201244808 六、發明說明： 【發明所屬技術領域3 發明領域 本發明係有關於一種處理從氣分流設備排出之氣體的 裝置及方法，該氣分流設備係藉由從水泥窯之窯尾起至最 下段旋風器之間之窯排氣流路’將燃燒氣體的一部分予以 抽氣並除去氣者。 t先前系好】 發明背景 習知，在成為引起水泥製造設備中之預熱器阻塞等問 題之原因的氣、硫、鹼等之中係著眼於尤為問題之氣，而 使用一種藉由從水泥窯之窯尾起至最下段旋風器之間之窯 排氣流路，來將燃燒氣體的一部分予以抽氣並除去氣的氣 分流設備。 如第3圖顯示，氣分流設備具備：探測器53，藉由從水 泥窯52之窯尾起至最下段旋風器（未圖示）之間之窯排氣流 路，將燃燒氣體的一部分予以抽氣；冷卻風扇54，對探測 器53内供給冷風以使抽氣氣體G1急冷；旋風器55，係作為 將抽氣氣體G1中之塵所含粗粉D1分離的分級機；冷卻器 56，冷卻包含從旋風器55所排出之微粉D2的抽氣氣體G2 ; 冷卻風扇57，對冷卻器56供給冷風，袋渡器58，將以冷卻 器56所冷卻之抽氣氣體G2中之塵之微粉D2進行集塵者；塵 槽59，回收從冷卻器56及袋濾器58所排出之微粉D2 ;溶解 槽60，使來自塵槽59之微粉D2溶解於水；及固液分離裝置 3 201244808 61 ’將來自溶解槽60之泥漿S1予以固液分離而固液分離成 水洗泥餅C與排水L。又，前述氣分流設備會將經固液分離 之水洗泥餅C及排水處理後的殘渣R返回至窯系，並於排水 處理後將排水L予以排放。 【發明内容】 發明概要 發明欲解決之課題 在上述氯分流設備51中，由於袋濾器58之排氣G3中含 有多量的S02，因此無法直接將該排氣G3釋出到系外而是 透過排氣風扇（未圖示）返回至窯系。此時，若使排氣G3返 回至誘導水泥窯52排氣的風扇（IDF)出口側，則有使從煙囪 釋出到大氣中之排氣中的S02增加之問題。又，若將上述排 氣G3返回至附設於水泥窯52之預熱器，則有招致水泥燒成 系之熱損失增加及熟料生產量降低，且引起因硫含量濃縮 所造成的塗料問題等之問題。 爰此，本發明係有鑑於上述習知技術中之問題點所進 行者，其目的在於：在不使水泥燒成系之熱損失增加的情 況下確保水泥燒成系之穩定運轉的同時，以低成本處理從 氣分流設備排出之氣體（氯分流排氣）。 用以解決課題之機構 為了遠成上述目的，本發明係一種氣分流排氣之處理 裝置，其係附設在氣分流設備，該氣分流設備係將燃燒氣 體的一部分一邊冷卻並一邊從水泥窯之窯尾起至最下段旋 風器之間的窯排氣流路抽氣，且從該抽氣氣體回收氣分流 4 201244808 塵，又，前述氣分流排氣之處理裝置之特徵在於具備：第1 溶解槽，添加鹼性試劑於前述所回收之氣分流塵中並進行 泥漿化；固液分離裝置，將已藉該第1溶解槽生成之泥漿進 行固液分離；第2溶解槽，使已藉該固液分離裝置生成之泥 餅再溶解；及脫硫塔，使已藉前述第2溶解槽生成之再溶解 後泥漿接觸該氯分流設備之排氣，以進行該排氣之脫硫。 而且，依據本發明，由於係藉由於氣分流塵中添加鹼 性試劑使氣分流塵中所含CaCl2及CaC03變化成Ca(OH)2，再 將該Ca(OH)2利用於氣分流設備之排氣脫硫，因此可有效地 將氣分流塵中所含鈣成分利用於脫硫，並可在未招致水泥 燒成系之熱損失增加的情況下確保水泥燒成系之穩定運轉 的同時，以低成本處理氣分流排氣。 又，由於會在固液分離裝置中除去泥漿中之鉀成分及 氣成分，因此再溶解後的泥漿之氯含有率很低而可將成為 鏽皮問題之原因的石膏溶解抑制到最低限度，且可抑制阻 礙回收物之有效利用的鉀石膏(K2Ca(S04)2)等之生成。 還有，由於CaCl2會溶解於水中，因此若不使其變化成 Ca(OH)2 ’則會在後段中含於所回收之工業鹽中而成為降低 工業鹽純度的主要因素，但由於有藉由與鹼性試劑之反應 使其變化成難溶解於水之Ca(OH)2，因此亦可防止工業鹽純 度之降低。 又，藉由鹼性試劑之添加，氣分流塵中所含重金屬之 中’錯(Pb)與硒(Se)會多量含於濾液側，因而在後段可使用 硫化劑等回收船’而础則即便含在所回收之工業鹽中亦不 201244808 成問題，故而可從氣分流塵有效率地除去鉛及硒。 在上述氣分流排氣之處理裝置中可具備：第2固液分離 裝置，用以將自前述脫硫塔排出之泥漿進行固液分離；及 供給機構，用以將已藉該第2固液分離裝置固液分離之濾液 供給至前述第2溶解槽。藉此，可循環使用所固液分離之濾 液進行有效利用，並可於泥餅側回收石膏。 在上述氣分流排氣之處理裝置中可具備調整槽，該調 整槽係於已藉前述第1固液分離裝置所固液分離之濾液中 添加硫化劑及pH調整劑，以使該濾液中所含重金屬不溶解 化。藉此，可使船等不溶解化而在後段有效率地進行回收。 在上述氣分流排氣之處理裝置中可具備第3固液分離 裝置，用以將自前述調整槽所排出之濾液予以固液分離。 藉此，可於泥餅側回收鉛等重金屬。 在上述氣分流排氣之處理裝置中可具備鹽回收裝置， 還可具備氣-氣加熱器，前述鹽回收裝置係從已自前述第3 固液分離裝置排出之濾液回收鹽，而前述氣-氣加熱器係將 自前述抽氣氣體回收之熱利用於前述鹽回收裝置中之鹽回 收。藉此，可有效地利用氣分流排氣所保有之熱且可將鹽 回收。 前述氣-氣加熱器可從集塵前述抽氣氣體之高溫集塵 機的排氣中進行熱回收，藉由從已除塵之高溫氣體進行熱 回收，可提升熱效率。 又，本發明係一種氣分流排氣之處理方法，係在一氣 分流設備中，該處理方法之特徵在於：添加鹼性試劑於前 201244808 述所回收之氯分流塵中並進行泥漿化後，使該泥毁脫水， 使所獲得之泥餅再溶解，使該泥餅已再溶解之泥漿接觸該 氣分流設備之排氣以進行該排氣之脫硫。又，前述氣分流 設備係將燃燒氣體的一部^ —邊冷卻並一邊從水泥寞之寞 尾起至最下段旋風器之間的窯排氣流路抽氣，且從該抽氣 氣體回收亂分流塵。依據本發明，與上述發明同樣地可有 效地將氣分流塵中所含鈣成分利用於脫硫以處理氣分流排 氣，並可將成為鏽皮問題原因的石膏之溶解抑制在最低限 度’且可抑制阻礙回收物之有效利用的卸石膏(K2Ca(s〇4)2) 等之生成，而且，亦可防止回收之工業鹽純度的降低，還 可從氣分流塵有效率地除去鉛及硒。 在上述氣分流排氣之處理方法中，可將前述泥漿之pH 調整為13以上且14以下，而在該pH區域中可有效率地使氣 分流塵中所含CaCl2及CaC03變成Ca(〇H)2。 發明效果 如以上，依據本發明，可在未使水泥燒成系之熱損失 增加的情’况下確保水泥燒成系之穩定運轉的同時，以低成 本處理氣分流排氣。 圖式簡單說明 第1圖係顯示本發明之氣分流排氣之處理裝置之第1實 施形態的全體構成圖。 第2圖係顯示本發明之氣分流排氣之處理裝置之第2實 施形態的全體構成圖。 第3圖係顯示習知之氣分流設備的全體構成圖。 201244808 【實施冷式】 用以實施發明之形態 接下來參照圖式説明用以實施本發明之形態。 第1圖係顯示設有本發明之氣分流排氣之處理裝置之 第1實施形態的氣分流設備，該氣分流設備碌以下述元件 等構成：探測器3，係藉由從水泥寒2之熏尾起至最下段旋 風器（未圖示）之間之熏排氣流路，以來自冷卻風扇4、5之冷 風’將燃燒氣體的一部分G—邊冷卻炎一邊抽氣；旋風器6， 用以將以探測器3抽氣之抽氣氣體G丨中所含之塵的粗粉D ι 分離；冷卻器7，用以將從旋風器6排出之包含微粉〇2的抽 氣氣體G2冷卻；袋濾器8，將來自冷卻器7之抽氣氣體〇3進 行集塵；脫硫塔11，進行從袋濾器8透過風扇10所供給之排 氣G4的脫硫處理；塵槽9 ’用以貯留從冷卻器7及袋濾器8 所排出之塵D5(D3+D4);第1溶解槽12，添加驗性試劑至從 塵槽9排出之塵（氣分流塵)D6中並進行泥漿化；第！固液分 離裝置13 ’將從第1溶解槽12所排出之泥漿S1予以固液分 離；第2固液分離裝置15，將於脫硫塔11產生之泥漿S3予以 固液分離；第2溶解槽14，使從第1固液分離裝置13所排出 之泥餅C1溶解至來自第2固液分離裝置15之濾液L2(循環水 CW);調整槽16，用以添加硫化劑或pH調整劑於從第1固液 分離裝置13所排出之濾液L1 ;及第3固液分離裝置17，將從 調整槽16所排出之濾液L3予以固液分離。有關探測器3〜塵 槽9之構成，除使用2架的冷卻風扇4、5來冷卻燃燒氣體G 之點以外，與習知的氯分流設備為同樣構成’故省略詳細 201244808 説明。 第1溶解槽12係為了利用水（或溫水）將來自塵槽9之塵 D6予以泥漿化，並且添加NaOH等驗性試劑使塵D6中所含 CaCl2及CaC〇3變化成Ca(OH)2而設置。 第1固液分離裝置13係用以將從第1溶解槽12所排出之 泥漿S1予以固液分離而設置。經固液分離之泥餅c 1係供給 至第2溶解槽14，濾液L1則供給至調整槽16。 第2溶解槽14係用以使從第1固液分離裝置13所排出之 泥餅C1再溶解而設置’已使泥餅c 1溶解於循環水中之 泥漿S2在脫硫塔11中係利用於袋濾器8之排氣G4的脫硫。 脫硫塔11係用以利用從第2溶解槽14所供給之泥衆 S2，使從袋濾器8透過風扇10所供給之排氣脫硫而設置。 包含藉由脫硫所生成之二水合石膏的泥漿S3係返回至第2 固液分離裝置15 ’所脫硫之排氣G5則返回至水泥窯2之排氣 系。 第2固液分離裝置15係用以將從脫硫塔u供給之泥漿 S3予以g]液分離而設置，經固液分離之濾液[2會作為循環 水CW而在第2溶解槽14再利用。另一方面，·固液分離 之泥餅C2側則有二水合石膏Gy回收。 6周整槽16係用以於從第丄固液分離裝置13所排出之渡 液U中添加NaSH等硫化劑或pH調整劑使船等重金屬不溶 解化而設置。作為pH調整劑，可利用Na〇H、Ca(〇H)2、㈤、 Mg(OH)2、還有硫酸等。 第3固液刀離褒置17係用以將從調整槽ι6所排出之遽 201244808 予以固液分離而設置，可從經固液分離之濾液L4藉由 鹽回收社gg 裝置回收工業鹽，亦邛進行排水處理。又，於經固 液刀離之泥餅C3側有船等重金屬回收。 接下來，參照第1圖説明具有上述構成之氣分流設備1 之動作。 长將從水泥窯2之寞尾起至最下段旋風器之間之窯排氣 l路中之燃燒氣體的一部分G，一邊藉由探測器3抽氣一邊 藉由來自冷卻風扇4、5之冷風進行冷卻。藉此，可生成氣 化合物之微晶。該氣化合物之微晶係位置偏在抽氣氣體G1 所含之塵的微粉側，因此可將藉旋風器6分級之粗粉D1作為 艮泥原料而返回至附設於水泥窯2中之預熱器等。 ，、將包含藉由旋風器6分離之微粉D2的抽氣氣體G2導入 j部器7，以進行抽氣氣體G2與媒體之熱交換。再將藉由熱 交換所冷卻之抽氣氣體⑺導人錢H8，並在錢器8中將 抽氣氣體G3巾所含之塵附㈣收。在袋濾⑼所回收之 塵D4係與從冷卻器7所排出之細一起作為塵出而暫時貯 留於塵槽9，再作為塵〇6導入至第丨溶解槽12。 將導入至第1溶解槽12中之塵D6在第丨溶解槽12内與水 (或溫水)及NaOH等驗性試航合，以生錢細。在此， 將第1溶解槽12内之PH調整成13.5±〇·5。藉此，應D6中所含 之CaCl2及CaC03可與驗性試劑起反應而生成Ca(〇i^，該等 的妈成分可有效地_錢段之脫硫仙巾之脫硫。而， 驗性試劑中，除NaOH以外亦可使用k〇h等。 又，由於㈤2會溶解於水，因此若未與上述驗性試劑 201244808 起反應變化成Ca(OH)2，將會含於後段之第3固液分離裝置 17之濾液L4中而包含在所回收之工業鹽中。其結果會使工 業鹽純度降低，因此’與上述鹼性試劑之反應亦可發揮防 止工業鹽純度之降低的效果。 此外，藉由上述驗性試劑之添加，塵D6中所含之重金 屬中’錯(Pb)與砸(Se)會分別以第1圖中顯示之比例分離至 濾液L1與濾液L2中且多數供給至調整槽16側，因此藉由後 段之s周整槽16及第3固液分離裝置17可有效率地回收鉛。 而，硒雖然很少藉由調整槽16及第3固液分離裝置17而回 收，但即便含在所回收之工業鹽中亦不成問題，因此可有 效率地從塵D6除去。另—方面，泥餅C1中所含之鎘、銅、 鋅、鉛、硒等不溶金屬及氟化合物最終會在第2固液分離裝 置15中與石膏Gy—同排出系外。 接下來’藉由第1固液分離裝置13將從第1溶解槽12所 排出之泥漿si予以固液分離，一邊將泥漿S1進行固液分離 -邊將固液分離而獲得的泥餅予以水洗，#以除去氣成 为。將已除去氣成分之泥餅C1供給至第2溶解槽14而再溶解 的泥毁S2 ’供給至脫硫塔丨丨以利用於脫硫。@，脫硫後的 排氣G5係導入至水泥窯2之排氣系。 在此，存於上述再溶解之泥漿S2中的Ca(〇Hh會在脫硫 塔11中與袋濾Θ 8之排氣(34中所含之s〇2起反應而轉換成 一水合石膏(CaS04 · 2H2〇)。此時，已在第1固液分離裝置 13中除去鉀成分與氣成分，因此將泥㈣丨再溶解之泥聚％ 的氣含有率很低’可將成為數問題原因的^膏之溶解抑 201244808 制在最低限度，並且可抑制鉀石膏（K2Ca(S〇4)2)之生成。 而，一旦鉀石膏添加至水泥中，將會影響水泥品質一尤其 是強度一因此必須抑制其生成。 接下來，藉由第2固液分離裝置15，可將從脫硫塔11所 排出之泥漿S3予以固液分離，並將於泥餅C2側獲得之二水 合石膏Gy以水泥磨機與水泥熟料一起粉碎而供於水泥製 造。另一方面，可將經分離之濾液L2作為循環水CW再利用 於第2溶解槽14中之泥漿S2之生成。 另一方面，將藉由第1固液分離裝置13經固液分離之濾 液L1供給至調整槽16，並於濾液L1添加NaSH等硫化劑或 pH調整劑使鉛等重金屬沉澱化，再以第3固液分離裝置17 進行固液分離後，於泥餅C3側回收重金屬。而，若有必要， 將濾液L3供給至第3固液分離裝置17之前，可添加濾過助 劑。又，可從以第3固液分離裝置17經固液分離之濾液L4 回收工業鹽，亦可將濾液L4於排水處理後加以排放。回收 工業鹽時，如上述已使CaCl2變化成Ca(OH)2，因此可獲得 低鈣濃度且KC1含有率高的工業鹽。 接下來，參照第2圖説明本發明之氣分流排氣之處理裝 置的第2實施形態。 該氣分流設備31之特徵在於具備高溫集塵機32來替代 氯分流設備1之冷卻器7及袋濾器8，並於高溫集塵機32之後 段配置氣-氣加熱器33,且將以氣-氣加熱器33所升溫之大氣 利用於鹽回收。有關氯分流設備31之其他構成要素皆與第1 圖中所示之氣分流設備1相同，故而賦予同一參照編號並省 12 201244808 略有關該等之説明。 例如，高溫集塵機32具備陶瓷濾器，為具有至9〇(rc左 右為止之耐熱性的耐熱型麟ϋ、或具有雜性之高温處 理型電集塵機，係在未將包含從旋風器6所排出之微粉d2 的抽氣氣體G2冷卻的情況下進行集塵，然後將所集塵之慶 (氣分流塵)D3供給至塵槽9。 现-軋加熱器33係用以藉由從高溫集塵機32所排出之 抽氣氣體G3將從周圍所納入之空氣以加熱再將以氣-氣加 熱器33所加熱之高溫空氣A2利用於後段之鹽回收而設置。 又，藉由與空氣A2之熱交換，可進行在脫硫塔⑴口以脫硫 之排氣G4的溫度調整而抑制固結之產生。此外，亦可將以 氣-氣加熱器33所回收之熱利用於脫硫塔11之排氣G5之升 溫。 藉由上述構成’可將包含藉旋風器6分離之微粉D2的抽 氣氣體G2導人兩溫集塵機32後，在高溫集塵機32中回收抽 氣氣體G2中所含之塵D2，而從高溫集塵機32所排出之塵〇3 會暫時貝了留於塵槽9再作為塵〇4而導入至第丨溶解槽12。 又，從周圍所納入之空氣八丨及高溫集塵機32之排氣G3被導 入氣-氣加熱器33中且在兩者間進行熱交換以後，高溫空氣 A2會被利用於鹽回收，而從氣-氣加熱器^所排出之排氣G4 則會在導人脫鱗11後脫硫。其料程減分流設備1之情 況相同。 如以上，本實施形態中之氯分流排氣之處理裝置與第1 實施形&、發揮同樣的效果的同時，可將氣分流排氣之顯熱 13 201244808 利用於鹽回收，藉此可達到降低鹽回收之成本等。 又，在上述實施形態中，雖就於溶解槽12使塵D6溶解 之情況加以説明，然當鈣成分不足時，亦可分餾藉旋風器6 分離之粗粉D1，使其溶解至溶解槽12或溶解槽14中，藉以 補充妈成分。 C圖式簡單說明3 第1圖係顯示本發明之氯分流排氣之處理裝置之第1實 施形態的全體構成圖。 第2圖係顯示本發明之氣分流排氣之處理裝置之第2實 施形態的全體構成圖。 第3圖係顯示習知之氣分流設備的全體構成圖。 【主要元件符號說明】 1、31、51…氣分流設備 14…第2溶解槽 2、52…水泥窯 15…第2固液分離裝置 3、53…探測器 16…調整槽 4、5、54、57".•冷卻風扇 17…第3固液分離裝置 6、55…旋風器 32…高溫集塵機 7、56…冷卻器 33…氣-氣加熱器 8、58…袋濾器 60…溶解槽 9、59…塵槽 61…固液分離裝置 10…風扇 A1…空氣 11…脫硫塔 A2 · · ·向溫空氣 12…第1溶解槽 C…水洗泥餅 13…第1固液分離裝置 Cl、C2、C3.··泥餅 14 201244808 CW…循環水 G…燃燒氣體的一部分 D1…粗粉 Gl、G2、G3…抽氣氣體 D2···微粉 G3、G4、G5…排氣 D3、D4、D5.··塵 R…殘渣 D3、D6···塵(氣分流塵） SI、S2、S3".泥漿 L···排水 U、L2、L3、L4.·.濾液 Gy…石膏(二水合石膏） 15201244808 VI. Description of the Invention: [Technical Field of the Invention] FIELD OF THE INVENTION The present invention relates to an apparatus and method for treating a gas discharged from a gas distribution device by using a kiln from a kiln to a lowermost stage The kiln exhaust flow path between the cyclones 'extracts a part of the combustion gas and removes the gas. BACKGROUND OF THE INVENTION It is known that gas, sulfur, alkali, etc., which are causes of problems such as blockage of a preheater in a cement manufacturing facility, are particularly problematic, and a cement is used. A kiln exhaust flow path from the kiln kiln to the lowermost cyclone to extract a part of the combustion gas and remove the gas from the gas splitting device. As shown in Fig. 3, the gas splitting device is provided with a detector 53 for supplying a part of the combustion gas from the kiln exhaust flow path from the kiln end of the cement kiln 52 to the lowermost cyclone (not shown). Pumping; cooling fan 54, supplying cold air to the detector 53 to quench the exhaust gas G1; the cyclone 55 is used as a classifier for separating the coarse powder D1 contained in the dust in the exhaust gas G1; the cooler 56, The pumping gas G2 containing the fine powder D2 discharged from the cyclone 55 is cooled; the cooling fan 57 supplies cold air to the cooler 56, and the bag feeder 58 picks up the fine powder of the dust in the pumping gas G2 cooled by the cooler 56. D2 carries out the dust collector; the dust tank 59 recovers the fine powder D2 discharged from the cooler 56 and the bag filter 58; the dissolution tank 60 dissolves the fine powder D2 from the dust tank 59 in the water; and the solid-liquid separation device 3 201244808 61 ' The slurry S1 from the dissolution tank 60 is subjected to solid-liquid separation and solid-liquid separation into a washed mud cake C and a drain water L. Further, the gas splitting device returns the washed mud cake C and the residue R after the drain treatment to the kiln system, and discharges the drain water L after the drain treatment. SUMMARY OF THE INVENTION PROBLEMS TO BE SOLVED BY THE INVENTION In the chlorine splitting device 51, since the exhaust gas G3 of the bag filter 58 contains a large amount of S02, it is not possible to directly discharge the exhaust gas G3 to the outside of the system. The air fan (not shown) returns to the kiln system. At this time, if the exhaust gas G3 is returned to the outlet side of the fan (IDF) that induces the exhaust of the cement kiln 52, there is a problem that the amount of S02 in the exhaust gas released from the chimney to the atmosphere is increased. Further, when the exhaust gas G3 is returned to the preheater attached to the cement kiln 52, the heat loss of the cement firing system is increased and the clinker production amount is lowered, and the coating problem caused by the concentration of sulfur is caused. The problem. Accordingly, the present invention has been made in view of the above problems in the prior art, and an object thereof is to ensure stable operation of a cement firing system without increasing the heat loss of the cement firing system. The gas discharged from the gas splitting device (chlorine split exhaust) is processed at a low cost. In order to achieve the above object, the present invention is directed to a gas split exhaust gas treatment device which is attached to a gas splitting device which cools a part of the combustion gas while being cooled from the cement kiln. The kiln exhaust flow path from the kiln end to the lowermost cyclone is evacuated, and the gas is diverted from the exhaust gas 4 201244808 dust. Further, the gas split exhaust gas treatment device is characterized by: first dissolution a tank, adding an alkaline reagent to the gas recovered by the foregoing gas separation and sizing; the solid-liquid separation device solid-liquid separation of the slurry formed by the first dissolution tank; and the second dissolution tank The mud cake formed by the solid-liquid separation device is redissolved; and the desulfurization tower causes the mud which has been dissolved by the second dissolution tank to contact the exhaust gas of the chlorine branching device to perform desulfurization of the exhaust gas. Moreover, according to the present invention, since CaCl2 and CaC03 contained in the gas-distributed dust are changed to Ca(OH)2 by adding an alkaline agent to the gas-distributed dust, the Ca(OH)2 is used in the gas-splitting device. Since the exhaust gas is desulfurized, the calcium component contained in the gas-distributed dust can be effectively utilized for desulfurization, and the stable operation of the cement-fired system can be ensured without increasing the heat loss of the cement-fired system. The gas split exhaust gas is treated at a low cost. Further, since the potassium component and the gas component in the slurry are removed in the solid-liquid separation device, the chlorine content of the re-dissolved slurry is low, and the gypsum dissolution which is a cause of the scale problem can be minimized. It is possible to suppress the formation of potassium gypsum (K2Ca(S04)2) or the like which hinders efficient use of the recovered material. In addition, since CaCl2 is dissolved in water, if it is not changed to Ca(OH)2', it will be contained in the recovered industrial salt in the latter stage, which becomes a major factor in reducing the purity of industrial salt, but it is borrowed. It is changed from a reaction with an alkaline reagent to Ca(OH)2 which is hardly soluble in water, so that the purity of the industrial salt can also be prevented from being lowered. Further, by the addition of the alkaline agent, the amount of "wrong" (Pb) and selenium (Se) contained in the gas-distributed dust is contained in the filtrate side, so that a recovery vessel such as a vulcanizing agent can be used in the latter stage. Even if it is contained in the recovered industrial salt, it is not a problem with 201244808. Therefore, lead and selenium can be efficiently removed from the gas-distributed dust. The gas separation and exhaust gas treatment device may include: a second solid-liquid separation device for solid-liquid separation of the slurry discharged from the desulfurization tower; and a supply mechanism for borrowing the second solid liquid The filtrate of the solid-liquid separation of the separation device is supplied to the second dissolution tank. Thereby, the solid-liquid separation filtrate can be recycled for efficient use, and the gypsum can be recovered on the mud cake side. The treatment device for the gas-distributed exhaust gas may include an adjustment tank for adding a vulcanizing agent and a pH adjuster to the filtrate which has been solid-liquid separated by the first solid-liquid separation device, so that the filtrate is contained in the filtrate. Contains heavy metals that do not dissolve. Thereby, the ship or the like can be insoluble and efficiently recovered in the subsequent stage. The gas separation and exhaust gas treatment device may include a third solid-liquid separation device for solid-liquid separation of the filtrate discharged from the adjustment tank. Thereby, heavy metals such as lead can be recovered on the mud cake side. The gas separation and exhaust gas treatment device may include a salt recovery device, and may further include a gas-gas heater, wherein the salt recovery device recovers salt from the filtrate discharged from the third solid-liquid separation device, and the gas- The gas heater utilizes the heat recovered from the exhaust gas described above for salt recovery in the aforementioned salt recovery device. Thereby, the heat retained by the gas split exhaust gas can be effectively utilized and the salt can be recovered. The gas-gas heater can perform heat recovery from the exhaust gas of the high-temperature dust collector that collects the exhaust gas, and the heat efficiency can be improved by heat recovery from the high-temperature gas that has been removed. Furthermore, the present invention is a method for treating a gas-distributed exhaust gas, which is characterized by a method of adding an alkaline reagent to the chlorine-removed dust recovered in the previous 201244808 and slurrying it, thereby making the method The mud is dewatered, the obtained mud cake is redissolved, and the mud which has been redissolved by the mud cake is contacted with the exhaust gas of the gas splitting device to perform desulfurization of the exhaust gas. Further, the gas splitting device cools one portion of the combustion gas and draws air from the kiln exhaust flow path between the tail of the cement concrete and the lowermost cyclone, and recovers the gas from the exhaust gas. Divide the dust. According to the present invention, in the same manner as the above-described invention, the calcium component contained in the gas-distributed dust can be effectively utilized for desulfurization to treat the gas-distributed exhaust gas, and the dissolution of gypsum which is a cause of the scale problem can be suppressed to a minimum. It can suppress the formation of unloading gypsum (K2Ca(s〇4)2) which hinders the effective use of the recovered material, and also prevent the reduction of the purity of the recovered industrial salt, and can efficiently remove lead and selenium from the gas-distributed dust. . In the method for treating the gas-distributed exhaust gas, the pH of the mud may be adjusted to 13 or more and 14 or less, and in the pH region, CaCl2 and CaC03 contained in the gas-distributed dust may be efficiently changed into Ca (〇H). )2. Advantageous Effects of Invention As described above, according to the present invention, it is possible to ensure the stable operation of the cement firing system without increasing the heat loss of the cement firing system, and to distribute the exhaust gas at a low cost. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a view showing the entire configuration of a first embodiment of a gas-splitting exhaust gas treating apparatus according to the present invention. Fig. 2 is a view showing the entire configuration of a second embodiment of the gas splitting and exhausting apparatus of the present invention. Fig. 3 is a view showing the overall configuration of a conventional gas distribution device. 201244808 [Implementation of the Cold Type] Mode for Carrying Out the Invention Next, the form for carrying out the invention will be described with reference to the drawings. Fig. 1 is a view showing a gas splitting apparatus according to a first embodiment of the present invention, which is provided with a gas splitting and exhausting apparatus according to the present invention. The gas distributing apparatus is constituted by the following elements: the detector 3 is cooled by cement. a smoked exhaust flow path from the tail to the lowermost cyclone (not shown), with a cold air from the cooling fans 4, 5 'cooling a part of the combustion gas G side while pumping; the cyclone 6, The coarse powder D ι for separating the dust contained in the pumping gas G 抽 pumped by the detector 3 is cooled; the cooler 7 is used for cooling the pumping gas G2 containing the fine powder 〇 2 discharged from the cyclone 6 The bag filter 8 collects the exhaust gas 〇3 from the cooler 7; the desulfurization tower 11 performs desulfurization treatment from the bag filter 8 through the exhaust gas G4 supplied from the fan 10; the dust tank 9' is used for The dust D5 (D3+D4) discharged from the cooler 7 and the bag filter 8 is stored; the first dissolution tank 12 is added to the dust (gas-distributed dust) D6 discharged from the dust tank 9 and mudd; The first! The solid-liquid separation device 13' solid-liquid separation of the slurry S1 discharged from the first dissolution tank 12, and the second solid-liquid separation device 15 for solid-liquid separation of the slurry S3 generated in the desulfurization tower 11; the second dissolution tank 14. The mud cake C1 discharged from the first solid-liquid separation device 13 is dissolved in the filtrate L2 (circulating water CW) from the second solid-liquid separation device 15, and the adjustment tank 16 is used to add a vulcanizing agent or a pH adjusting agent. The filtrate L1 discharged from the first solid-liquid separation device 13 and the third solid-liquid separation device 17 solid-liquid separation of the filtrate L3 discharged from the adjustment tank 16. The configuration of the detector 3 to the dust chamber 9 is the same as that of the conventional chlorine flow dividing device except that the cooling fans 4 and 5 are used to cool the combustion gas G. Therefore, the detailed description of 201244808 is omitted. The first dissolution tank 12 is for slurrying dust D6 from the dust tank 9 by water (or warm water), and adding an chlorinating reagent such as NaOH to change CaCl2 and CaC〇3 contained in the dust D6 into Ca(OH). 2 and set. The first solid-liquid separating device 13 is provided for solid-liquid separation of the slurry S1 discharged from the first dissolution tank 12. The mud cake c 1 subjected to solid-liquid separation is supplied to the second dissolution tank 14, and the filtrate L1 is supplied to the adjustment tank 16. The second dissolution tank 14 is configured to re-dissolve the mud cake C1 discharged from the first solid-liquid separation device 13 to provide a slurry S2 in which the mud cake c1 is dissolved in the circulating water, and is used in the desulfurization tower 11 Desulfurization of the exhaust gas G4 of the bag filter 8. The desulfurization tower 11 is provided to desulfurize the exhaust gas supplied from the bag filter 8 through the fan 10 by the mud S2 supplied from the second dissolution tank 14. The slurry S3 containing the dihydrate gypsum formed by the desulfurization is returned to the exhaust system G5 which is desulfurized by the second solid-liquid separation device 15', and is returned to the exhaust system of the cement kiln 2. The second solid-liquid separation device 15 is provided for separating the slurry S3 supplied from the desulfurization tower u into the liquid, and the solid-liquid separation filtrate [2 is reused as the circulating water CW in the second dissolution tank 14 . On the other hand, the solid cake separation side of the mud cake C2 is recovered by the dihydrate gypsum Gy. The 6-well tank 16 is provided by adding a vulcanizing agent such as NaSH or a pH adjuster to the liquid U discharged from the second solid-liquid separation device 13 to insolubilize heavy metals such as ships. As the pH adjuster, Na〇H, Ca(〇H) 2, (5), Mg(OH) 2, sulfuric acid, or the like can be used. The third solid-liquid knives are disposed 17 for the solid-liquid separation of the 遽201244808 discharged from the adjustment tank ι6, and the industrial salt can be recovered from the solid-liquid separated filtrate L4 by the salt recovery gg device.排水 Drainage treatment. In addition, heavy metals such as ships are recovered on the side of the C3 side of the mud cake. Next, the operation of the gas distributing device 1 having the above configuration will be described with reference to Fig. 1 . A portion G of the combustion gas in the kiln exhaust road from the tail of the cement kiln 2 to the lowermost cyclone is exhausted by the detector 3 while being cooled by the cooling fan 4, 5 Cool down. Thereby, crystallites of the gas compound can be produced. The microcrystalline system of the gas compound is located on the side of the fine powder of the dust contained in the exhaust gas G1, so that the coarse powder D1 classified by the cyclone 6 can be returned as a raw material of the mud to the preheater attached to the cement kiln 2. Wait. The pumping gas G2 including the fine powder D2 separated by the cyclone 6 is introduced into the j-part 7 to exchange heat between the pumping gas G2 and the medium. The pumping gas (7) cooled by the heat exchange is then introduced into the money H8, and the dust contained in the pumping gas G3 towel is attached (4) in the money unit 8. The dust D4 collected in the bag filter (9) is temporarily stored as dust in the dust tank 9 together with the fines discharged from the cooler 7, and introduced into the second dissolution tank 12 as dust mites 6. The dust D6 introduced into the first dissolution tank 12 is combined with water (or warm water) and NaOH in the second dissolution tank 12 to make the money fine. Here, the pH in the first dissolution tank 12 is adjusted to 13.5 ± 〇 · 5. Therefore, CaCl2 and CaC03 contained in D6 can react with the test reagent to form Ca (〇i^, which can effectively desulfurize the desulfurized scarves of the money segment. In the reagents, k〇h, etc. may be used in addition to NaOH. Since (5) 2 is dissolved in water, if it does not react with the above-mentioned test reagent 201244808 to change to Ca(OH)2, it will be included in the latter paragraph. (3) The filtrate L4 of the solid-liquid separation device 17 is contained in the recovered industrial salt. As a result, the purity of the industrial salt is lowered, so that the reaction with the above-mentioned alkaline agent can also exhibit the effect of preventing the decrease in the purity of the industrial salt. Further, by the addition of the above-mentioned test reagent, the "wb" and the ruthenium (Se) in the heavy metal contained in the dust D6 are separated into the filtrate L1 and the filtrate L2 in the ratio shown in Fig. 1, and the majority is supplied. Up to the side of the adjustment tank 16, the lead can be efficiently recovered by the s-well groove 16 and the third solid-liquid separation device 17 in the subsequent stage. However, the selenium is rarely used by the adjustment tank 16 and the third solid-liquid separation device 17 Recycling, but even if it is contained in the recovered industrial salt, it is not a problem, so it can be efficiently Dust D6 is removed. On the other hand, insoluble metals such as cadmium, copper, zinc, lead, and selenium contained in the cake C1 and the fluorine compound are eventually discharged out of the second solid-liquid separation device 15 together with the gypsum Gy. Then, the slurry si discharged from the first dissolution tank 12 is subjected to solid-liquid separation by the first solid-liquid separation device 13, and the mud cake obtained by separating the solid-liquid separation while the slurry S1 is subjected to solid-liquid separation is washed with water. In order to remove the gas, the mud cake C1 from which the gas component has been removed is supplied to the second dissolution tank 14, and the re-dissolved sludge S2' is supplied to the desulfurization tower for use in desulfurization. @, after desulfurization The exhaust gas G5 is introduced into the exhaust system of the cement kiln 2. Here, the Ca stored in the re-dissolved slurry S2 (the 〇Hh is in the desulfurization tower 11 and the venting of the bag filter 8 (34 The s〇2 is reacted and converted into monohydrate gypsum (CaS04 · 2H2 〇). At this time, the potassium component and the gas component have been removed in the first solid-liquid separation device 13, so that the mud (tetra) bismuth is re-dissolved. The gas content rate is very low', which can be the cause of several problems, the dissolution of the cream, 201244808 is at a minimum, and can inhibit potassium. The formation of the paste (K2Ca(S〇4)2). However, once the potassium gypsum is added to the cement, it will affect the quality of the cement, especially the strength, so it must be inhibited from formation. Next, by the second solid-liquid separation device 15. The slurry S3 discharged from the desulfurization tower 11 can be solid-liquid separated, and the dihydrate gypsum Gy obtained on the C2 side of the mud cake is pulverized together with the cement clinker for cement production. On the other hand, the separated filtrate L2 can be reused as the circulating water CW in the slurry S2 in the second dissolution tank 14. On the other hand, the filtrate L1 which is solid-liquid separated by the first solid-liquid separation device 13 is supplied. To the adjustment tank 16, a vulcanizing agent such as NaSH or a pH adjuster is added to the filtrate L1 to precipitate a heavy metal such as lead, and then solid-liquid separation is performed by the third solid-liquid separator 17, and then heavy metal is recovered on the mud cake C3 side. Further, if necessary, a filtrate aid may be added before the filtrate L3 is supplied to the third solid-liquid separator 17. Further, the industrial salt may be recovered from the filtrate L4 which is subjected to solid-liquid separation by the third solid-liquid separation device 17, or the filtrate L4 may be discharged after being subjected to drainage treatment. When the industrial salt is recovered, CaCl2 is changed to Ca(OH)2 as described above, so that an industrial salt having a low calcium concentration and a high KC1 content can be obtained. Next, a second embodiment of the treatment apparatus for the gas-distributed exhaust gas of the present invention will be described with reference to Fig. 2 . The gas distribution device 31 is characterized in that a high temperature dust collector 32 is provided instead of the cooler 7 and the bag filter 8 of the chlorine flow dividing device 1, and the gas-gas heater 33 is disposed in the subsequent stage of the high temperature dust collector 32, and the gas-gas heater is used. 33 elevated temperatures are used for salt recovery. The other components of the chlorine splitting device 31 are the same as those of the gas splitting device 1 shown in Fig. 1, and therefore the same reference numerals are assigned and the description is omitted 12 201244808. For example, the high-temperature dust collector 32 is provided with a ceramic filter, and is a heat-resistant type of arsenic having a heat resistance of about 9 〇 or a high-temperature treatment type electric dust collector having a miscellaneous property, and is not included in the cyclone 6 The dust extraction gas G2 of the fine powder d2 is cooled to collect dust, and then the collected dust (gas split dust) D3 is supplied to the dust tank 9. The present-rolling heater 33 is used to be used from the high-temperature dust collector 32. The discharged exhaust gas G3 is set by heating the air incorporated in the surroundings and then using the high-temperature air A2 heated by the gas-gas heater 33 for recovery of the salt in the latter stage. Further, by heat exchange with the air A2, The temperature adjustment of the desulfurization exhaust gas G4 at the port of the desulfurization tower (1) can be suppressed to suppress the occurrence of consolidation. Further, the heat recovered by the gas-gas heater 33 can be utilized for the exhaust gas of the desulfurization tower 11. According to the above configuration, the exhaust gas G2 including the fine powder D2 separated by the cyclone 6 can be guided to the two-stage dust collector 32, and the dust D2 contained in the exhaust gas G2 is recovered in the high-temperature dust collector 32, The dust mites 3 discharged from the high-temperature dust collector 32 will temporarily stay. The dust tank 9 is further introduced into the second dissolution tank 12 as the dust mites 4. Further, the air gossip incorporated from the surroundings and the exhaust gas G3 of the high-temperature dust collector 32 are introduced into the gas-gas heater 33 and are carried out between the two. After the heat exchange, the high-temperature air A2 is used for salt recovery, and the exhaust gas G4 discharged from the gas-gas heater ^ is desulfurized after the descaling step 11. The same is true for the material-reduction shunt device 1 As described above, the chlorine split exhaust gas treatment device of the present embodiment can achieve the same effect as the first embodiment and the same, and can utilize the sensible heat 13 201244808 of the gas split exhaust gas for salt recovery. Further, in the above embodiment, the case where the dust D6 is dissolved in the dissolution tank 12 will be described. However, when the calcium component is insufficient, the coarse powder D1 separated by the cyclone 6 may be fractionally distilled. It is dissolved in the dissolving tank 12 or the dissolving tank 14 to supplement the mating component. Brief Description of the Drawings 3 Fig. 1 is a view showing the entire configuration of the first embodiment of the chlorine shunting and exhausting apparatus of the present invention. Figure 2 shows the gas split exhaust of the present invention. The entire configuration of the second embodiment of the processing apparatus. Fig. 3 is a view showing the overall configuration of a conventional gas distributing device. [Description of main components] 1. 31, 51... gas distributing device 14... second dissolution tank 2 52...cement kiln 15...second solid-liquid separation device 3,53...detector 16...adjustment tank 4,5,54,57"•cooling fan 17...third solid-liquid separation device 6,55...cyclone 32... High-temperature dust collector 7, 56... cooler 33... gas-gas heater 8, 58... bag filter 60... dissolution tank 9, 59... dust tank 61... solid-liquid separation device 10... fan A1... air 11... desulfurization tower A2 · Warm air 12... First dissolution tank C... Washed mud cake 13... First solid-liquid separation device Cl, C2, C3. · Mud cake 14 201244808 CW... Circulating water G... Part of the combustion gas D1...Coarse powder Gl, G2, G3... exhaust gas D2···fine powder G3, G4, G5... exhaust D3, D4, D5.··dust R...residue D3, D6···dust (gas split dust) SI, S2 S3". Mud L···Drainage U, L2, L3, L4.·. Filtrate Gy...Gypsum (dihydrate gypsum) 15