) 200304535 the compactability of the remnants. According to yet another embodiment of the third group of inventions, The second mixed component is washed with water from a wet drain, And the first mixed component is separated, at this time, Particles below 2 sinks (often with a particularly severe pollutant burden) can definitely be separated from recyclable residues. This wash water can advantageously be sent to a wet drain, as described above, By returning water in this way, The consumption of fresh water can be as low as possible. It is recommended that the separated metal be washed with water from the drain, Allowing any sticking combustion residue to be washed away, It is advantageous to use a sieving step to mechanically separate the components. Adding a soluble heavy metal precipitant to the effluent water is quite helpful to improve the quality of the recovered combustion residues'. As a result, these heavy metals can be separated by adding a precipitant. Next, the first to third sets of invention embodiments of the present invention will be further described with reference to the attached drawings. Specific amounts (such as weight) and percentages used in the following are typical of the examples, The invention should not be limited by these amounts. Figures 1 and 2 are flowcharts of the first group of inventive methods. The first group of inventions will be described in detail with reference to these drawings. In the methods shown in Figures 1 and 2, 100 kg of waste (block 100) containing 220 kg of ash is fed to a mass combustion system and its combustion method makes 25% to 75% of the weight of the combustion residue produced into a fully sintered bottom Gray (box 1 0 2), A total of 300 kg of combustion residues, These residues fall into a wet drain (blocks -26- (20) (20) 200304535 10 4), The residue was suffocated there, Is then discharged (blocks 10 6), After a separation procedure (including screening) and possible washing (block 1 0 8), 200 kg of fully sintered bottom ash was separated (block 110), And reuse it (block 1 1 2). 尙 100 kg of unsintered combustion residue is returned to the combustion program (block 1 1 4), The weight of the dust that leaves with the flue gas is 20 kg. And recovered in a flue gas filter (block 1 1 6) and by washing the boiler tubes (block 1 1 8), The recovered dust is sent to a separate disposal road (block 120). In the method shown in Figure 2, 3 10 kg of combustion residue fell into a wet exhaust, And 10 kilograms of flying dust are sent back to the combustion program. Otherwise, the method shown in Figure 2 is the same as that shown in Figure 1, Therefore, the same blocks as those in Fig. 1 are designated by the same reference numerals. Next, the method embodiments of the second group of inventions will be described with reference to the working flowcharts of Figs. As shown in Figure 3, 100 kg of waste containing 200 kg of ash (box 300) is burned after being supplied to a grid-based system (box 300). This combustion process produces 800 kilograms of flue gas (block 301) and 300 kilograms of combustion residues. These residues are forwarded to a wet exhauster (block 3 04), From there, Because it gets wet, 3 1 5 kg of combustion residue or bottom ash (box 3 0 6) is taken out, The removed residue is mechanically separated, Here we select 8 mi particle size (box 3 0 8). This procedure divides 2 15 kg of combustion residue or bottom ash into a main component with a particle size greater than 8 iM (box 3 1 0) and a particle size with a particle size less than 8 uun about 1 00-27- (21) (21) 200304535 The subdivision and the most subdivision of the kilogram (box 3 1 2). Bottom ash with a particle size greater than 8 and consisting of coarse and oversized components is subjected to humidification treatment (block 3 1 4), In this procedure, Provide 100 litres of water from the wet drainer to wash the bottom ash. It consists of 15 kg of fine particles with a particle size of less than 8 minutes. Actually, The bottom ash is washed on a sieve, The screen allows passage of 8 mm or less. The water that has been used to wash the bottom ash is returned to the wet exhauster The washed bottom ash is taken out and can be used immediately for reuse Such as paving (blocks 3 1 6), And about 100 kilograms of fine particles removed by screening are generally returned to the grid system for further sintering. however, The amount of subdivision can also be used for other purposes (block 3 18). 40 litres of make-up or fresh water is added to compensate for the loss of water in the wet drain, Because combustion residues naturally carry water when they are removed from the wet exhaust. The above procedure can be changed as shown in Figure 4, In this variation, After the humidification of the main component with a particle diameter greater than 8 wakes, rinse with fresh water. In particular, In order to remove the components that are mixed in by the humidification of water in the wet discharger, 80 litres of fresh water (box 3 2 0) is added to the main component of 200 kg (box 3 2 2). 40 litres of rinsing water is retained for scrubbing the flue gas or for other disposal The other 40 kg is returned to the wet drain as make-up water to make up for the loss of water. The base ash washed in this way can be directed to other recycling programs. FIG. 5 shows another embodiment of the program of the second group of inventions. In this variation, 100 kg of waste (block 500) containing 220 kg of ash is supplied to a grid-based system (block 50 2) and burned. This burning (22) (22) 200304535 burning procedure produces 800 kg of flue gas (block 504) and 320 kg of combustion residues. These residues are forwarded to a wet drain (box 5 06). 3 3 6 kg of combustion residues are taken out of the wet exhaust, The weight increase is because the fine particles from the bottom ash, that is, the fine particles contained in the bottom ash washing water, are returned to the wet discharger. 40 litres of water were added to the wet drain to replenish the loss of water, 3 3 6 kg of bottom ash or combustion residue before sending to a filter, The strainer allows components with a particle size of 3 2 imn to pass (block 5 0 8). The over-sized components with a particle size greater than 3 2 min are first sent to a metal separator (block 5 10). The separated bottom ash of the metal is conveyed to a crusher (block 5 1 2) which produces a bottom ash with a particle size of about 8 mm. The crushed bottom ash is conveyed to another screen (block 5 14) which allows a particle size of 8 inm to pass through, 100 kg of bottom ash or combustion residue with a particle size of less than 8 mm is removed by a mechanical separation procedure, And it's better to go back to the grid-based system, The bottom ash is discarded or further processed (block 5 1 5), The remaining coarse fraction is sent to a metal separator (block 5 1 6). The metal components removed by the metal separator and the metal components separated by the above metal separation step are collected and subjected to humidification treatment, With humidification, The bottom ash particles adhering to the metal component are washed away (block 5 1 8), As a result, 20 kg of iron and non-rhenium metal (block 5 2 0) used in the recycling process were obtained. The weight of the removed base ash or coarse metal (particle size 8 ~ 3 2 legs) weighs 2 1 5 kg (box 5 2 2), 60 kg of coarse weight is sent to a crusher (block 5 2 4), Particle size reduced to less than 2 min, After crushing, Crushed portion mixed with 1 5 5 kg of unmilled coarse portion, And the mixture is humidified with a strainer that allows the particle size 2 to pass through (block 5 2 6 -29-(23) (23) 200304535). The 1,000 liters of washing water required for humidification Wet Drain Supply, Humidification treatment produces 155 kg bottom ash with a particle size of 8 ~ 3 2 and 4 5 kg subdivision with a particle size of 2 ~ 8 inm, These two components are used in the reuse process, that is, as the building material or the sub-floor of the road (block 5 2 8). The subdivided particles with a particle size smaller than 2 bands removed by the humidification process are returned to the wet discharger. The working flowchart in FIG. 6 is a basic change of the embodiment in FIG. 3. Which uses a precipitant that dissolves metals, The precipitant is injected into the wet discharger to reduce the lead concentration in the water in the discharger from 2 mg / L to 0.05 mg / L (box 3 2 6) 'This precipitant will be dissolved in the addition of 200 kg of bottom ash Wet lead in about 20 liters of bottom ash water was reduced to 1 1T1 g, The 400 kg error is in the flue gas generated by the combustion process (block 300). In a mechanical separation procedure with a sieve that allows a particle size of 8 m to pass (block 308), In 400 grams of lead, 200 grams of lead remain in the 200 kg bottom ash (box 3 1 0) sent to the recycling program after washing, on the other hand, 200 grams of lead with a particle size smaller than 8 sides (block 3 1 2)-back to the grid-based system (block 3 0 2). In addition, the third group of inventions will be described with reference to Figs. 7-10 Method embodiment. As shown in Figure 7, 1,000 kg of waste (block 7 00) containing 220 kg of ash is fed to a grid-based system (block 7 002) and its combustion method is such that the weight of the resulting combustion residue is 2 5 to 7 5% becomes fully sintered bottom ash, This combustion produces 800 kilograms of flue gas with -30- (24) (24) 200304535 and 300 kilograms of combustion residues. These residues are sent to a wet drain (block 7 0 6), Under humidification, 3 1 5 kg of residue or bottom ash is removed (box 7 0 8), The removed residue is now mechanically separated, The screening size is 8 mm (box 7 1 0). This program divides 2 15 kg of combustion residue into a main component with a particle size greater than 8 (block 7 1 2) and a subdivided amount and a subdivided amount with a particle size less than 8 min (block 7 14). The bottom ash consisting of coarse and oversized particles with a particle size greater than 8 min is humidified (block 7 1 6). In this procedure, 100 litres of water taken out of the wet drainer washes the bottom ash, As a result, 15 kg of fine ingredients with a particle size of less than 8 gram were washed out. In fact, the bottom ash is washed with a strainer that allows 8 mm or less to pass through. The water that has been used to wash the bottom ash is returned to the wet discharger with the subdivision and subdivision, The washed bottom ash is taken out and can be used immediately in the reuse program. Such as paving (block 7 1 8). The 100-kilogram subdivision removed by screening is generally returned to the grid-based system for further sintering. however, The amount of subdivision can also be used in other programs (block 7 2 0). 40 litres of make-up or fresh water is added to make up for the loss of water in the wet drain, This is because combustion residues naturally carry water out when they are removed from the wet exhaust. The above program can also be modified as shown in Figure 8, In this embodiment, After the main component with a particle size larger than 8 wakes up, it is rinsed with fresh water (block 7 2 2) (block 7 2 4). In particular, In order to remove the carrier composition formed by humidifying the water from the wet discharger, Add 200 litres of fresh water to the main component of 200 kg. 40 liters of flushing water is used for flue gas scrubbing (block 7 2 6) or other disposal treatment, The other 40 males -31-(25) (25) 200304535 kg are returned to the wet drain as make-up water for water loss, The bottom ash washed in this way can be introduced into other reuse programs. FIG. 9 is another embodiment of a program of the third group of inventions. In this embodiment, 100 kg of waste containing 2 200 kg of ash (box 9 0 0) is sent to a grid-based system (box 9 0 2), This combustion process produces 800 kg of flue gas (box 904) and 320 kg of combustion residues. These residues are forwarded to a wet drain (box 906). 3 3 6 kg of combustion residues are taken out of the wet exhaust, The weight increase is due to the fine particles contained in the bottom ash wash water returning to the wet drain. 40 litres of water are added to the wet drain to replenish the loss of water, 3 3 6 kg of bottom ash or combustion residue is sent to a filter, The strainer allows a fraction of 32 mm to pass through (block 908). Large-size components with a particle size greater than 32 imn are first sent to a metal separator (box 9 1 0), The separated bottom ash is conveyed to a crusher (block 9 12) which produces a bottom ash with a particle size of about 8 mm. The crushed bottom ash is conveyed to another filter (block 9 1 4) which allows a particle size of 8 imn to pass through. 100 kilograms of bottom ash or combustion residue with a particle size of less than 8 mm are removed by mechanical separation procedures, And it's better to go back to the grid-based system, The bottom ash is disposed of or further processed (block 9 1 5), The remaining coarse component is sent to a metal separator (block 9 1 6). The metal components removed by the metal separator and the metal components separated by the metal separation step described above are collected and subjected to a humidification treatment (block 9 1 8), With humidification, The ash particles adhering to the metal component are washed away, As a result, 20 kg of ferrous and non-ferrous metals were used for the reuse process (box 9 2 0), Removed ground ash or coarse component of metal (particle size 8 ~ 3 2 with -32- (26) (26) 200304535) weight is 2 1 5 kg (box 9 2 2), 60 kg of coarse weight is sent to a crusher (box 9 2 4), Particle size reduced to less than 2 mm, After crushing, The crushed portion is mixed with 1 5 5 kg of unmilled coarse portion, And the mixture is humidified with a filter that allows a particle size of 2 minutes to pass through (block 9 2 6), 100 litres of wash water required for humidification are supplied by a wet drain Humidification treatment produces a base ash with a particle size of 8 ~ 3 2 legs and a subdivision of 4 5 kg with a particle size of 2 ~ 8mm. These two components are used in the reuse program (block 9 2 8), on the other hand , Subdivisions with a particle size of less than 2 mm removed by the humidification process are returned to the wet discharger. The working flowchart in FIG. 10 is a basic change of the embodiment in FIG. 7. Where a precipitant that dissolves metals is used, The precipitant is injected into the wet discharger to reduce the lead concentration in the water in the discharger from 2 mg / L to 0. 〇5 mg / L (box 7 2), this precipitant will reduce the lead dissolved in about 20 liters of bottom ash water that has humidified 200 kg of bottom ash to 1 mg, 400 kg of lead in In the flue gas produced by the combustion process (block 70 2). In the mechanical separation procedure of a sieve that allows a particle size of 8 nun to pass (block 7 10), out of 400 grams of lead, 200 grams of lead is left after being washed and sent to the reuse program. In 200 kg of bottom ash (block 7 1 2), on the other hand, 200 grams of lead and a fine particle size smaller than 8 mm (block 7 1 4) are returned to the grid-based system (block 7 0). 6) As described above, according to the first group of inventions of the present invention, it provides a method 'where a fully sintered bottom ash of a desired quality can be obtained without using downstream melting -33- (27) (27) 200304535 or glass化 Units. Moreover, according to the second group of inventions of the present invention, it provides a method in which the bottom ash content of good quality can be separated, avoiding the disadvantages of dust flying and problems caused by entering air from the furnace, and reducing further waste of water. In addition, the third group of inventions of the present invention provides a method in which the combustion process can be adjusted to obtain a fully sintered bottom ash of a desired quality without the need for a downstream melting or vitrification unit, avoiding the disadvantages of avoiding dust flying with minimal equipment and Problems caused by air entering from the furnace also reduce further waste of water. Although the present invention has been described with embodiments, it is not limited to this. For those skilled in the art, all modifications, changes and additions can be easily made without departing from the technical scope of the present invention. [Brief Description of the Drawings] FIG. 1 is a working flowchart of an embodiment of the first group of inventive methods. FIG. 2 is a working flowchart of another embodiment of the first group of inventive methods. FIG. 3 is a working flowchart of an embodiment of the second group of inventive methods. FIG. 4 is a working flowchart of another embodiment of the second group of inventive methods. FIG. 5 is a working flowchart of another embodiment of the second group of inventive methods. FIG. 6 is a working flowchart of another embodiment of the second group of inventive methods. FIG. 7 is a working flowchart of an embodiment of the third group of inventive methods. FIG. 8 is a working flowchart of another embodiment of the third group of inventive methods. FIG. 9 is a working flowchart of another embodiment of the third group of inventive methods. FIG. 10 is a working flowchart of another embodiment of the third group of inventive methods. -34-