200405823 (1) 玖、發明說明 【發明所屬之技術領域】 本發明有關於含鈣粉體之處理方法及裝置，特別是有 關於水洗處理焚化飛灰等含鈣粉體的方法及裝置。 【先前技術】 雖然近年來推展利用焚化飛灰等廢棄物的水泥原料化 # 等的再循環，不過，隨著廢棄物的處理量增加，挾帶進入 水泥窯的氯等揮發成份的量亦增加，構成引發水泥製造設 備中預熱器的閉塞等問題的原因。因此，在預先從焚化飛 灰等除去氯成份之後，用來作爲水泥原料。此際，利用水 溶性氯化合物容易溶於水的性質，在混合焚化飛灰等與 水，溶出氯之後，利用帶式過濾器等水洗設備，水洗除去 焚化飛灰所含水溶性氯化合物，此後，利用其作爲水泥原 料。 # 不過，於焚化飛灰中大多含有鈣，在水洗時，鈣會溶 解於水，從而出現積垢發生並成長於水洗設備內的情形。 若放置此積垢不管，會導致焚化飛灰的水洗脫氯處理效率 降低，有引起水洗設備運轉障礙之虞。特別是由於近年來 將大量熟石灰投入焚化都市垃圾等的焚化爐，以此作爲戴 奧辛對策，故容易發生碳酸鈣的積垢，期望有防止積垢所 造成障礙的因應措施。 【發明內容】 (2) 200405823 本發明是爲消除此種問題而提出之技術，其目的在於 提供可抑制積垢的成長，高效率進行焚化飛灰等含錦粉體 的水洗脫氯的方法及裝置。 本發明第1含鈣粉體之處理方法是於含鈣粉體溶解於 水後，進行固液分離的水洗方法，其在含鈣粉體溶解於水 時，添加二水石膏的結晶、氯副產塵粉及硫酸、二氧化碳 中任一個，析出錦。 p 且可在將二水石膏的結晶及氯副產塵粉的任一個與水 強行混合後，混合含鈣粉體於此混合液。又，亦可同時將 二水石膏的結晶及氯副產塵粉的任一個、水與含鈣粉體強 行混合。 更且，較佳地，藉由真空過濾析出鈣的溶解液，進行 固液分離，獲得濾餅，同時，使真空過濾之際發生的排氣 回流至濾餅上循環。 本發明第2含鈣粉體之處理方法是於含鈣粉體溶解於 φ水後進行固液分離的水洗方法，其於氣體吸收反應槽中對 流反應藉由水洗排水及分散手段微細化的二氧化碳，析出 水洗排水中的重金屬類，此後，於與氣體吸收反應槽形成 爲一體的脫氣槽中，自水洗排水脫氣。 且，分散手段具有彈性，藉由間歇吹入二氧化碳’可 除去分散手段的堵塞。 又，本發明第1含鈣粉體之處理裝置是於含鈣粉體溶 解於水後進行固液分離的水洗裝置，其具備將含鈣粉體與 水混合並溶解的混合槽，以及將二水石膏的結晶、氯副產 -6 - (3) 200405823 塵粉及硫酸、二氧化碳中任一個供至混合槽的供給手段。 且，就供給手段而言’可使用強行混合二水石膏的結 晶及氯副產塵粉中任一個與水的強行混合手段或同時強行 混合二水石膏的結晶及氯副產塵粉中任一個、水與含弼粉 體的強行混合手段’以及將強行混合手段所強行混合的混 合液供至混合槽的泵。 β 又，較佳地’進一步具備藉由真空過濾在混合槽中獲 ‘ φ 得的溶解液，于以固液分離，獲得濾餅的真空過濾裝置， φ 以及使自真空過濾裝置產生的排氣回流至真空過濾裝置內 的濾餅上而循環的循環手段。 本發明第2含鈣粉體之處理裝置是於含鈣粉體溶解於 水後進行固液分離的水洗裝置，其具備設有微細化並吹入 二氧化碳的分散手段，並對流反應水洗排水及二氧化碳， 析出水洗排水中的重金屬類的吸收反應槽，以及連通氣體 吸收反應槽，與氣體吸收反應槽形成爲一體，同時，自通 Φ過氣體吸收反應槽的水洗排水脫氣的脫氣槽。 φ 而且，分散手段具有彈性，亦可具備藉由間歇吹入來 自分散手段的二氧化碳，除去分散手段的堵塞的吹入控制 手段。於此情形下，較佳地，使用具有橡膠製分散板或橡 膠製分散管的手段作爲分散手段。 【實施方式】 「用以實施發明之最佳形態」 以下根據附圖說明本發明實施形態。 h 1 (4) 200405823 於第1圖中槪略顯示本發明實施形態的焚化飛灰處理 方法的流程。收容焚化飛灰的槽2、收容氯副產塵粉的槽 3以及收容二水石膏的槽4連接於混合槽1，同時，硫酸 槽6經由泵5連接於混合槽1。 又，作爲真空過濾裝置的帶式過濾器7經由淤漿泵 1 a連接於混合槽1。帶式過濾器7大致區分具備水封式真 空泵8、氣液分離槽9及1 0、真空托盤1 1及1 2、配置於 • 真空托盤1 1及1 2上方並且具有複數開口部的格網1 3、 於格網1 3上方移動的無端帶狀濾布丨4、圍遮格網1 3及 濾布1 4的帷幕部1 5、用來將淤漿S供至濾布！ 4上的供 給托盤1 6以及供給用來洗淨淤漿S的液體l的洗淨水托 盤17。 真空托盤11及12經由氣液分離槽9及1〇與真空泵 8連通。真空托盤1 1及1 2形成上方開口箱狀，可藉圖略 驅動手段’經由配置於導軌1 8上的複數滾子1 9，沿濾布 φ 1 4的移動方向，於導軌1 8上往復移動。 格網1 3是設在真空托盤1 1及1 2上方，於樹脂、金 屬等形成的板狀構件穿設複數開口部的構件。 濾布1 4形成於格網1 3上方移動的無端狀帶，藉複數 滾子20支持，沿箭頭方向旋轉。爲了洗淨濾布1 4，於過 濾部以外的部份配置噴射高壓水等的噴射噴嘴2 1。 真空泵8的出口配管22連接於帷幕部1 5，配置成使 真空泵8的排氣回流至帷幕部1 5內。 帷幕部1 5藉由圍覆格網1 3及濾布14上方，防止系 -8- (5) (5)200405823 統外的大氣滲入。 氣液分離槽9及1 0分別配置於真空托盤1 1及1 2與 真空泵8之間，氣液分離槽9進行從經由供給托盤1 6供 至格網1 3上的淤漿S分離的液體與氣体的氣液分離，氣 液分離槽1 〇進行從藉洗淨水洗淨的淤漿S分離的液體與 氣體的氣液分離。 於氣液分離槽1 〇進一步連接吸收反應·脫氣槽2 3。 其次，就本實施形態的焚化飛灰處理方法加以說明。 首先，將來自槽2的飛灰及水供至混合槽1，同時，添加 來自槽4的二水石膏於混合槽1，將其混合攪拌。藉此， 形成以二水石膏作爲種晶，於其周圍析出鈣成份並附著成 長的淤漿S。此時，將焚化飛灰與水的重量比例如定爲 1 : 5，爲了促進鈣成份附著、成長於種晶，較佳地’二水 石膏的添加量爲混合槽1內水的重量的〇 · 1〜1 〇 % ，水的溫 度爲20〜60°c。 爲了更有效附著、成長鈣成份於種晶，宜在混合槽1 中一面對水、焚化飛灰及二水石膏進行1 0到2 0分的緩慢 攪拌，一面將其貯存，較佳地，進行3 0分到1小時的緩 慢攪拌。 由於如此在焚化飛灰溶解於水時添加二水石膏’析出 錦，故將在固液分離之際帶式過濾器7的格網1 3堵塞等 不當情形抑至最小限度，同時’消除混合槽1中積垢的麻 煩。 且由於在添加二水石膏於混合槽1之際’難以使用例 (6) 200405823 如裙式進料器等每次添加少量’故亦可預先將二水石膏分 散於與溶解焚化飛灰的水相異的水中，此後’形成淤漿， 使用淤漿泵將其添加於混合槽1。 此後，沿箭頭所示方向旋轉帶式過濾器 7的濾布 14，同時，運轉真空泵8’在真空托盤11及12的真空度 提高狀態下，藉淤漿泵1 a ’自混合槽1 ’經由供給托盤 16，將 p 淤漿S供至帶式過濾器7的濾布1 4上。經由格網1 3 至真空托盤1 1，液體自淤漿S分離’與藉由真空抽吸自 帷幕部1 5內導出的氣體一起被導入氣液分離槽9，進行 氣液分離。於氣液分離槽9中分離的液體亦即母濾液排出 系統外，氣體經由真空泵8回流至帷幕部1 5。 又，於過濾部以外的部份中，濾布1 4藉自噴射噴嘴 2 1噴出的高壓水洗淨，自洗淨水托盤1 7將此際洗淨完的 液體L供至過濾部的濾布1 4上。藉此，濾布1 4上的淤漿 φ S以液體L洗淨，並經過真空過濾。此際，藉由沿濾布1 4 的移動方向往復移動真空托盤1 1及1 2，提高過濾效率。 藉著真空抽吸，經由格網1 3，於真空托盤1 2中液體自淤 漿S分離，獲得脫氯濾餅C。又，將自淤漿S分離的液體 與存在帷幕部1 5內的氣体一起導入氣液分離槽1 0，進行 氣液分離。於氣液分離槽1 0中分離的液體亦即溶解水排 出至吸收反應脫氣槽2 3，氣體經由真空泵8回流至帷 幕部1 5。 由於如上述使真空泵8的排氣回流至帷幕1 5供真空 -10- (7) 200405823 過濾，故可降低使用於真空過濾的氣體中二氧化 制二氧化碳的積垢發生，繼續穩定運轉。 且由於難以藉帷幕部1 5完全圍住格網1 1 4，故自系統外就氣體僅補充自帷幕部1 5逸 份，不過，此際以補充二氧化碳含量減少的氣體 更且，於上述實施形態中，固然藉由使真空 氣回流至帷幕1 5，減低二氧化碳含量，不過， φ 配置二氧化碳除去裝置於帷幕部1 5的排氣循環2 又，若隨著真空托盤1 1及1 2的往復移動， 盤1 1及1 2的箱狀開口部超出帷幕部1 5所圍範 下，繼續運轉真空泵8，即有吸入含二氧化碳的 形發生。於此情形下，較佳地，配置成將真空泵 導入真空托盤11及12，俾不會極力吸入大氣本J 雖然使用帶式過濾器7作爲真空過濾裝置， 可使用離心分離機等其他形式的固液分離裝置。 φ 且在將二水石膏供至混合槽1時，以強行混 膏與水，或強行混合水、二水石膏與焚化飛灰 此，可進一步增加鈣成份的析出量。 在強行混合二水石膏與水方面，有如第2圖 混合泵24混合二水石膏與水，經由軟管泵25及 合機2 6供至混合槽1的方法。於此，靜態型混名 以 2kg/cm 2程度的高壓，經由埋設於內部的多數 行混合攪拌二水石膏與水的裝置。 又，在強行混合水、二水石膏與焚化飛灰方 ,碳量，抑 3及濾布 漏的氣體 較佳。 泵8的排 更佳的是 5統。 在真空托 圍外狀態 大氣的情 8的排氣 % ° 不過，亦 合二水石 較佳。藉 所示，藉 靜態型混 ¥機26是 突起物強 面，有如 -11 - (8) 200405823 第3圖所示，於攪拌槽2 7內混合水、二水石膏與焚化飛 灰，經由軟管泵2 5及靜態型混合機2 6供至混合槽1的方 法。 即使替代二水石膏，自槽3將氯副產塵粉供至混合槽 1， 仍形成以氯副產塵粉爲核心，於其周圍析出錦成份並 附著成長的Μ發。同樣地，即使替代二水石膏或氯副產塵 鲁粉’驅動栗5，自硫酸槽6將硫酸供至混合槽1，仍形成 析出鈣成份的淤漿S。因此，可消除帶式過濾器7的格網 1 3的堵塞等或混合槽1等的積垢麻煩。進一步亦可藉由 替代硫酸’將二氧化碳供至混合槽1，形成析出鈣成份的 淤漿S。 又，亦可將含有二水石膏、氯副產塵粉及硫酸、二氧 化碳等中的複數個供至混合槽1。 其次，就本發明含鈣灰塵處理方法之實驗例加以說 _明。 在水洗處理氯副產塵粉方面，以二水石膏作爲種晶， 相對於貯存在混合槽1中的水，添加0.5%或1 .〇%於第1 圖的混合槽1中，使用帶式過濾器7進行固液分離，持續 運轉約3個月期間。其與過去未使用種晶，經過1 2小時 程度，即因帶式過濾器的格網堵塞而無法繼續運轉的情形 相比較，大幅改善。又，即使於混合槽1中，相對於過去 附著性高的積垢成長，在添加種晶情形下，仍只是激積、 附著不到1 mm的積垢，即便是沉落於混合槽1底部的粒 -12- (9) 200405823 子，雖很微細，卻幾乎無附著性。 比較在添加二水石膏於氯副產塵粉與焚化飛灰的混合 物（氯副產塵粉的重量比爲25% )以及不添加情形下帶式過 濾器的格網的重量增加，結果如次。 二水石膏添加率 ) ___— 0_ 0.5 0 J 8 0 〇 200 1 70 格網的重量增加 （g/3曰） 由此表可知，於添加構成種晶的二水石臂丨@形下運轉 3日後的格網重量增加相較於未添加情形’變成1 /4 度，可作達到過去4倍的長時間運轉。 又，隨著藉由添加種晶降低附著性，脫氯爐餅的過爐 性亦增加。帶式過濾器的過濾面積固然由濾鉼的水穿透優 良度、空氣穿透優良度等來決定，不過’如下表所不’在 混合槽1的溫度爲5 5 °C下，比較添加種晶情形與未添加 情形，亦可減低過濾面積約25% ° -13- (10) 200405823200405823 (1) 发明 Description of the invention [Technical field to which the invention belongs] The present invention relates to a method and a device for processing calcium-containing powder, and more particularly, a method and a device for washing calcium-containing powder such as incinerated fly ash by water washing. [Previous technology] Although recycling of cement raw materials such as incineration fly ash and other waste materials has been promoted in recent years, as the amount of waste treated increases, the amount of volatile components such as chlorine carried into the cement kiln also increases. It is the cause of problems such as blocking of preheaters in cement manufacturing equipment. Therefore, it is used as a raw material for cement after removing chlorine components from incinerated fly ash and the like in advance. In this case, the water-soluble chlorine compound is easily soluble in water. After dissolving the incinerated fly ash and water to dissolve the chlorine, the water-soluble chlorine compound contained in the incinerated fly ash is removed by washing with water using a water filter such as a belt filter. And use it as a cement raw material. # However, most of the incinerated fly ash contains calcium. When washed, the calcium will dissolve in water, which will cause scale to grow and grow in the water washing equipment. If this scale is left unattended, the efficiency of the water-eluent chlorine treatment of incinerated fly ash will be reduced, and the operation of the water washing equipment may be hindered. In particular, in recent years, a large amount of slaked lime has been put into incinerators such as municipal waste incinerators as a countermeasure against dioxin. Therefore, calcium carbonate deposits are apt to occur, and measures are required to prevent the obstacles caused by the deposits. [Summary of the Invention] (2) 200405823 The present invention is a technique proposed to eliminate such a problem, and the object thereof is to provide a method for suppressing the growth of scale and efficiently incinerating chlorine-eluted water containing bromide powder such as fly ash. And device. The first calcium-containing powder treatment method of the present invention is a water-washing method for solid-liquid separation after the calcium-containing powder is dissolved in water. When the calcium-containing powder is dissolved in water, crystals of gypsum dihydrate and chlorine are added. Any of dust-producing powder, sulfuric acid, and carbon dioxide, the brocade is precipitated. p. After forcibly mixing any of the crystals of dihydrate gypsum and chlorine by-product dust powder with water, calcium-containing powder can be mixed in this mixed liquid. It is also possible to forcibly mix any of the crystals of dihydrate gypsum and chlorine by-product dust powder, water and calcium-containing powder. Furthermore, preferably, the calcium-dissolved solution is precipitated by vacuum filtration, and solid-liquid separation is performed to obtain a filter cake. At the same time, the exhaust gas generated during vacuum filtration is returned to the filter cake and circulated. The second calcium-containing powder processing method of the present invention is a water-washing method in which the calcium-containing powder is dissolved in φ water and then subjected to solid-liquid separation. The convection reaction in a gas absorption reaction tank is carried out by washing with carbon dioxide and minimizing carbon dioxide. The heavy metals in the water washing and drainage are precipitated, and thereafter, the gas is degassed from the water washing and drainage in a degassing tank formed integrally with the gas absorption reaction tank. Moreover, the dispersing means is flexible, and the clogging of the dispersing means can be removed by intermittently blowing carbon dioxide '. In addition, the first calcium-containing powder processing device of the present invention is a water-washing device for solid-liquid separation after the calcium-containing powder is dissolved in water, and includes a mixing tank for mixing and dissolving the calcium-containing powder and water, and Crystals of hydrogypsum and by-products of chlorine-6-(3) 200405823 Any of dust powder, sulfuric acid, and carbon dioxide is supplied to the mixing tank. Moreover, in terms of supply means, either the crystals of the dihydrate gypsum and chlorine by-product dust powder may be forcibly mixed with water, or the crystals of the dihydrate gypsum and chlorine by-product dust powder may be forcibly mixed at the same time. , Forced mixing means of water and thorium-containing powder, and a pump for supplying the mixed liquid forcibly mixed by the forced mixing means to the mixing tank. β It is further preferred to further include a vacuum filtration device that obtains φ obtained in a mixing tank by vacuum filtration, and uses solid-liquid separation to obtain a filter cake, φ, and exhaust gas generated from the vacuum filtration device Circulation means for returning to the filter cake in the vacuum filtration device for circulation. The second calcium-containing powder processing device of the present invention is a water-washing device for solid-liquid separation after the calcium-containing powder is dissolved in water. The heavy metal-based absorption reaction tank in which the washing water is discharged, and the gas absorption reaction tank which communicates with the gas absorption reaction tank are integrated into the gas absorption reaction tank, and at the same time, the degassing tank is degassed from the washing water drainage through the gas absorption reaction tank. φ In addition, the dispersing means is flexible, and it may be provided with a blowing control means for removing the clogging of the dispersing means by intermittently blowing carbon dioxide from the dispersing means. In this case, it is preferable to use a means having a dispersion plate made of rubber or a dispersion tube made of rubber as the dispersion means. [Embodiment] "Best Mode for Carrying Out the Invention" An embodiment of the present invention will be described below with reference to the drawings. h 1 (4) 200405823 The process flow of the incineration fly ash treatment method according to the embodiment of the present invention is schematically shown in FIG. 1. A tank 2 for incineration fly ash 2, a tank 3 for storing by-product chlorine dust, and a tank 4 for dihydrate gypsum are connected to the mixing tank 1, and a sulfuric acid tank 6 is connected to the mixing tank 1 via a pump 5. A belt filter 7 as a vacuum filtration device is connected to the mixing tank 1 via a slurry pump 1a. The belt filter 7 is roughly divided into a grid including a water-sealed vacuum pump 8, a gas-liquid separation tank 9 and 10, a vacuum tray 1 1 and 1 2, and a plurality of openings arranged above the vacuum tray 1 1 and 1 2 1 3. Endless band-shaped filter cloth moving above the grid 1 3 丨 4. Curtains surrounding the grid 1 3 and the filter cloth 1 4 5. It is used to supply the slurry S to the filter cloth! The supply tray 16 on 4 and the washing water tray 17 on which the liquid 1 for washing the slurry S is supplied. The vacuum trays 11 and 12 communicate with the vacuum pump 8 through the gas-liquid separation tanks 9 and 10. The vacuum trays 11 and 12 are formed in the shape of an open box at the top, and can be driven by means of a figure 'through a plurality of rollers 19 arranged on the guide rail 18, and reciprocating on the guide rail 18 along the moving direction of the filter cloth φ 1 4 mobile. The grid 13 is a member provided above the vacuum trays 11 and 12 and having a plurality of openings formed in a plate-like member formed of resin, metal, or the like. The filter cloth 14 is formed on an endless belt that moves above the grid 13 and is supported by a plurality of rollers 20 and rotates in the direction of the arrow. In order to clean the filter cloth 14, spray nozzles 21 for spraying high-pressure water or the like are arranged in a part other than the filter section. The outlet pipe 22 of the vacuum pump 8 is connected to the curtain portion 15 and is arranged so that the exhaust gas of the vacuum pump 8 flows back into the curtain portion 15. The curtain portion 15 covers the grid 13 and the filter cloth 14 to prevent infiltration of the atmosphere outside the system -8- (5) (5) 200405823. The gas-liquid separation tanks 9 and 10 are respectively disposed between the vacuum trays 11 and 12 and the vacuum pump 8, and the gas-liquid separation tank 9 performs liquid separation from the slurry S supplied to the grid 13 through the supply tray 16 The gas-liquid separation from the gas, and the gas-liquid separation tank 10 performs gas-liquid separation of the liquid and the gas separated from the slurry S washed with washing water. An absorption reaction / deaeration tank 23 was further connected to the gas-liquid separation tank 10. Next, an incineration fly ash treatment method according to this embodiment will be described. First, fly ash and water from the tank 2 are supplied to the mixing tank 1, and at the same time, dihydrate gypsum from the tank 4 is added to the mixing tank 1, and the mixture is stirred. As a result, a dihydrate gypsum is used as a seed crystal, and a calcium component is precipitated around the gypsum, and a grown slurry S is attached. At this time, the weight ratio of incinerated fly ash to water is set to 1: 5, for example. In order to promote the adhesion of calcium components and grow on the seed crystals, it is preferred that the amount of dihydrate gypsum is equal to the weight of water in the mixing tank 1. · 1 ~ 10%, the temperature of water is 20 ~ 60 ° c. In order to more effectively adhere and grow the calcium component to the seed crystal, it is suitable to mix it slowly in the mixing tank 1 while facing the water, incinerated fly ash and dihydrate gypsum for 10 to 20 minutes, and store it, preferably, Stir slowly for 30 minutes to 1 hour. Since the dihydrate gypsum is added when the incinerated fly ash is dissolved in water, improper clogging of the grid 13 of the belt filter 7 during solid-liquid separation is minimized, and the mixing tank is eliminated. Trouble with dirt in 1. In addition, when adding dihydrate gypsum to the mixing tank 1, it is difficult to use the example (6) 200405823 such as adding a small amount each time such as a skirt feeder, so the dihydrate gypsum can be dispersed in advance with the water that dissolves the incinerated fly ash Dissimilar water, after which a slurry was formed and added to the mixing tank 1 using a slurry pump. Thereafter, the filter cloth 14 of the belt filter 7 is rotated in the direction indicated by the arrow, and at the same time, the vacuum pump 8 'is operated to increase the vacuum of the vacuum trays 11 and 12, and the slurry pump 1a' is passed from the mixing tank 1 ' The supply tray 16 supplies the p slurry S to the filter cloth 14 of the belt filter 7. Via the grid 13 to the vacuum tray 11, the liquid is separated from the slurry S 'and is introduced into the gas-liquid separation tank 9 together with the gas led out from the curtain portion 15 by vacuum suction, and gas-liquid separation is performed. The liquid separated in the gas-liquid separation tank 9, that is, the mother filtrate, is discharged out of the system, and the gas is returned to the curtain portion 15 through the vacuum pump 8. In addition to the part other than the filtering part, the filter cloth 14 is washed by the high-pressure water sprayed from the spray nozzle 21, and the self-washing water tray 17 supplies the liquid L thus washed to the filtering part of the filtering part. Cloth 1 on 4. Thereby, the slurry φS on the filter cloth 14 was washed with the liquid L, and was vacuum-filtered. At this time, the vacuum trays 11 and 12 are moved back and forth along the moving direction of the filter cloth 14 to improve the filtration efficiency. By vacuum suction, the liquid was separated from the slurry S in the vacuum tray 12 through the grid 13 to obtain a dechlorinated filter cake C. The liquid separated from the slurry S is introduced into the gas-liquid separation tank 10 together with the gas stored in the curtain portion 15 to perform gas-liquid separation. The liquid separated in the gas-liquid separation tank 10, that is, dissolved water, is discharged to the absorption reaction degassing tank 23, and the gas is returned to the curtain portion 15 through the vacuum pump 8. As described above, the exhaust gas of the vacuum pump 8 is returned to the curtain 15 for vacuum -10- (7) 200405823 for filtering, so that the generation of carbon dioxide from carbon dioxide in the gas used for vacuum filtering can be reduced, and stable operation can be continued. And because it is difficult to completely surround the grid 1 1 4 by the curtain 15, the gas from the outside of the system only replenishes 15 escapes from the curtain. However, in this case, supplementing the gas with a reduced carbon dioxide content is even more important. In the form, although the vacuum gas is returned to the curtain 15 to reduce the carbon dioxide content, a carbon dioxide removal device φ is arranged in the exhaust cycle 2 of the curtain 15 and if the vacuum trays 11 and 12 reciprocate When moving, the box-shaped openings of the disks 1 1 and 12 exceed the range surrounded by the curtain 15, and the vacuum pump 8 continues to operate, and the shape containing carbon dioxide is sucked. In this case, preferably, it is configured to introduce the vacuum pump into the vacuum trays 11 and 12, so that it will not suck into the atmosphere as much as possible. Although the belt filter 7 is used as a vacuum filtering device, other types of solids such as a centrifugal separator can be used. Liquid separation device. φ When the dihydrate gypsum is supplied to the mixing tank 1, forcefully mix the paste with water, or forcefully mix the water, dihydrate gypsum, and incinerated fly ash. This can further increase the precipitation of calcium. The forcible mixing of dihydrate gypsum and water is as shown in Fig. 2. The mixing pump 24 mixes the dihydrate gypsum and water and supplies it to the mixing tank 1 via the hose pump 25 and the mixer 26. Here, the static type mixer is a device that mixes and stirs the dihydrate gypsum and water at a high pressure of about 2 kg / cm 2 through a plurality of rows buried inside. In addition, in the forced mixing of water, dihydrate gypsum and incinerated fly ash, the amount of carbon, 3 and the leakage of filter cloth are better. The row of the pump 8 is more preferably 5 lines. Exhaust condition in the atmosphere outside the vacuum enclosure 8%% However, it is better to combine dihydrate. As shown, the static mixing machine 26 is the strong surface of the protrusions, as shown in Figure 3 at -11-(8) 200405823. Mix the water, dihydrate gypsum, and incinerated fly ash in the mixing tank 27, as shown in Figure 3. Method for supplying the pump 25 and the static mixer 26 to the mixing tank 1. Even if the dihydrate gypsum is replaced, the chlorine by-product dust powder is supplied from the tank 3 to the mixing tank 1, and the chlorine by-product dust powder is still formed as a core, and brocade components are precipitated around it, and a long hair is attached. Similarly, even if the dihydrate gypsum or chlorine by-product dust powder is used to drive the chestnut 5, the sulfuric acid is supplied from the sulfuric acid tank 6 to the mixing tank 1, and a slurry S in which calcium components are precipitated is formed. Therefore, clogging of the grids 13 and the like of the belt filter 7 and the trouble of fouling of the mixing tank 1 and the like can be eliminated. Further, carbon dioxide may be supplied to the mixing tank 1 by replacing sulfuric acid 'to form a slurry S in which calcium components are precipitated. Further, a plurality of gypsum, chlorine by-product dust, sulfuric acid, carbon dioxide, and the like may be supplied to the mixing tank 1. Next, experimental examples of the method for treating calcium-containing dust according to the present invention will be described. For the washing of chlorine by-product dust, water gypsum is used as seed crystals, and 0.5% or 1.0% of the water stored in the mixing tank 1 is added to the mixing tank 1 in FIG. 1 using a belt type. The filter 7 performs solid-liquid separation, and is continuously operated for about 3 months. Compared with the case where the seed crystal has not been used in the past, it has been improved for about 12 hours, that is, the case where the grid of the belt filter is blocked and cannot continue to operate. In addition, even in the mixing tank 1, the growth of deposits with high adhesion compared with the past, when seed crystals were added, the deposition was still only precipitating, and the deposit was less than 1 mm, even if it was sinking on the bottom of the mixing tank 1. The seeds of -12- (9) 200405823, although very fine, have almost no adhesion. Comparing the mixture of dihydrate gypsum with chlorine by-product dust and incinerated fly ash (the weight ratio of chlorine by-product dust is 25%) and the weight increase of the mesh of the belt filter without adding, the results are as follows . Addition rate of dihydrate gypsum) ___— 0_ 0.5 0 J 8 0 〇200 1 70 Weight increase of the grid (g / 3) From this table, it can be seen that after adding the dihydrate stone arm constituting the seed crystal, @ 形 下 转 3 days Compared with the non-addition case, the increase in the weight of the grid becomes 1/4 degree, which can be used for long-time operation that reaches 4 times of the past. In addition, as the adhesion is reduced by adding seed crystals, the overheating property of the dechlorination furnace cake is also increased. The filter area of the belt filter is determined by the water penetration and air penetration of the filter. However, 'not shown in the table below', the temperature of the mixing tank 1 is 5 5 ° C. Crystalline and non-added conditions can also reduce the filtration area by about 25% ° -13- (10) 200405823
處理物 高濃渡 氯副產塵粉 低濃度 氯副產塵粉 過濾面積（m 2) 「有種晶」 1.86 1 .69 過濾面積（m 2) 「無種晶」 1.44 1.23 減低率（％ ) 23 27Treatment area High-concentration chlorine by-product dust powder Low-concentration chlorine by-product dust powder Filtration area (m 2) “With seed” 1.86 1.69 Filtration area (m 2) “No seed” 1.44 1.23 Reduction rate (%) 23 27
其次，就有關藉靜態型混合機2 6強行混合的實驗例 加以說明。 比較在淤漿化氯副產塵粉與水時，藉靜態型混合機 2 6強行混合情形與未如此進行情形，進一步比較在添加 種晶情形與未如此進行情形下，攪拌淤漿後過濾之際的透 過份的浮遊粒子狀物質的濃度，獲得如下表結果。且在實 ϋ驗時，使用溫度5 0 °C的水，於攪拌激漿3 0分後，進行過 濾。 浮遊粒子狀物質的濃度（ppm) 種晶 Μ j\\\ 有 強行混合 並 j\\\ 3 0 0 0 700 有 1500 230 由此表可知，由於藉靜態型混合機2 6強行混合情形 • 14 - (11) 200405823 以及添加種晶情形相較於均未實施情形，通過濾布的浮遊 粒子狀物質的量減少，故推定溶解的鈣附著、成長於種晶 上。進一步比較進行強行混合及種晶的添加二者的情形與 均未實施的情形，通過濾布的浮遊粒子狀物質的量在1 /1 〇 以下，推定大量的鈣附著、成長於種晶上 4 於此顯示氣體吸收反應·脫氣槽2 3的構造於第4圖 中。 > B 此氣體吸收反應·脫氣槽23大致區分具備使氣液分離Next, an experimental example of forced mixing by a static mixer 26 will be described. Compare the situation of forcible mixing by static mixer 26 and the case when the by-product dust powder and water are slurried, and further compare the case where the seed crystal is added and the case where the slurry is not so filtered. The following table shows the concentrations of the suspended particulate matter in the permeate fraction. In the actual test, water was used at a temperature of 50 ° C, and the slurry was stirred for 30 minutes before filtering. Concentration of floating particulate matter (ppm) Seed crystals M \\ with forced mixing and j \\\ 3 0 0 0 700 with 1500 230 It can be seen from the table that the forced mixing by the static mixer 2 6 • 14 -(11) 200405823 and the case where seed crystals were added, the amount of suspended particulate matter passing through the filter cloth was reduced compared to the case where neither seed crystals were added. Therefore, it is estimated that dissolved calcium adheres to and grows on the seed crystals. Further comparison is made between the case of forced mixing and the addition of seed crystals, and the case where neither is implemented. The amount of suspended particulate matter of the filter cloth is 1/1/10 or less, and it is estimated that a large amount of calcium adheres to and grows on the seed crystals. 4 The structure of the gas absorption reaction / degassing tank 23 is shown in FIG. 4. > B This gas absorption reaction and degassing tank 23 is roughly divided to have gas-liquid separation
槽1 〇所分離的液體L 1與自下方供給的氣體G相對流反 應的反應槽3 1，以及從排自反應槽3 1的液體L2脫氣的 脫氣槽3 2。反應槽3 1形成底部開口的方柱形，於上部連 接用來供給液體L1的給水管3 5以及氣體G的排氣管 34，於下部配置供給氣體G的給氣管3 5，以及用來將供 自給氣管35的氣體G的氣泡直徑微細化成0.5〜3 mm的橡 膠製散氣板3 6。散氣板3 6是於橡膠板上具有多數細刻紋 φ的構件，一供給氣體，橡膠即藉氣體G的壓力伸張，自 I 多數刻紋吹入氣體G。且，亦可設置多孔板來替代散氣板 3 6。進一步於反應槽3 1的給水管3 3的出口配置用來於反 應槽3 1內高效率分散供自給水管3 3的液體L 1的液體分 散板3 7。又於反應槽3 1的內部配置用來對液體L1及氣 體G的上下方向的流體進行整流的格子狀整流板3 8。 脫氣槽3 2的上部成方柱狀，下部成角錐狀，脫氣槽 3 2的內部與反應槽3 1的下部連通。又，脫氣槽3 2的上 部對大氣開放，於上部形成將脫氣的液體L2排出的排水 -15- (12) 200405823 口 3 9 ’於下部形成排出沉殿物（淤渣）的淤渣排出口 4〇。 又’於脫氣槽3 2設置用來添加凝聚劑C的圖略添加裝 置、用來攪拌脫氣槽3 2內部的攪拌機4 1以及用來測定脫 氣槽3 2內液體的P Η値的P Η計。 又’反應槽3 1的給氣管3 5經由鼓風機等構成的吹入 控制裝置4 3連接於圖略之水泥燒製用窯。 自第1圖所示氣液分離槽1 0經由給水管3 3供至反應 φ 槽31的液體L1含有Ca + 2、SO-2、M g + 2等金屬離子。含 有多量二氧化碳的氣體G自圖略水泥燒製用窯經由吹入 控制裝置4 3吹入反應槽3 1。氣體G自反應槽3 1下部的 給氣管3 5經由散氣板3 6吹入學，其氣泡直徑微細化成 0.5〜3 mm，於反應槽3 1內與液體L1對流並接觸，中和液 體L1中的Ca + 2、SO·2、M g + 2等離子，產生CaC03、 CaS04、MgC03 等。 由於此際氣體G的氣泡直徑藉散氣板3 6微細化，故 着積垢附著於反應槽3丨內面的情形大幅減少，同時，反應 效率提高’氣體量變動伴生的反應效率變化減小，容易進 行伴隨氣體量變動所作PH控制。又，亦藉液體分散板3 7 及整流板3 8奏得反應效率提高，氣體量變動伴生的反應 效率變化進一步減小等效果。 於反應槽3 1中的反應結束後的氣體G經由排氣管3 4 排入大氣。另一方面，與氣體G相反應結束的液體L2導 入脫氣槽3 2內部脫氣，同時，因不溶化而發生的前述金 屬碳酸鹽藉自圖略添加裝置添加的凝聚劑C凝聚。脫氣槽 -16- (13) 200405823 32 內的液體L2藉攪拌機4 1攪拌，促進反應。又’藉 Ρ Η計4 2監視脫氣槽3 2內的液體L 2的Ρ Η値’藉吹入控 制裝置4 3，根據Ρ Η計4 2的輸出，控制氣體G對反應槽 3 1的供給量。 於脫氣槽3 2中金屬碳酸鹽凝聚的液體L 2經由排水口 3 9供至圖略沉降槽等，沉降於沉降槽的金屬碳酸鹽則被 φ 排出系統外。又，發生於脫氣槽3 2的沉澱物T藉栗等經 由淤渣排出口 4 0排出。 按照反應槽3 1內的液體L1與脫氣槽3 2內的液體L2 的比重差，在反應槽3 1的液面高於脫氣槽3 2的液面狀態 下平衡，即使來自氣液分離槽1 〇的液體L 1的供給量有些 許變動，只要溢自排水口 3 9的溢流量變動些許即可，無 需過去的水平控制。 其中，由於散氣板3 6由具有彈性的橡膠形成，故如 第5圖所不’在氣體G未吹入時，呈平面形狀，不過， 氣體G —吹入’散氣板3 6即藉氣體〇的壓力向外膨脹彎 曲成凸狀。因此，若藉吹入控制裝置4 3間歇進行氣體G 的供給/停止，散氣板3 6的形狀即變化，藉此，可除去附 著於散氣板3 6表面的積垢。亦即，可消除散氣板3 6的堵 塞。 又，亦可如第6圖所不，使用具有彈性的橡膠形成的 散氣管4 4來替代散氣板3 6。如同散氣板3 6，散氣管4 4 是於橡膠管上具有多數細刻紋的構件，一供給氣體G，橡 -17 - (14) 200405823 膠即藉氣體G的壓力，如鏈線所示伸張，自多數刻紋吹 入氣體G。即便使用此種散氣管44 ’同時，藉吹入控制 裝置4 3間歇進行氣體G的供給/停止’仍可因散氣管4 4 的形狀變化而除去附著於散氣管4 4表面的積垢，可消除 散氣管44的堵塞。 進一步如第7圖所不，於橡膠製散氣管44附近上下 作動自如地配設升舉構件4 5，即使藉由定期上昇升舉構 ^ 件4 5 ,升舉散氣管44的中央部，使其變形，仍可除去附 著於散氣管4 4表面的積垢。 如以上說明，根據本發明，於水洗處理焚化飛灰、氯 副產塵粉等含鈣粉體時’可抑制水洗設備內積垢的發生· 成長，可有效防止積垢所造成的障礙。 【圖式簡單說明】 第1圖是槪略顯示本發明實施形態的含鈣粉體處理方 φ法的流程的流程圖； 第2圖是顯示變形例的含鈣粉體溶解方法的圖面； 第3圖是顯示另一變形例的含鈣粉體溶解方法的圖 面； 第4圖是顯示實施形態所用氣體吸收反應·脫氣槽的 剖視圖； 第5圖是顯示散氣板的剖視圖； 第6圖是顯示散氣管的剖視圖； 第7圖是顯示積垢除去裝置的圖面。 -18- (15) (15)200405823 主要元件對照表 1混合槽 1 a淤漿泵 2、3、4 槽 5硫酸槽 7帶式過濾器 8 真空泵 9、1 0 氣液分離槽 1 1、1 2 真空托盤 1 3格網 14 濾布 1 5 帷幕部 1 6 供給托盤 18 導軌 1 9、2 0 滾子 2 2出口配管 2 3脫氣槽 2 5軟管泵 2 6靜態型混合器 27攪拌槽 3 1反應槽 3 2脫氣槽 3 3給水管 -19-The reaction tank 31 which reacts the liquid L1 separated from the tank 10 with the gas G supplied from below, and the degassing tank 32 which degassed the liquid L2 discharged from the reaction tank 31. The reaction tank 31 is formed in a square column shape with an open bottom, and is connected to a water supply pipe 35 for supplying liquid L1 and an exhaust pipe 34 for gas G at the upper portion, and a gas supply pipe 35 for supplying gas G to the lower portion, and a The bubble diameter of the gas G supplied from the gas supply pipe 35 is reduced to a rubber diffuser plate 36 of 0.5 to 3 mm. The diffuser plate 36 is a member having a plurality of fine marks φ on the rubber plate. When the gas is supplied, the rubber is stretched by the pressure of the gas G, and the gas G is blown from the majority of the marks I. Moreover, a perforated plate may be provided instead of the diffuser plate 36. Further, an outlet of the water supply pipe 3 3 of the reaction tank 31 is provided with a liquid dispersion plate 37 for efficiently dispersing the liquid L 1 supplied from the water supply pipe 3 3 in the reaction tank 31. A grid-shaped rectifying plate 38 for rectifying the liquid in the vertical direction of the liquid L1 and the gas G is arranged inside the reaction tank 31. The upper part of the degassing tank 32 is formed in a square column shape, and the lower part is pyramid-shaped. The inside of the degassing tank 32 is communicated with the lower part of the reaction tank 31. In addition, the upper part of the degassing tank 32 is opened to the atmosphere, and a drain for discharging the degassed liquid L2 is formed on the upper part. Discharge port 40. In addition, a schematic adding device for adding coagulant C is provided in the degassing tank 3 2, a stirrer 41 for stirring the inside of the degassing tank 3 2, and a method for measuring the P 液体 of the liquid in the degassing tank 3 2. P Count. The gas supply pipe 35 of the reaction tank 31 is connected to a cement firing kiln (not shown) via a blow-in control device 4 3 constituted by a blower or the like. The liquid L1 supplied from the gas-liquid separation tank 10 shown in FIG. 1 to the reaction via the water supply pipe 3 3 in the φ tank 31 contains metal ions such as Ca + 2, SO-2, and M g + 2. A gas G containing a large amount of carbon dioxide is blown into the reaction tank 31 from the kiln for cement firing through a blowing control device 4 3. The gas G is blown in from the gas supply pipe 35 in the lower part of the reaction tank 31 through the diffuser plate 36, and the bubble diameter is reduced to 0.5 to 3 mm, and the liquid L1 is convected and contacted in the reaction tank 3 1 to neutralize the liquid L1. Ca + 2, SO · 2, M g + 2 plasma, CaC03, CaS04, MgC03 and so on. At this time, the bubble diameter of the gas G is made finer by the diffuser plate 36. Therefore, the deposition of dirt on the inner surface of the reaction tank 3 is greatly reduced, and at the same time, the reaction efficiency is increased, and the change in the reaction efficiency caused by the fluctuation of the gas amount is reduced. It is easy to carry out pH control with the change of gas amount. In addition, the liquid dispersion plate 37 and the rectifying plate 38 can also improve the reaction efficiency, and further reduce the change in the reaction efficiency caused by the change in the amount of gas. The gas G after the completion of the reaction in the reaction tank 31 is discharged into the atmosphere through the exhaust pipe 3 4. On the other hand, the liquid L2, which has completed the reaction with the gas phase G, is introduced into the degassing tank 32 and deaerated. At the same time, the aforementioned metal carbonate which is caused by insolubilization is coagulated by the coagulant C added by the schematic addition device. Degassing tank -16- (13) 200405823 32 The liquid L2 in the mixer is stirred by the mixer 41 to promote the reaction. In addition, by monitoring the P of the liquid L 2 in the degassing tank 3 2 by the P 4 meter 4 2, the gas G is controlled to the reaction tank 3 1 by the blow-in control device 4 3 according to the output of the P 4 meter 4 2. Supply amount. The liquid L 2 condensed by the metal carbonate in the degassing tank 32 is supplied to the settling tank and the like through the drain port 39, and the metal carbonate settling in the settling tank is discharged out of the system by φ. Further, the sediment T generated in the degassing tank 32 is discharged through the sludge discharge port 40 through chestnuts and the like. According to the difference between the specific gravity of the liquid L1 in the reaction tank 31 and the liquid L2 in the degassing tank 32, the liquid surface in the reaction tank 31 is higher than the liquid level in the degassing tank 32, even if it comes from gas-liquid separation. The supply amount of the liquid L 1 in the tank 10 is slightly changed, as long as the overflow flow from the drain port 39 is slightly changed, the previous level control is not necessary. Among them, since the diffuser plate 36 is formed of elastic rubber, it does not have a flat shape when the gas G is not blown as shown in FIG. 5. However, the gas G is blown into the diffuser plate 3 6 to borrow. The pressure of the gas 0 expands and bends into a convex shape. Therefore, if the supply / stop of the gas G is intermittently performed by the blow-in control device 4 3, the shape of the air diffusing plate 36 is changed, thereby removing the deposits on the surface of the air diffusing plate 36. That is, clogging of the air diffusing plate 36 can be eliminated. Alternatively, instead of the diffuser plate 36, a diffuser tube 4 4 made of elastic rubber may be used as shown in FIG. 6. Like the diffuser plate 36, the diffuser tube 4 4 is a member with most fine engravings on the rubber tube. As soon as the gas G is supplied, the rubber -17-(14) 200405823 is the pressure of the gas G, as shown by the chain line. Stretching, gas G is blown in from most engravings. Even if such a diffuser 44 is used, 'the gas G is intermittently supplied / stopped by the blowing control device 4 3 at the same time', the scale attached to the surface of the diffuser 44 can be removed due to the shape change of the diffuser 4 4. The blockage of the air diffusing pipe 44 is eliminated. Further, as shown in FIG. 7, a lifting member 45 is arbitrarily arranged in the vicinity of the rubber diffuser 44 and the central portion of the diffuser 44 is lifted even if the lifting member 45 is regularly raised. This deformation can still remove the scale attached to the surface of the air diffuser 44. As described above, according to the present invention, when calcium-containing powder such as incinerated fly ash and chlorine by-product dust is washed with water, the generation and growth of scale in the washing equipment can be suppressed, and obstacles caused by scale can be effectively prevented. [Brief Description of the Drawings] FIG. 1 is a flowchart showing a flow of a method for processing a calcium-containing powder according to an embodiment of the present invention; and FIG. 2 is a diagram showing a method for dissolving a calcium-containing powder in a modified example. Fig. 3 is a diagram showing a method for dissolving a calcium-containing powder according to another modification; Fig. 4 is a sectional view showing a gas absorption reaction and degassing tank used in the embodiment; Fig. 5 is a sectional view showing a diffuser plate; Fig. 6 is a cross-sectional view showing a diffuser; Fig. 7 is a view showing a scale removing device. -18- (15) (15) 200405823 Comparison table of main components 1 Mixing tank 1 a Slurry pump 2, 3, 4 Tank 5 Sulfuric acid tank 7 Belt filter 8 Vacuum pump 9, 1 0 Gas-liquid separation tank 1 1, 1 2 Vacuum tray 1 3 grid 14 Filter cloth 1 5 Curtain 1 6 Supply tray 18 Guide 1 9 2 Roller 2 2 Outlet piping 2 3 Degassing tank 2 5 Hose pump 2 6 Static mixer 27 Stirring tank 3 1 reaction tank 3 2 degassing tank 3 3 water supply pipe -19-
•f>4S (16)200405823 3 4排氣管 3 5給氣管 36 > 44 散氣管 3 7液分散板 3 9 排水口 4 〇 排出口 4 1攪拌機• f > 4S (16) 200405823 3 4 exhaust pipe 3 5 air supply pipe 36 > 44 diffuser pipe 3 7 liquid dispersion plate 3 9 drainage port 4 〇 discharge port 4 1 mixer
42 PH 計 43 吹入控制裝置 45升舉構件42 PH meter 43 Blow-in control device 45 Lifting member
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