200300134 玖、發明說明 發明所屬之技術領域 本發明係關於矽酸質肥料用原料.及其製造方法者。 先前技術 矽酸質肥料主要係以對水稻補給矽酸爲目的之肥料， 含有可溶性矽酸1 〇質量％至2 0質量％以上，鹼性份2 5 質量％至 3 Q質量％以上，作爲水田的土壤保持及老化水 田的土壤改質劑被大量地使用著。又，近年來，有關矽 酸質肥料可強化植物體，不易受到病蟲害侵害之作用受 到注目，不只是水稻，亦日益擴及使用於小黃瓜等的蔬 菜類。 矽酸質肥料雖亦可由天然資源的硅灰石製造， 惟， 現今大多數的矽酸質肥料係以高爐爐渣作爲原料而製 造。欲由高爐爐渣製造矽酸質肥料，例如，於日本專利 特開昭5 5 - 1 1 3 6 8 7號公報所示般，係將由高爐所排出之 熔融狀態的高爐爐渣徐徐冷卻使其固化，使此固化的塊 狀的高爐爐渣乾燥之後，加以粉碎，調整爲所要的粒度 作成爲矽酸質肥料。然而，高爐爐渣的鹼性度 (C a Ο / S i Ο 2 )，由於會促進高爐內的脫硫反應，故通常須 調整於1 . 2 4 ~ 1 · 2 6程度的範圍內，因此，以高爐爐渣作 爲原料的矽酸質肥料的鹼性度理所當然地也在該範圍 中，而成爲鹼性份比較多的肥料。又，通常，於高爐爐 渣中含有13〜15質量％程度的A1203,當然肥料中會含有 如此多量的A 1 2 0 3。因而，經由使用這樣的矽酸質肥料， 7 200300134 於對土壤投與矽酸之同時，也會投與鹼性材料及A 1 2 Ο 3。 於曰本的農地原本以酸性土壤居多，因此，使用上述 般的鹼性份多的矽酸質肥料原係符合土壤改良的目的 者。然而，近來，隨著以矽酸質肥料爲始之肥料的施肥 量之增加，酸性土壤的問題已在減少中，因此，代之以 向來所使用之鹼性份多的矽酸質肥料，轉而需求矽酸含 有量高且鹼性份少的矽酸質肥料。 又，以高爐爐渣爲原料之矽酸質肥料中多量地含有之 A 1 2〇3並非作爲肥料的有效成分，另一方面，A 1 2 0 3會將 土壤中的磷酸固定住成爲植物無法利用的形態，或會阻 礙矽酸的溶出性之問題也曾被提出。 發明內容 本發明之目的，在於提供一種可用以廉價地製得矽酸 (可溶性矽酸）的含有量多且鹼性份少（更佳者爲 A 1 2 0 3 含有量少）的矽酸質肥料的矽酸質肥料用原料。 又，本發明之其他的目的，在於提供用以製得上述矽 酸質肥料用原料之較佳的矽酸質肥料用原料之製造方 法。 又，本發明之另外的目的，在於提供使用上述矽酸質 肥料用原料的矽酸質肥料及其製造方法。 本發明者等，於肥料的組成及製造成本方面，就符合 上述的要求之矽酸質肥料用原料一再加以檢討之下，結 果發現：用高爐熔融鐵的熔融鐵預備處理步驟中所回收 的特定的爐渣作爲矽酸質肥料的原料爲極佳者，可在不 8 200300134 外加以特殊的處理之下直接利用來作爲矽酸質肥料用原 料，而且可顯現出作爲肥料之優異的性能。又，發現： 其中尤以具有特定的鹼性度之爐渣，而以經由特定的冷 卻條件下製得之爐渣更佳，可顯示出作爲肥料之特別優 異的性能。 基於這樣的發現，依據本發明所提供的矽酸質肥料用 原料，係高爐熔融鐵的熔融鐵預備處理步驟中所回收之 爐渣；其特徵在於，係含有經由使熔融鐵中的矽經氧化 所生成之矽酸，且係由含有可溶性矽酸1 〇質量％以上之 爐渣所構成。 上述矽酸質肥料用原料，其可溶性矽酸的含有量以儘 可能高爲佳，以含有可溶性矽酸2 0質量％以上爲佳，而 以3 Q質量％以上更佳。 此處，上述矽酸質肥料用原料之中的下述（1 )、（ 2 ) 者，由於係含有可溶性矽酸2 0質量％以上，故爲較佳的 肥料用原料。 (1 )於熔融鐵預備處理步驟中回收之後，至少於 1 3 0 Q〜1 Q Q Q °C的溫度區域間以 1 〇 °C /分未滿的冷卻速度 施行冷卻所得到之爐渣，且係由鹼性度（C a 0 / S i 0 2 )爲 0 . 5 2 ~ 2 . 0的爐渣所構成的矽酸質肥料用原料。 (2 )於熔融鐵預備處理步驟中回收之後，至少於 1 3 0 Q〜1 0 0 0 °C的溫度區域間以 1 〇 °C /分以上的冷卻速度 施行冷卻所得到之爐渣，且係由鹼性度（C a Ο / S i 0 2 )爲 0 . 4 9〜2 . 0的爐渣所構成的矽酸質肥料用原料。 9 200300134 又，上述矽酸質肥料用原料之中的下述（3 )者，由於含’ 有3 0質量％以上的可溶性矽酸，故爲特佳的肥料用原料。 (3 )於熔融鐵預備處理步驟中回收之後，至少於 1 3 0 0〜1 0 0 0 °C的溫度區域間以 1 〇 °C /分以上的冷卻速度 施行冷卻所得到之爐渣，且係由鹼性度（C a 0 / S i Ο 2 )爲 0 . 5 0 ~ 1 . 5的爐渣所構成的矽酸質肥料用原料。 於上述矽酸質肥料用原料中，就肥料之低鹼性化的觀 點考量，爐渣的鹼性度（C a 0 / S i Ο 2 )以1 . 2 4未滿爲佳。 又，就肥料之低鹼性化且得到矽酸之所要的溶解特性等 的觀點考量，爐渣的鹼性度（C a Ο / S i 0 2 )以◦ . 5 ◦以上、 1 . 2 4未滿爲佳。又，就提高肥料中的有效成分且提高矽 酸的溶出特性的觀點考量，爐渣的A 1 2 0 3含有量以1 0質 量％以下爲佳。 用作爲上述矽酸質肥料用原料之爐渣，由可容易地滿 足上述之爐渣的條件的觀點考量，以使用熔融鐵脫矽爐 渣爲佳。 上述矽酸質肥料用原料，可直接地用作爲矽酸質肥 料，或可用作爲矽酸質肥料的主原料。因而，本發明係 提供這樣的矽酸質肥料。 於將上述矽酸質肥料用原料作成爲矽酸質肥料之時， 以對矽酸質肥料用原料進行碎裂處理及/或整粒爲佳。 上述矽酸質肥料用原料，尤其是經碎裂處理及/或整粒 之矽酸質肥料用原料，以經過使用適當的黏合劑之造粒 步驟作成爲矽酸質肥料爲佳，這樣的矽酸質肥料，不易 10 200300134 發生施肥時的飛散、因雨水而流出、阻礙地面的透水性 及透氣性之問題。又，由於形狀規則且近於球狀，沒有 稜角，故取用性亦佳。 欲得到可滿足上述般的條件之矽酸質肥料用原料，以 下述製造方法爲佳。 (1 )於高爐熔融鐵的熔融鐵預備處理步驟中，經由對熔 融鐵供給氧源使熔融鐵中的矽氧化而生成矽酸，經由將 含有該矽酸的爐渣回收並使其固化，製得含有可溶性矽 酸 1 〇質量％以上之爐渣的矽酸質肥料用原料之製造方 法。 又，由上述的要點來看，此製造方法中之特佳的條件， 係如下述： (2 )於上述（1 )的製造方法中，經由將熔融鐵預備處理 步驟中所回收之鹼性度（c a〇/ S i〇2 )爲 0 . 5 2〜2 . 0的爐 渣，至少於1 3 0 0〜1 Q 0 ◦ °C的溫度區域之間以1 ◦ °C /分未 滿的冷卻速度使其固化，製得含有可溶性矽酸2 Q質量％ 以上之爐渣的矽酸質肥料用原料之製造方法。 (3 )於上述（1 )的製造方法中，經由將熔融鐵預備處理 步驟中所回收之鹼性度（Ca〇/ Si〇2)爲 0.49〜2.0的爐 渣，至少於1 3 0 0 ~ 1 0 0 ◦ °C的溫度區域之間以1 0 °C /分以 上的冷卻速度使其固化，製得含有可溶性矽酸2 0質量％ 以上之爐渣的矽酸質肥料用原料之製造方法。 (4 )於上述（1 )的製造方法中，經由將熔融鐵預備處理 步驟中所回收之鹼性度（C a〇/ S i〇2 )爲 0 · 5 0〜1 . 5的爐 11 200300134 渣，至少於1 3 ◦ 0〜1 ◦ ο 0 °c的溫度區域之間以1 ο Τ： /分以 上的冷卻速度使其固化，製得含有可溶性矽酸3 Q質量％ 以上之爐渣的矽酸質肥料用原料之製造方法。 (5 )於上述（1 )〜（4 )中任一的製造方法中，於對熔融鐵 添加C a 〇系造渣劑之同時，經由其添加量之調整，對回 收之爐渣的鹼性度（C a 0 / S i 0 2 )進行調整的矽酸質肥料 用原料之製造方法。 (6 )於上述（1 )〜（5 )中任一的製造方法中之熔融鐵預 備處理步驟係脫矽處理步驟的矽酸質肥料用原料之製造 方法。 又，用上述各製造方法中所得之矽酸質肥料用原料可 製造矽酸質肥料。因而，本發明亦提供如此的矽酸質肥 料之製造方法。又，於製造時，以施行對上述的矽酸質 肥料用原料的碎裂處理及/或整粒步驟、添加黏合劑之造 粒步驟爲佳。 如上述之本發明之矽酸質肥料用原料，由於可溶性矽 酸之含有量多且鹼性份少，且可直接利用熔融鐵預備處 理步驟中所生成的爐渣，而可用以極爲廉價地製得矽酸 質肥料。因此，可製得可代替習用的以高爐爐渣作爲原 料之矽酸質肥料的有用之矽酸質肥料，且，就可以有效 利用熔融鐵預備處理中所生成的爐渣的層面而言，甚具 有工業價値。又，依據本發明之矽酸質肥料用原料之製 造方法，可安定地製造方法所述的矽酸質肥料用原料。 實施方式 12 200300134 下面，就本發明之矽酸質肥料用原料及其製造方法的 詳細與較佳的實施形態加以說明，並就由該矽酸質肥料 用原料製得之矽酸質肥料及其製造方法加以說明。 本發明之矽酸質肥料用原料，係高爐熔融鐵的熔融鐵 預備處理步驟中所回收之爐渣；其係含有經由使熔融鐵 中的矽經氧化所生成之矽酸，且係由含有可溶性矽酸1 〇 質量％以上（而以2 0質量％以上更佳、尤以3 0質量％以上 爲特佳）之爐渣所構成。此處，所謂之可溶性矽酸，係指 可溶於 0 . 5莫耳的鹽酸溶液的矽酸（依據肥料公定分析 法）。 作爲用於本發明之矽酸質肥料用原料的爐渣，尤以高 爐熔融鐵的脫矽處理步驟中所回收之脫矽爐渣爲佳。於 作爲熔融鐵預備處理而施行的熔融鐵的脫磷處理中，熔 融鐵中的矽濃度愈低則脫磷處理效率可提高，故於脫磷 處理前須施行熔融鐵的脫矽處理。此脫矽處理，係在高 爐鑄床的熔融鐵桶內或熔融鐵裝盛容器內施行，藉由對 熔融鐵中，添加氧氣及氧化鐵等之氧源而進行。添加到 此熔融鐵中的氧源，會與熔融鐵中的矽反應生成矽酸， 生成含有此矽酸之所謂脫矽爐渣。此處，於自高爐放出 熔融鐵之時，會於排出熔融鐵之同時排出高爐爐渣 (Ca0-Si02-Al203-Mg0系爐渣），此高爐爐渣，雖可經 由設置於高爐爐渣鑄床之撈除器（s k i mm e r )使其與熔融 鐵分離，惟，部分的高爐爐渣無可避免地會流入到熔融 鐵裝盛容器中。因此，於上述脫矽處理後所回收的爐渣 13 200300134 (脫矽爐渣）’係由脫矽反應所生成的矽酸與高爐爐渣所 融合而成’其組成，係以矽酸爲主成份，並含有適量的 Ca〇、與少量的 Al2〇3、Mg〇、Mn〇、Fe〇等，又，可溶 性矽酸的含有量亦爲滿足於作爲矽酸質肥料之必須的水 準（10質量％以上）。 例如’一般的脫矽爐渣的組成，爲S i 〇 2 : 2 5〜5 0質量 %、 Ca〇：7 ·5 〜50 質量 ％、 MgO ： 0.5 〜3 質量％、Al2〇3: 1~5質量％、Mn〇: hi。質量％程度，鹼性度亦較高爐爐 渣低，通常係在0 · 3 ◦以上、1 · 2 4未滿的範圍內。因而， 將這樣的脫砂爐渣直接作爲原料的矽酸質肥料，較之以 局爐爐澄作爲原料之砂酸質肥料，其特徵在於，jg ◦ 2含 有量高（因而’可溶性S i 〇 2含有量亦高）、鹼性份低，並 且植物所不需要（依於情況甚至會有害）的A 1 2 〇 3的含 有量少，且含有對植物有用的微量成分之Mn0及，因 此’可謂是非常優異的矽酸質肥料。又，於脫矽處理係 在熔融鐵裝盛容器內進行的情況，經由將混入的高爐爐 渣進一步去除後進行脫矽處理，亦可得到矽酸含有量更 高的脫矽爐渣。 又，就使肥料作成爲低鹼性的觀點考量，用作爲矽酸 質肥料用原料的脫矽爐渣的鹼性度（Ca〇/si〇2)以m 未滿爲佳，而以1 · 0 0以下更佳，尤以〇 · 7 〇以下爲特佳。 脫砂爐澄的驗性度，可經由調整脫矽處理時的C a 〇系 造渣劑的添加量，或經由投與s i 0 2源等來調整。 又’於脫砂爐渣中所含有的A 1 2 〇 3爲植物所不要的成 14 200300134 分，A 1 2 0 3的含有量若多，肥料的有效成分量會相對地 減少。再者，A 1 2 Ο 3有阻礙矽酸的溶出性，且會將土壤 中的磷酸固定住作成爲植物無法利用的形態的顧慮，故 以儘量少爲佳。A 1 2 0 3的含有量若超過1 0質量％，則此 等問題有明顯化的顧慮，故A 1 2 0 3的含有量以作成爲1 0 質量％以下爲佳，而以5質量％以下更佳。通常，脫矽爐 渣中的A 1 2 0 3的大部分爲來自於高爐爐渣中，因而，經 由將與熔融鐵一起流入熔融鐵裝盛容器內之高爐爐渣在 脫矽處理前除去，可降低脫矽爐渣中的A 1 2 0 3含有量。 因此之故，相對於由高爐爐渣所構成的矽酸質肥料用原 料中通常含有1 4〜1 8質量％的A 1 2 Ο 3，本發明之矽酸質肥 料用原料中，A 1 2 Ο 3含有量可容易地作成爲5質量％以下。 矽酸質肥料，當然以可溶性矽酸的含有量高爲佳，惟， 依據本發明者等之檢討的結果，發現：於提高可溶性矽 酸的含有量之外，在爐渣（尤其是脫矽爐渣）的鹼性度 (C a Ο / S i〇2 )、甚至於回收後的爐渣的冷卻速度方面，亦 存在著較佳的條件。 圖1爲顯示高爐熔融鐵的脫矽處理步驟中所回收之各 種的鹼性度（C a 0 / S i Ο 2 )之爐渣，於將剛回收後的爐渣以 通常的方法徐徐地冷卻者，與以鐵板上排渣等的方法進 行急冷者，其等之鹼性度與矽酸可溶率（=(可溶性矽酸量 /總矽酸量）X 1 〇 〇 )間的關係經調查之結果者。又，圖2 爲顯示將圖1的結果以爐渣中的可溶性矽酸含有量來整 理者，圖3爲顯示將圖2的鹼性度（C a〇/ S i〇2 ) ·· 0 . 3〜0 · 7 15 200300134 的範圍擴大之曲線圖。 依據此等，作爲全體之爐渣鹼性度（c a 0 / S i 0 2 )若增 高，則矽酸可溶率亦增高。又，爐渣鹼性度若增高，雖 可溶性矽酸含有量會增加，惟，達到一定的鹼性度以上， 則由於全矽酸量減少之故而會減少。然而，於使回收的 爐渣徐徐地冷卻的情況，與急速冷卻的情況，於爐渣鹼 性度與可溶性矽酸含有量的關係上會有差異，且，尤其 是所得之可溶性矽酸含有量會相差甚大。亦即，於使回 收之爐渣徐徐冷卻之情況，於爐渣鹼性度：◦. 5 2〜2 . 0 的範圍中，可得到可溶性矽酸含有量：2 ◦質量％以上； 又，於爐渣鹼性度：〇 . 6 3 ~ 1 · 0的範圍中，可得到可溶 性矽酸含有量：3 0質量％以上。另一方面，於使回收之 爐渣急速冷卻之情況，於爐渣鹼性度：Q . 4 9〜2 · Q的範 圍中，可得到可溶性矽酸含有量：2 ◦質量％以上；又， 於爐渣鹼性度：〇 · 5 0〜1 . 5的範圍中，可得到可溶性矽 酸含有量：3 0質量％以上；且，於爐渣鹼性度：0 · 5 1 ~ 0 · 9 5 的範圍中，可得到可溶性矽酸含有量：4 0質量％以上。 於使這樣的脫矽處理步驟中所回收之爐渣以通常的形 態徐徐冷卻的情況，與使其急速冷卻的情況，皆可得到 高的可溶性矽酸含有量，良好適當的鹼性度的範圍。在 此特定的鹼性度的範圍下，可得到高的可溶性矽酸含有 量，理由據認係因：脫矽爐渣的主要礦物爲 S i長鏈的 C a S i 0 3 (矽灰石）之故，而有不易溶解的性質，鹼性度若 高，則矽酸的長鏈會被C a切斷，而使溶解性增高。 16 200300134 又，於使特定的鹼性度的爐渣急速冷卻的情況，與在 通常的形態下徐徐地冷卻的場合相比較，可溶性矽酸含 有量可大幅地增高。此情形，據認係因：經由使爐渣急 速冷卻，爐渣的組織會變成爲適於溶解性增高的玻璃構 造之故。 依本發明者等檢討之結果，發現：爲了得到圖1及圖 2所示般的效果，須使回收之爐渣至少在1 3 0 Q〜1 0 0 0 °C 的溫度區域（而以 1 4 ◦ 0 ~ 9 5 ◦ °C的溫度區域爲佳）間，以 1 ◦ °C /分以上（而以 2 0 °C /分以上爲佳）的冷卻速度進行 冷卻（急速冷卻）。此處所謂之 1 Q °C /分以上的爐渣的冷 卻速度，與通常的爐渣的冷卻形態（徐徐冷卻）相較，可 說是相當快速的冷卻速度。於這樣的冷卻條件下，藉由 使熔融體或於過冷卻液體溫度區域的爐渣急速冷卻，可 得到前述般的溶解性優異之爐渣組織。又，於上述溫度 區域外的冷卻條件，由於對形成的組織沒有大的影響， 故可爲任意的。 由上述的理由，於本發明中，經由下述（1 )或（2 )的爐 渣，可得到可溶性矽酸爲2 0質量％以上的矽酸質肥料用 原料。 (1 )於回收後，至少在 1 3 0 0〜1 0 0 0 °c的溫度區域間以 10 °c /分未滿的冷卻速度進行冷卻所得之爐渣，且鹼性度 (Ca〇/Si〇2)爲〇.52〜2.0白勺爐渣。 (2 )於回收後，至少在 1 3 0 0〜1 0 0 ◦ °C的溫度區域間以 1 〇 °C /分以上的冷卻速度進行冷卻所得之爐渣，且鹼性度 17 91132281 200300134 (Ca〇/Si〇2)爲0.49〜2.0白勺爐渣° 又，於本發明中，經由下述（3 )或（4 )的爐渣，可得到 可溶性矽酸爲3 0質量％以上的矽酸質肥料用原料。 (3 )於回收後，至少在 1 3 ◦ 0 ~ 1 0 0 0 °C的溫度區域間以 1 〇 °C /分未滿的冷卻速度進行冷卻所得之爐渣，且鹼性度 (Ca〇/ Si〇2)爲0.63 — 1.0白勺爐澄。 (4 )於回收後，至少在 1 3 ◦◦〜1 ◦◦ 0 °C的溫度區域間以 1 〇 °C /分以上的冷卻速度進行冷卻所得之爐渣，且鹼性度 (Ca〇/Si〇2)爲0.50 — 1.5白勺爐渣。 再者，於本發明中，經由下述（5 )的爐渣，可得到可溶 性矽酸爲4 0質.量％以上的矽酸質肥料用原料。 (5 )於回收後，至少在 1 3 0 0〜1 ◦ 0 0 °C的溫度區域間以 1 〇 °C /分以上的冷卻速度進行冷卻所得之爐渣，且鹼性度 (Ca〇/Si〇2)爲0.51-0.95的爐渣。 又，用以使回收之爐渣在上述特定的溫度區域中以上 述冷卻速度急速冷卻的具體方法，並無特別限定，可考 慮例如：經由對生成的爐渣以高壓空氣噴吹使其飛散， 在使爐渣冷卻之同時施行粒狀化的方法（高壓空氣粉碎 法）；經由對生成的爐渣以高壓水噴吹使其飛散，於使爐 渣冷卻之同時施行粒狀化的方法（高壓水粉碎法）；使生 成之爐渣流出到厚鋼板上，經由厚鋼板的強制冷卻與往 空氣中的放熱使爐渣冷卻的方法等，任一方法皆可。又， 於通常的冷卻形態之徐徐冷卻的情況，通常以爐渣皿容 納爐渣，然後，再排渣到爐渣處理場。 18 200300134 通常，肥料中的有效矽酸之可溶性矽酸的含有量’雖 可在Q · 5莫耳鹽酸溶液的強酸環境下測定（肥料公定分 析法），惟，吾等認爲實際上多數土壤爲pH 7程度的中 性環境，故上述可溶性矽酸量的測定値與實際作物的# 收未必有恆定的關連。因此，作爲矽酸質肥料的性能’ 在通常的〇 · 5莫耳鹽酸溶液中的矽酸的溶解性’和P H 7 附近的矽酸的溶解性兩者皆爲重要。經檢討的結果’發200300134 (ii) Description of the invention Technical field to which the invention belongs The present invention relates to raw materials for silicic acid fertilizers and to a method for producing the same. The prior art silicic fertilizer is mainly a fertilizer for the purpose of supplying silicic acid to rice. It contains soluble silicic acid at 10 mass% to 20 mass% or more, and alkaline content at 25 mass% to 3 Q mass% or more. It is used as paddy field. Soil conditioners for soil conservation and aging paddy fields are widely used. In recent years, the use of siliceous fertilizers to strengthen plants has been attracting attention, not only for rice but also for vegetables such as gherkins. Although siliceous fertilizers can also be made from wollastonite, which is a natural resource, most siliceous fertilizers today are manufactured using blast furnace slag as a raw material. To produce a siliceous fertilizer from blast furnace slag, for example, as shown in Japanese Patent Laid-Open No. 5 5-1 1 3 6 8 7, the molten blast furnace slag discharged from the blast furnace is slowly cooled and solidified. After drying the solidified block-shaped blast furnace slag, it is pulverized and adjusted to a desired particle size to produce a silicic acid fertilizer. However, the basicity of the blast furnace slag (C a Ο / S i Ο 2) promotes the desulfurization reaction in the blast furnace. Therefore, it is usually necessary to adjust it within the range of 1.2 2 to 1 · 26. Therefore, The alkalinity of the silicic acid fertilizer which uses a blast furnace slag as a raw material is naturally also in this range, and it becomes a fertilizer with a relatively large amount of alkalinity. In general, A1203 is contained in the blast furnace slag in an amount of about 13 to 15% by mass. Of course, such a large amount of A 1 2 0 3 is contained in the fertilizer. Therefore, by using such a silicic acid-based fertilizer, 7 200300134, when the silicic acid is administered to the soil, the alkaline material and A 1 2 0 3 are also administered. The original agricultural land in Yu Yueben is mostly acidic soil. Therefore, the use of the above-mentioned basic silicic acid fertilizer is suitable for the purpose of soil improvement. However, recently, with the increase in the amount of fertilizer starting with silicic fertilizer, the problem of acidic soil has been reduced. Therefore, it has been replaced by silicic fertilizer with more alkaline content. There is a need for silicic acid fertilizers with high silicic acid content and low alkaline content. In addition, A 1 2 03, which is contained in a large amount in the siliceous fertilizer using blast furnace slag as a raw material, is not an effective ingredient of the fertilizer. On the other hand, A 1 2 0 3 fixes phosphoric acid in the soil and becomes unusable by plants. The problem of the morphology, which may hinder the dissolution of silicic acid, has also been raised. SUMMARY OF THE INVENTION An object of the present invention is to provide a silicic acid that can be used to inexpensively obtain silicic acid (soluble silicic acid) with a large content and a low alkaline content (more preferably, the content of A 1 2 0 3 is small). Raw materials for silicic fertilizers for fertilizers. Another object of the present invention is to provide a method for producing a preferred raw material for silicic acid fertilizer for producing the raw material for silicic acid fertilizer. Another object of the present invention is to provide a silicic acid fertilizer using the raw material for silicic acid fertilizer and a method for producing the same. The inventors have repeatedly reviewed the raw materials for silicic acid fertilizers that meet the above requirements in terms of fertilizer composition and manufacturing costs. As a result, they have found that the specific properties recovered in the molten iron preliminary processing step using blast furnace molten iron The slag is excellent as a raw material for silicic fertilizer, and can be directly used as a raw material for silicic fertilizer without special treatment. It can also show excellent performance as a fertilizer. In addition, it was found that, among them, slag having a specific alkalinity is particularly preferable, and slag prepared under a specific cooling condition is more preferable, and can exhibit particularly excellent performance as a fertilizer. Based on such findings, the raw material for silicic acid fertilizer provided by the present invention is the slag recovered in the molten iron preliminary processing step of blast furnace molten iron; The generated silicic acid is composed of slag containing 10% by mass or more of soluble silicic acid. The content of the soluble silicic acid in the raw material for silicic acid fertilizer is preferably as high as possible, more preferably 20% by mass or more, and more preferably 3% by mass or more. Here, among the above-mentioned raw materials for siliceous fertilizers, the following (1) and (2) are preferable raw materials for fertilizers because they contain 20% by mass or more of soluble silicic acid. (1) After recovering in the molten iron preliminary treatment step, the slag obtained by performing cooling at a cooling rate of 10 ° C / min or less at a temperature region of at least 130 Q ~ 1 QQQ ° C is determined by A raw material for silicic acid fertilizer composed of slag having a basicity (C a 0 / S i 0 2) of 0.5 2 to 2.0. (2) After recovering in the molten iron preliminary treatment step, the slag obtained by performing cooling at a cooling rate of 10 ° C / min or more in a temperature range of at least 130 Q to 100 ° C, and A raw material for silicic acid fertilizer composed of slag having a basicity (C a 0 / S i 0 2) of 0.4 9 to 2.0. 9 200300134 In addition, among the above-mentioned raw materials for siliceous fertilizers, the following (3), because they contain 30% by mass or more of soluble silicic acid, are particularly good raw materials for fertilizers. (3) After recovering in the molten iron preliminary processing step, the slag obtained by performing cooling at a cooling rate of 10 ° C / min or more in a temperature range of at least 13,000 to 1 0 ° C, and A raw material for silicic acid fertilizer composed of slag having a basicity (C a 0 / S i Ο 2) of 0.5 0 to 1.5. Among the raw materials for silicic acid fertilizer mentioned above, considering the viewpoint of low alkalinity of the fertilizer, the basicity (C a 0 / S i 〇 2) of the slag is preferably less than 1.2. In addition, from the viewpoint of reducing the alkalinity of the fertilizer and obtaining the desired dissolution characteristics of silicic acid, the basicity of the slag (C a 0 / S i 0 2) is ◦. 5 ◦ or more, and 1.2 2 or less. Full is better. From the viewpoint of improving the effective ingredients in the fertilizer and improving the dissolution characteristics of the silicic acid, the content of A 1 2 0 3 in the slag is preferably 10% by mass or less. The slag used as the raw material for the siliceous fertilizer is preferably desmelted from the silicon slag by using molten iron from the viewpoint that the conditions of the slag described above can be easily satisfied. The above-mentioned raw materials for siliceous fertilizers can be used directly as siliceous fertilizers or can be used as the main raw materials of siliceous fertilizers. Therefore, the present invention provides such a siliceous fertilizer. When the above-mentioned raw material for a silicic fertilizer is used as a silicic fertilizer, it is preferable that the raw material for the silicic fertilizer is subjected to a shredding treatment and / or sizing. The above-mentioned raw materials for silicic acid fertilizer, especially the raw materials for silicic acid fertilizer which have been subjected to chipping treatment and / or whole grain, are preferably made into silicic acid fertilizer through a granulation step using an appropriate binder. Acid fertilizers are not easy. 10 200300134 Problems such as scattering during fertilization, outflow due to rain, and obstruction of water permeability and air permeability of the ground. In addition, since the shape is regular and nearly spherical, and has no edges and corners, it is also easy to use. To obtain a raw material for silicic acid fertilizer which can satisfy the above-mentioned conditions, the following production method is preferred. (1) In the molten iron preliminary processing step of blast furnace molten iron, silicon is oxidized by supplying an oxygen source to the molten iron to generate silicic acid, and slag containing the silicic acid is recovered and solidified to obtain Method for producing a raw material for silicic acid fertilizer containing slag of 10% by mass or more of soluble silicic acid. Further, from the above-mentioned points, the particularly preferable conditions in this manufacturing method are as follows: (2) In the manufacturing method of (1) above, the alkalinity recovered by the molten iron preliminary treatment step is (Ca〇 / S i〇2) Slag of 0.5 2 to 2.0, cooling at a temperature of less than 1 ° ° C / min to less than 1 300 ° C / min between the temperature range of 1 3 0 0 to 1 Q 0 A method for producing the raw material for silicic acid fertilizer containing slag containing 2 Q mass% or more of soluble silicic acid at a rate of solidification. (3) In the manufacturing method of the above (1), the slag having an alkalinity (Cao / Si〇2) recovered in the molten iron preliminary treatment step of 0.49 to 2.0 is less than 1 300 to 1 A method for manufacturing a raw material for silicic acid fertilizer containing slag containing 20% by mass or more of soluble silicic acid, which is solidified between a temperature range of 0 0 ° C and a cooling rate of 10 ° C / min or more. (4) In the manufacturing method of (1) above, the furnace 11 200300134 in which the alkalinity (C a0 / S i〇2) recovered in the molten iron preliminary treatment step is 0 · 50 to 1.5 is obtained. The slag is solidified in a temperature range of 1 3 ◦ 0 to 1 ◦ 0 ° C at a cooling rate of 1 ο: T / min or more to obtain silicon containing slag containing 3 Q mass% or more of soluble silicic acid. Method for producing raw materials for acid fertilizer. (5) In the production method of any one of (1) to (4) above, while adding a Ca 0-based slag-forming agent to the molten iron, the alkalinity of the recovered slag is adjusted by adjusting the amount of addition thereof. (C a 0 / S i 0 2) A method for producing a raw material for silicic acid fertilizer adjusted. (6) The molten iron preparation processing step in the manufacturing method of any one of (1) to (5) above is a method for manufacturing a raw material for siliceous fertilizer in a desiliconization step. In addition, the silicic acid fertilizer can be produced from the raw materials for silicic acid fertilizer obtained by the above-mentioned respective production methods. Therefore, the present invention also provides a method for manufacturing such a siliceous fertilizer. In addition, during the production, it is preferable to perform the shredding treatment and / or granulation step of the above-mentioned raw material for silicic fertilizer, and the granulation step of adding a binder. As described above, the raw material for silicic acid fertilizer of the present invention can be produced extremely cheaply because the content of soluble silicic acid is large and the alkaline content is small, and the slag generated in the molten iron preliminary processing step can be directly used. Silicate fertilizer. Therefore, a useful silicic acid fertilizer which can replace the conventional silicic acid fertilizer using blast furnace slag as a raw material can be obtained, and it is very industrial in terms of effectively utilizing the slag generated in the molten iron preliminary treatment. Price 値. In addition, according to the method for producing a raw material for silicic acid fertilizer according to the present invention, the raw material for silicic acid fertilizer described in the method can be stably produced. Embodiment 12 200300134 Next, the detailed and preferred embodiments of the raw material for silicic acid fertilizer and its manufacturing method according to the present invention will be described, and the silicic acid fertilizer made from the raw material for silicic acid fertilizer and its production method will be described. The manufacturing method will be explained. The raw material for silicic acid fertilizer according to the present invention is the slag recovered in the molten iron preliminary processing step of blast furnace molten iron; it contains silicic acid generated by oxidizing silicon in the molten iron, and contains soluble silicon The acid is composed of slag of 10 mass% or more (and more preferably 20 mass% or more, and particularly preferably 30 mass% or more). Here, the so-called soluble silicic acid refers to silicic acid that is soluble in a 0.5 mol hydrochloric acid solution (based on the public fertilizer analysis method). As the slag used as the raw material for the siliceous fertilizer of the present invention, the desilication slag recovered in the desilication treatment step of the blast furnace molten iron is particularly preferred. In the dephosphorization treatment of molten iron performed as a preliminary treatment of molten iron, the lower the silicon concentration in the molten iron, the higher the efficiency of the dephosphorization treatment. Therefore, the desiliconization treatment of the molten iron must be performed before the dephosphorization treatment. This desilication treatment is performed in a molten iron drum or a molten iron container in a blast furnace casting bed, and is performed by adding an oxygen source such as oxygen and iron oxide to the molten iron. The oxygen source added to this molten iron reacts with the silicon in the molten iron to form silicic acid, so-called desilication slag containing this silicic acid is formed. Here, when the molten iron is discharged from the blast furnace, the blast furnace slag (Ca0-Si02-Al203-Mg0 series slag) is discharged at the same time as the molten iron is discharged. Although the blast furnace slag can be removed through the blast furnace slag caster It separates it from the molten iron, but part of the blast furnace slag inevitably flows into the molten iron container. Therefore, the slag recovered after the above desilication treatment 13 200300134 (desilication slag) is a combination of silicic acid generated from the desilication reaction and blast furnace slag. Its composition is based on silicic acid and Contains an appropriate amount of Ca0 and a small amount of Al203, Mg0, Mn0, Fe0, etc., and the content of soluble silicic acid is also at a level that is necessary as a silicic fertilizer (10% by mass or more) . For example, the composition of a general desilication slag is Si 〇2: 25-50% by mass, Ca0: 7.5-50% by mass, MgO: 0.5-3% by mass, Al203: 1-5 Mass%, Mn0: hi. The degree of alkalinity is also high, and the slag is low. Usually, it is in the range of more than 0 · 3 ◦ and less than 1 · 24. Therefore, the silicic acid fertilizer using such desanding slag directly as a raw material is characterized in that the content of jg ◦ 2 is high (thus 'soluble S i 〇2'), compared with the sandy acid fertilizer using a local furnace smelting as a raw material. The content is also high), the alkaline content is low, and the amount of A 1 2 03 that is not needed by the plant (even depending on the situation) is small, and it contains Mn0 and the trace components useful to the plant, so 'can be described It is a very good silicic fertilizer. In the case where the desilication treatment is performed in a molten iron container, the desilication slag having a higher silicic acid content can be obtained by further removing the mixed blast furnace slag and then performing a desilication treatment. From the viewpoint of making the fertilizer low in alkalinity, the alkalinity (Ca0 / si〇2) of the desilication slag used as the raw material for the silicic acid fertilizer is preferably less than m, and 1 · 0 It is more preferably 0 or less, and particularly preferably 0.7 or less. The degree of verification of the desalination furnace can be adjusted by adjusting the amount of the Ca 0 slagging agent added during the desilication process, or by administering the si 0 2 source. In addition, A 1 2 0 3 contained in the desanding slag is an unnecessary component of the plant. 14 200300134 minutes, and if the content of A 1 2 0 3 is large, the amount of active ingredients of the fertilizer will be relatively reduced. In addition, A 1 2 0 3 has the concern that the dissolution of silicic acid is hindered, and the phosphoric acid in the soil is immobilized as a form that cannot be used by plants. Therefore, it is preferably as small as possible. If the content of A 1 2 0 3 exceeds 10% by mass, there is a concern that these problems will be apparent. Therefore, the content of A 1 2 0 3 is preferably 10% by mass or less, and 5% by mass The following is better. Generally, most of A 1 2 0 3 in the desiliconized slag comes from the blast furnace slag. Therefore, by removing the blast furnace slag flowing into the molten iron container together with the molten iron before the desilication treatment, the desiliconization can be reduced. A 1 2 0 3 content in silicon slag. Therefore, the raw material for siliceous fertilizer composed of blast furnace slag usually contains 14 to 18% by mass of A 1 2 0 3. Among the raw materials for siliceous fertilizer of the present invention, A 1 2 〇 The content of 3 can be easily made 5 mass% or less. Of course, the silicic acid fertilizer is preferably a high content of soluble silicic acid. However, according to the results of the review by the inventors, it was found that, in addition to increasing the content of soluble silicic acid, There are also better conditions for the basicity (C a 0 / S i 02) and even the cooling rate of the recovered slag. FIG. 1 shows various slags of basicity (C a 0 / S i Ο 2) recovered in the desiliconization step of the blast furnace molten iron, and the slag immediately after the recovery is slowly cooled by a normal method. The relationship between the alkalinity and the solubility of silicic acid (= (soluble silicic acid content / total silicic acid content) X 1 〇〇) and those subjected to rapid cooling by methods such as slag removal on iron plates, etc. The result. In addition, FIG. 2 shows the results of FIG. 1 organized by the content of soluble silicic acid in the slag, and FIG. 3 shows the basicity (C a0 / S i〇2) of FIG. 2. 0.3 ～ 0 · 7 15 200300134 A graph with an enlarged range. Based on these, if the slag basicity (c a 0 / S i 0 2) as a whole is increased, the solubility of silicic acid is also increased. In addition, if the basicity of the slag is increased, the content of soluble silicic acid will increase. However, when the alkalinity exceeds a certain level, the total silicic acid content will decrease, which will reduce it. However, in the case where the recovered slag is cooled slowly, and in the case of rapid cooling, there is a difference in the relationship between the slag basicity and the content of soluble silicic acid, and in particular, the content of the obtained soluble silicic acid is different. Very big. That is, in the case where the recovered slag is slowly cooled, the content of soluble silicic acid can be obtained in the range of slag basicity: ◦ 5 2 to 2.0: 2 ◦ mass% or more; Degree of sexuality: in the range of 0.6 3 to 1 · 0, a soluble silicic acid content can be obtained: 30% by mass or more. On the other hand, when the recovered slag is rapidly cooled, the content of soluble silicic acid can be obtained in the range of slag basicity: Q. 4 9 ~ 2 · Q: 2 ◦ mass% or more; Alkalinity: in the range of 0.5 to 0.5, soluble silicic acid content can be obtained: 30% by mass or more; and in the range of slag basicity: 0 · 5 1 to 0 · 9 5 , Soluble silicic acid content can be obtained: 40% by mass or more. When the slag recovered in such a desiliconization step is slowly cooled in a normal state, and when it is rapidly cooled, a high soluble silicic acid content and a range of good and appropriate alkalinity can be obtained. In this specific range of alkalinity, a high content of soluble silicic acid can be obtained. The reason is believed to be that the main mineral of the desiliconized slag is Si long chain C a Si 0 3 (Wollastonite). For this reason, it has a property of being difficult to dissolve. If the basicity is high, the long chain of silicic acid will be cut by Ca and the solubility will be increased. 16 200300134 In addition, when the slag having a specific alkalinity is rapidly cooled, the content of soluble silicic acid can be significantly increased as compared with the case where it is slowly cooled in a normal form. In this case, it is considered that the structure of the slag becomes a glass structure suitable for increasing the solubility by rapidly cooling the slag. According to the results of the review by the inventors, it was found that, in order to obtain the effect as shown in FIG. 1 and FIG. 2, the recovered slag must be at least in a temperature range of 1 3 0 Q to 1 0 0 0 ° C (and 1 4 ◦ A temperature range of 0 to 9 5 ◦ ° C is preferred, and cooling is performed at a cooling rate of 1 ◦ ° C / min or more (and preferably 20 ° C / min or more) (rapid cooling). The cooling rate of the slag, which is above 1 Q ° C / min, is considerably faster than the cooling mode (slow cooling) of ordinary slag. Under such cooling conditions, by rapidly cooling the melt or the slag in the temperature range of the supercooled liquid, a slag structure having excellent solubility as described above can be obtained. The cooling conditions outside the above-mentioned temperature range may be arbitrary because they do not have a large influence on the structure formed. For the reasons described above, in the present invention, a raw material for a silicic acid fertilizer having a soluble silicic acid content of 20% by mass or more can be obtained through the slag of the following (1) or (2). (1) After recycling, the slag obtained is cooled at a cooling rate of 10 ° c / min or less at least in a temperature range of 1300 ~ 100 ° C, and the alkalinity (Ca0 / Si 〇2) is from 0.52 to 2.0 slag. (2) After the recovery, the slag obtained by cooling at a cooling rate of 10 ° C / min or more in a temperature range of at least 1300 to 100 ° C, and the basicity of 17 91132281 200300134 (Ca 〇 / Si〇2) is 0.49 to 2.0. In the present invention, a silicic acid fertilizer with a soluble silicic acid content of 30% by mass or more can be obtained through the following (3) or (4) slag. With raw materials. (3) After the recovery, the slag obtained by cooling at least 10 ° C / min under a cooling rate of at least 13 ° 0 ~ 100 ° C, and the alkalinity (Ca〇 / SiO2) is from 0.63 to 1.0. (4) After the recovery, the slag obtained by cooling at a cooling rate of 10 ° C / min or more in a temperature range of at least 13 ° C to 1 ° C at least 0 ° C, and the basicity (Ca0 / Si 〇2) is 0.50-1.5 slag. Furthermore, in the present invention, a raw material for a silicic acid-based fertilizer having a soluble silicic acid content of 40% by mass or more can be obtained through the slag of the following (5). (5) After the recovery, the slag obtained by cooling at a cooling rate of 10 ° C / min or more in a temperature range of at least 1300 to 1 ° 0 ° C, and the basicity (Ca0 / Si 〇2) Slag of 0.51-0.95. The specific method for rapidly cooling the recovered slag at the above-mentioned cooling rate in the specific temperature range is not particularly limited. For example, the generated slag may be sprayed with high-pressure air and scattered, and the Granulation method (high-pressure air pulverization method) while cooling the slag; spraying the generated slag with high-pressure water to disperse it, and granulating the slag while cooling (high-pressure water pulverization method); Any method may be used, such as a method of flowing the generated slag onto a thick steel plate, and cooling the slag by forced cooling of the thick steel plate and heat release to the air. In the case of slow cooling in the normal cooling mode, the slag is usually contained in a slag dish, and then discharged to the slag processing plant. 18 200300134 Generally, the content of soluble silicic acid in effective silicic acid in fertilizers can be measured under the strong acid environment of Q · 5 Mol hydrochloric acid solution (fertilizer analysis method), but we think that most soils are actually It is a neutral environment with a pH of about 7, so the above-mentioned determination of the amount of soluble silicic acid may not be constantly related to the # harvest of actual crops. Therefore, both the performance of the silicic acid fertilizer, the solubility of silicic acid in a normal 0.5 mol hydrochloric acid solution, and the solubility of silicic acid near Ph 7 are important. The result of the review ’
現：本發明之矽酸質肥料用原料，於通常的土壤的P H ^ P Η 7附近之矽酸溶解性（於中性區域的溶解性）’較習用 的高爐噴水粉碎爐渣所構成之矽酸質肥料用原料格外的 高。本發明者等，於具體地就0 . 2 Μ磷酸鹽溶液（Ρ Η 7 ) 中的砂酸溶解率加以確認的例子中’習用的咼爐噴水敕； 碎爐渣所構成之砂酸質肥料用原料，僅得到〇 · 1 %程度的 溶解率’相對於此，本發明之矽酸質肥料’則得到 〇 · 9 %〜4 . 3 %的高溶解率。又，其中尤以經過於Now: the raw material for silicic acid fertilizer of the present invention, the solubility of silicic acid (solubility in the neutral region) near the pH ^ P Η 7 of ordinary soil is better than the silicic acid composed of conventional blast furnace water spray slag The raw materials for high-quality fertilizers are exceptionally high. The present inventors and others have specifically confirmed examples of the dissolution rate of oxalic acid in a 0.2 M phosphate solution (P '7). For the raw materials, only a dissolution rate of about 0.1% is obtained. In contrast, the siliceous fertilizer of the present invention has a high dissolution rate of 0.9% to 4.3%. Moreover, among them
13 ◦ ◦〜1 ◦ Q0 °c的溫度區域間以1 〇 °c /分以上的冷卻速度 冷卻（急速冷卻）所得之爐渣，由其所構成者，尤其可得 到高溶解率。 上述之本 爲矽酸質肥 而作成矽酸 是經碎裂處 當的黏合劑 樣的矽酸質 發明之矽酸質肥料用原料，可直接使用作成 料’或經施以碎裂處理及/或整粒（粒度調整） 實肥料。又，上述矽酸質肥料用原料，尤其 莲及/或整粒的矽酸質肥料用原料，以使用適 趣經過造粒步驟而作成矽酸質肥料爲佳，這 肥料，不易發生施肥時的飛散、因雨水而流 19 200300134 出、阻礙地面的透水性及透氣性之問題。又，由於形狀 規則且近於球狀，沒有棱角，故取用性亦佳。 又，亦可對本發明之矽酸質肥料用原料配合以其他的 添加成分作爲矽酸質肥料。 其次，就本發明之矽酸質肥料用原料的製造方法加以 說明。 圖4爲顯示依據本發明之矽酸質肥料用原料之製造方 法的一實施形態者，圖中所示之設備係熔融鐵的脫矽處 理設備。用以容納自高爐（未圖示）流出之熔融鐵2的鍋 型的熔融鐵裝盛容器1，係搭載於台車3上可移送到圖4 所示之脫矽處理設備處。此脫矽處理設備中，裝備有自 上部吹下的氧氣配管6與噴射配管7。此等自上部吹下 的氧氣配管6及噴射配管7係可上下移動，可插入熔融 鐵裝盛容器1中使用。 自貯藏槽1 0的粉體狀的固體氧源5、自貯藏槽1 1的 粉體狀的造渣劑8 ( C a 0系造渣劑）及自貯藏槽1 2的粉體 狀的成分調整劑9，係分別供給到上述噴射配管7中。 此等粉體，可在單獨或混合狀態下經由作爲輸送氣體的 氮氣而供給到噴射配管7，自其前端吹入熔融鐵2中進 行添加。此情況，若調整噴射配管7的前端位置，亦可 將上述粒狀體吹入到脫矽爐渣4中。又，亦可經由使噴 射配管7的前端配置於脫矽爐渣4的上方之特定高度 處，將上述粒狀體投射到脫矽爐渣4的表面而進行添加。 又，圖中13〜15爲用以自貯槽（lifttank)lO〜12釋 20 200300134 出粉體的貯槽，1 6爲配料器（d i s p e n s e r )。貯藏槽1 〇 內的固體氧源5、貯藏槽1 1內的造渣劑8、與貯藏槽1 2 內的成分調整劑9，經由貯槽1 3〜1 5，可在分別獨立地 控制添加量及添加時間而進行吹送，又，亦可自噴射配 ' 管7單獨吹入氮氣對熔融鐵2進行攪拌。 此處’上述固體氧源5用以使熔融鐵2中的矽氧化而 添加者’可使用軋鐵氧化皮（mill scale)或鐵礦石等 的鐵氧化物。 前述造渣劑8，係用以與經由脫矽處埋所生成的矽酸 鲁 开夕成化合物，使生成的脫砂爐渣4的熔點降低的目的而 添加者，通常係使用C a 0。又，亦有爲了得到攪拌效果 或抑制爐渣的起泡而投入石灰石的情形。 上遮成分調整劑9，係用以調整生成之脫矽爐渣4的 成分而添加者，例如於矽酸質肥料中含有Fe2〇3、Mg〇、 心〇等的情況，可分別以鐵礦石、重燒菱鎂礦（magnesia ^ ^ker)、錳礦石等之含有所要的成分之物質作爲成分 調：劑9而添加。藉此’可使生成之脫矽爐渣4作成爲 · ,勺組成。又，於欲增加s 1 〇2成分的量之情況，可用 夕^或矽石等之含有si〇2的物質作爲成分調整劑9而添 加。p如此般，成分調整劑9，可因應於所須目的而使用 由Ρ%〇3、Mg0、Mn〇、Si〇2等之丄種以上作爲主成份的 物質。 於脫砂處理設備中，更進〜步一倂設置有由漏斗. 1 7 〜]q 9、自此等漏斗將原料釋出之裝置2〇〜η、釋出之. 21 200300134 原料（固體氧源、造渣劑、成分調整劑）的移送裝置2 3、 將用以原料裝入熔融鐵裝盛容器1內的斜管2 4所構成之 原料供給設備A，經由此原料供給設備A，可將漏斗1 7 內的固體氧源5、漏斗1 8內的造渣劑8及漏斗1 9內的 成分調整劑9，分別自上部添加到熔融鐵裝盛容器1內。 作爲此由上部添加之固體氧源5、造渣劑8及成分調整 劑9，可用通常之塊狀者。 於圖4所示般的脫矽處理設備中，固體氧源5、造渣 劑8及成分調整劑9之供給到熔融鐵裝盛容器1內，可 施行經由上述噴射配管7之吹入添加及經由上述原料供 給設備之由上部添加之任一者或兩者。 下面，就使用上述脫矽處理設備施行熔融鐵的脫矽處 理，以製造矽酸質肥料用原料之脫矽爐渣的方法加以說 明。 雖是在熔融鐵裝盛容器 1內施行熔融鐵 2的脫矽處 理，惟，爲了正確地掌握所生成之脫矽爐渣4的組成， 以在脫矽處理之前即掌握脫矽處理前之存在於高爐爐渣 的量及組成爲佳。此高爐爐渣的量，可經由爐渣厚度的 測定或覆蓋住熔融鐵2的液面之爐渣的面積率的目視觀 察等加以掌握。爐渣組成，雖可經由化學分析來把握， 惟，在經驗上，對其組成大致了解的情況，並不需要化 學分析。 於脫矽處理中，例如：於將固體氧源5自斜管2 4由上 部添加到熔融鐵裝盛容器1內之同時，自上部吹送氧氣 22 200300134 配管6將氧氣吹送到熔融鐵2的液面，再自噴射配管7 將氮氣吹入，使熔融鐵2與固體氧源5進行攪拌混合。 經由如此作法，氧氣與固體氧源5中的氧會與熔融鐵2 中的矽反應生成矽酸。生成之矽酸，與上述之高爐爐渣 混合·融合，於熔融鐵2上生成以矽酸爲主成分之脫矽 爐渣4。 此情況，爲了使生成之脫矽爐渣4低熔點化，以透過 噴射配管7或斜管24添加造渣劑8爲佳。又，透過噴 射配管7吹入固體氧源5亦可。於使用粉體狀的造渣劑 8及粉體狀的固體氧源5的情況，與使用塊狀者相比較， 反應界面面積增大，可迅速且安定地實施脫矽處理。 脫矽爐渣4的組成，會受生成之矽酸量所左右。因而， 須依據脫矽處理前的熔融鐵2的矽濃度與脫矽處理後的 熔融鐵2的目標矽濃度，而設定氧氣及固體氧源5的使 用總量。其時，於使用氧氣的情況，熔融鐵2的溫度會 上昇，另一方面，於使用固體氧源5的情況，熔融鐵2 的溫度會降低，故氧氣與固體氧源5的配合比率，宜在 使添加之氧成份量成爲同一之條件下，依於熔融鐵2的 溫度作適當的變更，例如於溫度條件條件良好的情況 中，亦可單獨使用固體氧源5。 又，須依於生成之矽酸的量及原來存在的高爐爐渣的 量，以使生成之脫矽爐渣4的鹼性度成爲在上述之較佳 範圍中的方式來決定造渣劑 8 ( C a 0系造渣劑）的添加 量。通常，鹼性度若未滿1 · 2 4，固可得到鹼性份少的矽 23 200300134 酸質肥料，惟，調整造渣劑8的添加量降低脫矽爐渣4 的鹼性度，可得到更低鹼性的矽酸質肥料。又，於調整 MgO等的成分調整劑的情況，須透過噴射配管7或斜管 2 4添加所需的成分調整劑9。 如此作法，熔融鐵2經脫矽處理，於熔融鐵2上生成 矽酸質肥料組成的脫矽爐渣 4。脫矽處理終了後，將脫 矽爐渣4自熔融鐵裝盛容器1取出，使其冷卻並固化。 冷卻·固化，可於自熔融鐵裝盛容器1取出時施行，亦 可於容納到容器中後，自該容器取出時施行亦可。 作爲冷卻固化之方法，如前面所述般，熔融體或於過 冷卻液體溫度區域進行急速冷卻的情況，可採用例如： 經由對生成的爐渣4以高壓空氣噴吹使其飛散，在使爐 渣冷卻之同時施行粒狀化的方法（高壓空氣粉碎法）；經 由對生成的脫矽爐渣4以高壓水噴吹使其飛散，於使爐 渣冷卻之同時施行粒狀化的方法（高壓水粉碎法）；使生 成之爐渣4流出到厚鋼板上，經由厚鋼板的強制冷卻與 往空氣中的放熱使爐渣冷卻的方法等的方法。又，於徐 徐冷卻的情況，係以爐渣皿容納爐渣，然後，再排渣到 爐渣處理場。 經過這樣的冷卻·固化可得到矽酸質肥料用原料之脫 矽爐渣。 又，上述所說明之實施形態雖係在熔融鐵裝盛容器 1 內進行脫矽處理者，惟，脫矽處理並非限定於上述實施 形態，亦可爲對自高爐送出熔融鐵經撈除機與高爐爐渣 24 200300134 分離後的高爐鑄床桶內或傾注桶內的熔融鐵2添加氧氣 或固體氧源來進行的脫矽處理。惟，此情況，由於高爐 爐渣的混入量無法即時把握，故須以經驗上可把握之高 爐爐渣的混入量爲基準來決定造渣劑的添加量。 又，上述說明之實施形態雖係用鍋型的熔融鐵裝盛容 器1的脫矽處理，惟，熔融鐵裝盛容器1並非限定於上 述的鍋型者，亦可使用如混鐵車（torpedo car )等之任 意的熔融鐵裝盛容器。又，脫矽處理設備的詳細及攪拌 氣體的吹入方式等亦非限定於上述實施形態中。 又，經脫矽處理之熔融鐵，亦可爲事先施以脫硫處理 者。 以上述般的作法所製造之矽酸質肥料用原料，其粒度 若適當，則可直接作爲矽酸質肥料，而冷卻·固化後的 形狀爲塊狀等的情況中，須施行碎裂處理及/或整粒（經 由篩別等作粒度調整）作成矽酸質肥料。又，必要時，亦 可配合以其他的添加成分作成矽酸質肥料。 矽酸質肥料用原料的碎裂（粉碎）方法並無特別限定， 可採用任何方法。例如可用顎式粉碎機、棒型硏磨機、 輪碾機、葉輪粉碎機等之粉碎機進行粉碎處理。又，整 粒可用任意的篩別裝置施行，亦可於對矽酸質肥料用原 料施行粉碎處理再進行整粒。 又，經碎裂處理及/或整粒之矽酸質肥料用原料，以用 適當的黏合劑並經造粒步驟作成矽酸質肥料爲佳，如此 作法所造粒成的矽酸質肥料，不易發生施肥時的飛散、 25 200300134 因雨水而流出、阻礙地面的透水性及透氣性之問題。又， 由於形狀規則且近於球狀’沒有稜角，故取用性亦佳。 造粒方法，並無特別限定，可採用一般的造粒方法， 例如：可採用使經由上述粉碎處理得到之粉碎物與黏合 劑用混合機混合，於一邊加入適量的水之下以造粒機施 行造粒’然後施行乾燥的方法。 作爲造粒機’可使用通常所使用者，例如：旋轉皿型 造粒機、旋轉圓筒型造粒機等，以將造粒後仍未進入所 要的粒度範圍者，直接或經粉碎等之處理後再度混合 機’作爲原料的一部份再利用之連續造粒方法爲佳。 圖5爲顯示本發明之矽酸質肥料用原料的造粒步驟的 一例者’經由上述粉碎處理所得之粉碎物（矽酸質肥料用 原料）2 5經由鏟斗機等裝入漏斗2 6，經計量之粉碎物2 5 自漏斗2 6透過輸送帶2 7供給到桶式旋轉造粒機2 8。並 將貯留在容器3 G之黏合劑2 9供給既定量到此桶式旋轉 造粒機2 8 ’對此桶式旋轉造粒機2 8中，經由桶式旋轉 造粒機2 8之旋轉，將粉碎物2 5與黏合劑2 9混合並進 行造粒。然後，以乾燥機3 1將造粒物乾燥，經由升降機 3 2供給到筛別裝置3 3進行篩別，再以冷卻器：3 4冷卻成 爲造粒肥料。又，亦可於冷卻器3 4冷卻後進行篩別作成 造粒肥料。 圖6爲顯示本發明之矽酸質肥料用原料的造粒步驟的 其他例者，經由上述粉碎處理得到之粉碎物2 5裝入漏斗 3 6中，經計量之粉碎物2 5則自漏斗3 6裝入到混合機 26 200300134 3 9中。又，貯留於容器3 8之黏合劑3 7亦定量地裝入混 合機3 9中。然後，粉碎物2 5與黏合劑3 7於混合機3 9 中混合，此混合物被供給到皿形造粒機4 0中，在此皿形 造粒機4 0中進行造粒。使皿形造粒機4 0中造粒所成之 造粒物載置於輸送帶4 1上，之後，與圖5的步驟同樣地， 於乾燥機3 1中進行乾燥，經由升降機3 2供給到篩別裝 置3 3進行篩別，再於冷卻器3 4中冷卻作成造粒肥料。 造粒步驟中所用的黏合劑，並無特別限定，可使用例 如：選自磷酸、黏土、膨潤土、聚乙烯醇、羧甲基纖維 素、聚丙烯酸、糖蜜、木質素、硫酸鎂、澱粉等之中的 1種以上作單獨或混合使用，惟，就造粒性與施肥後之 肥料粒子的崩解性考量，以澱粉、硫酸鎂、木質素爲適 合，由選自此等之中之1種以上作爲黏合劑的主成份來 使用爲佳。 於製造以矽酸質肥料用原料進行造粒之造粒物的肥料 的情況，作爲黏合劑所須要求的特性，可舉出：Φ可得 到優異的造粒性；②於施肥後，肥料粒子（造粒物）可容 易地崩解分散到土壤中；③具有適當的硬度，可於製造 方法中及自販售到施肥之間的操作中不會崩解；④黏合 劑成分調整劑對於包含土壤之環境不會有不良影響等。 上述澱粉、硫酸鎂、木質素可完全滿足此等諸特性。又， 其中尤以使用澱粉的情況，其所造粒之肥料粒子的硬度 特別高，且，澱粉會溶解於雨水及土壤中的水分，以適 度的速度使肥料粒子崩解，故爲特佳。又，由於澱粉可 27 200300134 經由添加水分而糊化，經由其後使其乾燥而固化，故造 粒性優異，且可被土壤中的微生物等分解，因此不會對 植物及環境造成不良影響。 作爲黏合劑使用之澱粉，可舉出：以玉米、木薯、小 麥、馬鈴薯、米等爲原料所作成者。此等澱粉中，其構 成成分之直鏈澱粉（d -葡萄糖接合成直鏈狀者）與支鏈 澱粉（d -葡萄糖接合成分枝狀者）的比例依於原料而 異，糯米及黑玉米等爲直鏈澱粉的比例較多。再者，作 爲澱粉的種類，原本的生澱粉、或經熱或酸、鹼、鹽、 酵素等處理之加工澱粉皆可。此等澱粉，不論其種類， 具有糊化的性質者皆適於作爲造粒黏合劑。 如此作法所造粒之矽酸質肥料的平均粒徑以〇 . 5〜6 mm 爲佳。平均粒徑若未滿Q . 5 mm，則施肥時會被風吹起致 使用性差，另一方面，若超過6 mm，則難以均一地散布。 更佳之粒徑爲1〜5 m TTI。 又，本發明之矽酸質肥料用原料之爐渣，於熔融鐵預 備處理步驟中並不須施行特別的處理（例如：於製造鉀肥 之情況之添加鉀原料、或施行用以使此鉀原料熔融的附 屬步驟），只須施行原來的熔融鐵預備處理步驟即可得 到。 實施例 (實施例1 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 28 200300134 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲1 5 ◦噸，熔融鐵組成爲，碳：4 · 5質量％、矽： 0.25質量％、磷：0.1Q5質量％、硫：0.032質量％、熔 融鐵溫度爲 1 1 4 1 °C。前步驟得到之高爐爐渣（C a 0 : 4 2 質量 ％、 S i 0 2 ： 33 質量 ％、MgO ： 7 質量 ％、Al2〇3: 15 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲3 6 0 kg。 以0 . 0 3質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 1 5 Q N m 3、鐵礦石燒結粉總量定爲 1 9 ◦ 0 k g。並以Q . 5 5作爲生成的脫矽爐渣的鹼性度之目 標値來決定作爲造渣劑之生石灰的添加量，將生石灰添 加量定爲3 0 0 k g。 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：9 0 0〜9 2 ◦ N m 3 / h r )連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：180~200kg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：20~40kg /分）與氮氣一起經由噴射配管 連續地吹送到熔融鐵中，以 1 〇分鐘的時間完成脫矽處 理。脫矽處理後的熔融鐵中矽濃度爲Q . 〇 3質量％，脫矽 處理後的熔融鐵溫度區域爲1 3 8 Q °C。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 製的鍋（以下記爲鑄鋼鍋）內。然後，使脫矽爐渣流入設 29 200300134 置於建構屋內之以厚度1 5〜2 0 mm的厚鋼板構築底面及側 面的鐵箱內，使其固化·冷卻，得到1 3 4 2 k g的塊狀爐 渣（矽酸質肥料用原料）。將此塊狀爐渣加以碎裂成粒徑 2 mm以下作成矽酸質肥料。此矽酸質肥料的成分分析値 示如表1。如表1所示般，所得之矽酸質肥料，爲S i Ο 2 含有量：5 5 . 4質量％、鹼性度：0 · 5 5、矽酸可溶率（對 可溶性矽酸的全矽酸份的比例：S - S i 0 2 / S i 0 2 ) : 3 9質 量％。 (實施例2 ) ' 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 5 0噸，熔融鐵組成爲，碳：4 . 7質量％、矽： 0.24質量％、磷：0.103質量％、硫·· 0.042質量％、熔 融鐵溫度爲 1 3 9 5 °C。前步驟得到之高爐爐渣（C a 0 : 4 4 質量％、 S i 0 2 : 35 質量 ％、MgO ： 6 質量 ％、A 1 2 〇 3 : 1 3 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 Q Q kg。 以0 . 1 2質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 7 4 N m3、鐵礦石燒結粉總量定爲 1 1 0 Q k g。並以Q . 7 5作爲生成的脫矽爐渣的鹼性度之目 標値來決定作爲造渣劑之生石灰的添加量，將生石灰添 30 200300134 加量定爲220kg。 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：8 5 0〜9 5 0 N m 3 / h r )連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：200〜24Qkg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：4 G〜5 0 k g /分）與氮氣一起經由噴射配管 連續地吹送到熔融鐵中，以 5分鐘的時間完成脫矽處 理。脫矽處理後的熔融鐵中矽濃度爲〇 . 1 2質量％，脫矽 處理後的熔融鐵溫度區域爲1 3 3 7 X：。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，使脫矽爐渣流入設置於建構屋內之以厚度 1 5〜2 0 mm的厚鋼板構築底面及側面的鐵箱內，使其固 化·冷卻，得到9 5 5 kg的塊狀爐渣（矽酸質肥料用原料）。 將此塊狀爐渣加以碎裂成粒徑2 mm以下，作成矽酸質肥 料。此矽酸質肥料的成分分析値示如表1。如表1所示 般，所得之矽酸質肥料，爲S i 0 2含有量：4 1 . 3質量％、 鹼性度：〇 · 7 5、矽酸可溶率：8 1質量％。 (實施例3 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 5 Q噸，熔融鐵組成爲，碳：4 · 4質量％、矽： 〇.20質量％、磷·· 0·100質量％、硫：0.030質量％、熔 31 200300134 融鐵溫度爲 1 4 Q Q t：。前步驟得到之高爐爐渣（C a Ο : 4 2 質量 ％、 S i Ο 2 : 33 質量 ％、M g Ο · 6 質量 ％、A 1 2 〇 3 * 1 3 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲3 7 0 kg。 以0 . 1 2質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 5 5 N m3、鐵礦石燒結粉總量定爲 7 0 0 k g。並以1 . 0 3作爲生成的脫矽爐渣的鹼性度之目標 値來決定作爲造渣劑之生石灰的添加量，將生石灰添加 量定爲225kg° 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：6 Q 0〜6 5 0 N m 3 / h r )連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：120~140kg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：40〜50kg /分）與氮氣一起經由噴射配管 連續地吹送到熔融鐵中，以 5分鐘的時間完成脫矽處 理。脫矽處理後的熔融鐵中矽濃度爲〇 . 1 2質量％，脫矽 處理後的熔融鐵溫度區域爲1 3 7 0 °C。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，使脫矽爐渣流入設置於建構屋內之以厚度 1 5〜2 0 mm的厚鋼板構築底面及側面的鐵箱內，使其固 化·冷卻，得到7 6 8 kg的塊狀爐渣（矽酸質肥料用原料）。 將此塊狀爐渣加以碎裂成粒徑2 mm以下，作成矽酸質肥 料。此矽酸質肥料的成分分析値示如表1。如表1所示 32 200300134 般，所得之矽酸質肥料，爲s i 0 2含有量：4 1 . 0質量％、 鹼性度：1 · 0 3、矽酸可溶率：7 6質量％。 (實施例4 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 5 0噸，熔融鐵組成爲，碳：4 · 5質量％、矽： 0.24質量％、磷：0·1〇5質量％、硫：Q.041質量％、熔 融鐵溫度爲 1 3 9 2 °C。前步驟得到之高爐爐渣（C a Ο : 4 4 質量 ％、 S i Ο 2 ： 36 質量 ％、Mg 0 ： 6 質量 ％、A 1 2 〇 3 : 1 3 質量％)流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 5 Q kg。 以0 . 1 2質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 7 4 N m3、鐵礦石燒結粉總量定爲 1 1 0 Q k g。並以1 . 3作爲生成的脫矽爐渣的鹼性度之目標 値來決定作爲造渣劑之生石灰的添加量，將生石灰添加 量定爲513kg。 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：8 5 ◦〜9 5 0 N m 3 / h r )連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：200~240kg/分），且自上部添加作爲造渣劑之生 石灰中的 2 5 0 kg之同時，將剩餘的生石灰（生石灰添加 200300134 速度：4 0〜5 5 k g /分）與氮氣一起經由噴射配管連續地吹 送到熔融鐵中，以5分鐘的時間完成脫矽處理。脫矽處 理後的熔融鐵中矽濃度爲〇 . 1 2質量％，脫矽處理後的熔 融鐵溫度區域爲1 3 3 7 °C。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，使脫矽爐渣流入設置於建構屋內之以厚度 1 5〜2 0 mm的厚鋼板構築底面及側面的鐵箱內，使其固 化·冷卻，得到 1 2 8 0 kg的塊狀爐渣（矽酸質肥料用原 料）。將此塊狀爐渣加以碎裂成粒徑 2 mm以下，作成矽 酸質肥料。此矽酸質肥料的成分分析値示如表1。如表1 所示般，所得之矽酸質肥料，爲S i Ο 2含有量：3 1 . 0質 量％、鹼性度：1 . 2 7、矽酸可溶率：7 8質量％。 (實施例5 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 5 Q噸，熔融鐵組成爲，碳：4 · 4質量％、矽： 0.14質量％、磷：Q.1Q5質量％、硫：0.040質量％、熔 融鐵溫度爲 1 4 0 0 °C。前步驟得到之高爐爐渣（C a 0 : 4 3 質量 ％、 S i Ο 2 : 34 質量 ％、MgO ： 6 質量 ％、A12〇3: 12 質量％)流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲3 8 0 kg。 以Q . Q 7質量％作爲脫矽處理後的熔融鐵中矽濃度的目 34 200300134 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 4 7 N m3、鐵礦石燒結粉總量定爲 6 0 4 k g。並以1 . 6作爲生成的脫矽爐渣的鹼性度之目標 値來決定作爲造渣劑之生石灰的添加量，將生石灰添加 量定爲400kg° 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：5 5 0 ~ 5 7 0 N m 3 / h 3：)連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：110~13Qkg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：70〜90kg /分）與氮氣一起經由噴射配管 連續地吹送到熔融鐵中，以 5分鐘的時間完成脫矽處 理。脫矽處理後的熔融鐵中矽濃度爲Q . Q 7質量％，脫矽 處理後的熔融鐵溫度區域爲1 3 8 0 °C。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，使脫矽爐渣流入設置於建構屋內之以厚度 1 5〜2 0 mm的厚鋼板構築底面及側面的鐵箱內，使其固 化·冷卻，得到9 4 1 k g的塊狀爐渣（矽酸質肥料用原料）。 將此塊狀爐渣加以碎裂成粒徑2 mm以下，作成矽酸質肥 料。此矽酸質肥料的成分分析値示如表1。如表1所示 般，所得之矽酸質肥料，爲S i 0 2含有量：3 2 _ 3質量％、 鹼性度：1 . 6 2、矽酸可溶率：8 3質量％。 (實施例6 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 35 200300134 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲1 5 0噸，熔融鐵組成爲，碳：4 . 2質量％、矽： 0.26質量％、磷：Q.10Q質量％、硫：0..038質量％、熔 融鐵溫度爲 1 4 1 ◦ t：。前步驟得到之高爐爐渣（C a Ο : 4 2 質量 ％、 S i 0 2 : 34 質量 ％、MgO ： 7 質量 ％、A 1 2 〇 3 : 1 5 質量％)流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 Q 0 kg。 以〇 . Q 7質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 1 3 1 N m3、鐵礦石燒結粉總量定爲 1689kg。又，爲了使矽酸質肥料的MgO含有量增高爲7 質量％以上，而添加作爲成分調整劑之培燒白雲石 (dolomite) 1 8 9 k g，並以◦· 5作爲生成的脫矽爐渣的 鹼性度之目標値來決定作爲造渣劑之生石灰的添加量， 將生石灰添加量定爲1 Q 〇kg。 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：7 0 0〜9 0 0 Nm3/hr)連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：1 6 0〜1 8 Q kg /分），且將作爲造渣劑之生石灰（生 石灰添加速度：1 〇 kg /分）和作爲成分調整劑之培燒白雲 石粉（培燒白雲石粉添加速度：18〜20kg /分）與氮氣一起 經由噴射配管連續地吹送到熔融鐵中，以1 0分鐘的時間 完成脫矽處理。脫矽處理後的熔融鐵中矽濃度爲 〇_〇7 36 200300134 質量％，脫矽處理後的熔融鐵溫度區域爲 1 3 8 0 °C。又， 於培燒白雲石 189kg中，Mg〇份爲 79kg，Ca〇份爲 1 1 0 k g 〇 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內，然後，經由高壓空氣粉碎法使其冷卻·固化，得 到1 3 2 6 k g的粒徑3 mm以下的粒狀爐渣（矽酸質肥料用原 料），直接用其作爲矽酸質肥料。此矽酸質肥料的成分分 析値示如上述之表1。如表1所示般，所得之矽酸質肥 料，爲Si02含有量：51.1質量％、鹼性度：0.50、矽 酸可溶率：64質量％。 (實施例7 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲1 5 0噸，熔融鐵組成爲，碳：4 · 2質量％、砂： 0.25質量％、磷：0.1Q0質量％、硫：0.038質量％、熔 融鐵溫度爲 1 4 0 0 °C。前步驟得到之高爐爐渣（CaO : 42 質量 ％、 S i 0 2 : 34 質量 ％、 MgO ： 7 質量 ％、Al2〇3: 15 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 0 0 kg。 以Q . 0 7質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 4 3 9 N m3、鐵礦石燒結粉總量定爲 37 200300134 1 5 8 2 k g。又，爲了使矽酸質肥料的 M g 0含有量增高爲 1〇質量％以上，而添加作爲成分調整劑之培燒白雲石 3 4 3 k g，並以0 . 6 6作爲生成的脫矽爐渣的鹼性度之目標 値來決定作爲造渣劑之生石灰的添加量，將生石灰添加 量定爲l〇〇kg。 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：1 4 7 0〜1 4 8 Q N m 3 / h r )連續地吹送到熔融熔融鐵液 面，並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添 加速度：310〜32Qkg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：2Qkg/分）和作爲成分調整劑之培燒白雲 石粉與氮氣一起經由噴射配管連續地吹送到熔融鐵中， 以5分鐘的時間完成脫矽處理。脫矽處理後的熔融鐵中 矽濃度爲〇 . 〇 7質量％，脫矽處理後的熔融鐵溫度區域爲 1380 °C。又，於培燒白雲石343kg中，Mg〇份爲143kg， Ca〇份爲 200kg 0 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，經由高壓空氣粉碎法使其冷卻·固化，得 到1 4 4 6 k g的粒徑3 mm以下的粒狀爐渣（矽酸質肥料用原 料），直接用其作爲矽酸質肥料。此矽酸質肥料的成分分 析値示如表1。如上述之表1所示般，所得之矽酸質肥 料，爲S i〇2含有量：4 4 · 4質量％、鹼性度：0 . 6 6、矽 酸可溶率：99質量％。 (實施例8 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 38 200300134 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 2 5噸，熔融鐵組成爲，碳：4 · 2質量％、矽： 0.18質量％、磷：0.105質量％、硫：0.038質量％、熔 融鐵溫度爲 1 3 9 ◦ °C。前步驟得到之高爐爐渣（C a 0 : 4 3 質量 ％、 S i 02 ： 3 4 質量 ％、MgO ： 7 質量 ％、Al2〇3: 12 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 Q Q kg。 以Q . 〇 7質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 6 6 N m3、鐵礦石燒結粉總量定爲 8 52kg 〇又，爲了使石夕酸質月巴料的Mg〇含有量增高爲10 質量％以上，而添加作爲成分調整劑之培燒白雲石 2 5 7 kg，並以0 . 9 5作爲生成的脫矽爐渣的鹼性度之目標 値來決定作爲造渣劑之生石灰的添加量，將生石灰添加 量定爲l〇〇kg。 脫矽處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：8 0 0〜9 0 0 N m 3 / h r )連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：160〜18Qkg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：2 0 kg /分）和作爲成分調整劑之培燒白雲 石粉（培燒白雲石粉添加速度：4Q~6Qkg /分）與氮氣一起 經由噴射配管連續地吹送到熔融鐵中，以5分鐘的時間 39 200300134 完成脫矽處理。脫矽處理後的熔融鐵中矽濃度爲 〇.〇7 質量％，脫矽處理後的熔融鐵溫度區域爲1 3 8 0 °c。又， 於培燒白雲石257kg中，Mg〇份爲 107kg，Ca〇份爲 150kg。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，經由高壓空氣粉碎法使其冷卻·固化，得 到1 Q 5 3 k g的粒徑3 mm以下的粒狀爐渣（矽酸質肥料用原 料），直接用其作爲矽酸質肥料。此矽酸質肥料的成分分 析値示如上述之表1。如表1所示般，所得之矽酸質肥 料，爲Si02含有量：37.3質量％、鹼性度：0.95、矽 酸可溶率：99質量％。 (實施例9 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 2 5噸，熔融鐵組成爲，碳：4 . 2質量％、矽： 0.26質量％、磷：0.105質量％、硫：0.038質量％、熔 融鐵溫度爲 1 3 9 (TC。前步驟得到之高爐爐渣（C a Ο : 4 4 質量 ％、 S i 0 2 : 35 質量 ％、MgO ： 7 質量 ％、A 1 2 〇 3 : 1 2 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 0 Q kg。 以Q . 0 7質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 40 200300134 將氧氣總量定爲 1 Q 9 N m3、鐵礦石燒結粉總量定爲 14 0 7kg。又，爲了使矽酸質肥料的 M g 0含有量增高爲 1 〇質量％以上，而添加作爲成分調整劑之培燒白雲石 2 5 7 k g，並以0 . 6 6作爲生成的脫矽爐渣的鹼性度之目標 値來決定作爲造渣劑之生石灰的添加量，將生石灰添加 量定爲 100kg° 脫砍處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：1 2 Q 0〜1 4 0 Q N m 3 / h r )連續地吹送到熔融熔融鐵液 面，並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添 加速度：260〜3QQkg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：2 ϋ k g /分）和作爲成分調整劑之培燒白雲 石粉（培燒白雲石粉添加速度〜60kg /分）與氮氣一起 經由噴射配管連續地吹送到熔融鐵中，以5分鐘的時間 完成脫矽處理。脫矽處理後的熔融鐵中矽濃度爲 Q . 〇 7 質量％，脫矽處理後的熔融鐵溫度區域爲1 3 9 Qt。又， 於培燒白雲石257kg中，Mg〇份爲 107kg，Ca〇份爲 1 5 0 kg ° 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內。然後，使脫矽爐渣流入設置於建構屋內之以厚度 1 5〜2 0 mm的厚鋼板構築底面及側面的鐵箱內，使其固 化·冷卻，得到 1 2 8 2 kg的塊狀爐渣（矽酸質肥料用原 料）。將此塊狀爐渣加以碎裂成粒徑 2 mm以下，作成矽 酸質肥料。此矽酸質肥料的成分分析値示如表1。如表1 所示般，所得之矽酸質肥料，爲S i 0 2含有量：4 5 . 5質 41 200300134 量％、鹼性度：0.66、矽酸可溶率：70質量％。 (實施例1 〇 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 5 0噸，熔融鐵組成爲，碳：4 · 7質量％、矽： 0.24質量％、磷：Q.103質量％、硫：0.042質量％、熔 融鐵溫度爲 1 3 9 5 °C。前步驟得到之高爐爐渣（C a Ο : 4 3 質量 ％、 S i 02 ： 35 質量 ％、MgO ： 7 質量 ％、Al2〇3: 12 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 ◦ 0 kg。 以0 . 0 9質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 1 〇 4 N m3、鐵礦石燒結粉總量定爲 1 3 3 3 kg。又，以0 · 5 1作爲生成的脫矽爐渣的鹼性度之 目標値來決定作爲造渣劑之生石灰的添加量，將生石灰 添加量定爲145kg。 脫砂處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：1 2 0 0〜1 3 0 0 N m 3 / h 3Γ )連續地吹送到熔融熔融鐵液 面，並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添 加速度：25 3〇0kg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：25〜35kg /分）與氮氣一起經由噴射配管 連續地吹送到熔融鐵中，以 5分鐘的時間完成脫矽處 42 200300134 理。脫矽處理後的熔融鐵中矽濃度爲〇 . 〇 9質量％，脫矽 處理後的熔融鐵溫度區域爲1 3 9 Q °C。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內，然後，經由高壓空氣粉碎法使其冷卻·固化，得 到1 1 ◦ Okg的粒徑3mm以下的粒狀爐渣（矽酸質肥料用原 料），直接用其作爲矽酸質肥料。此矽酸質肥料的成分分 析値示如上述之表1。如表1所示般，所得之矽酸質肥 料，爲Si02含有量：48.8質量％、驗性度：0.51、石夕 酸可溶率：99質量％。 (實施例1 1 ) 使用圖4所示之脫矽處理設備，施行熔融鐵的脫矽處 理以製造作爲矽酸質肥料用原料的脫矽爐渣，由此脫矽 爐渣製得矽酸質肥料。 將得自高爐之熔融鐵移送到脫矽處理設備中。熔融鐵 重量爲 1 5 0噸，熔融鐵組成爲，碳：4 · 4質量％、矽： 0.16質量％、磷：0.100質量％、硫：0.030質量％、熔 融鐵溫度爲 1 4 0 0 t：。前步驟得到之高爐爐渣（C a 0 : 4 3 質量 ％、 Si〇2: 34 質量 ％、MgO ： 7 質量 ％、A 1 2 0 3 · 12 質量％ )流入到熔融鐵裝盛容器中，此高爐爐渣量，由爐 渣的厚度之測定結果推算爲4 0 0 kg。 以Q . Q 7質量％作爲脫矽處理後的熔融鐵中矽濃度的目 標値來決定氧氣與固體氧源之鐵礦石燒結粉的添加量， 將氧氣總量定爲 62Nm3、鐵礦石燒結粉總量定爲 8 0 0 k g。又，以0 . 9 9作爲生成的脫矽爐渣的鹼性度之目 43 200300134 標値來決定作爲造渣劑之生石灰的添加量，將生石灰添 加量定爲25Qkg。 脫砂處理，係自由上部吹下之氧氣配管使氧氣（氧氣流 量：7 ◦◦〜8 ◦ 0 N m 3 / h r )連續地吹送到熔融熔融鐵液面， 並連續地自上部添加鐵礦石燒結粉（鐵礦石燒結粉添加 速度：150〜17Qkg/分），且將作爲造渣劑之生石灰（生 石灰添加速度：4Q〜60kg /分）與氮氣一起經由噴射配管 連續地吹送到熔融鐵中，以 5分鐘的時間完成脫矽處 理。脫矽處理後的熔融鐵中矽濃度爲Q . Q 7質量％，脫矽 處理後的熔融鐵溫度區域爲1 3 8 CTC。 然後，將生成之脫矽爐渣，以搔刮機進行搔刮到鑄鋼 鍋內，然後，經由高壓空氣粉碎法使其冷卻·固化，得 到9 1 0 kg的粒徑3 mm以下的粒狀爐渣（矽酸質肥料用原 料），直接用其作爲矽酸質肥料。此矽酸質肥料的成分分 析値示如表1。如表1所示般，所得之矽酸質肥料，爲 S i〇2含有量：4 0 · 6質量％、鹼性度：0 · 9 9、矽酸可溶率： 9 9質量％。 44 200300134 鹼性度 ΓΟ •X LD LT) if) 卜 m 〇 r- CN] rH CM \o 〇 LO LD σ\ KD 1~1 L0 Ch 〇 ο t~1 rH 〇 〇 〇 〇 〇 ο CN •Η CO /Si〇2 σ\ η rH 00 V£) O 00 卜 Γ0 00 V£) Ch σ\ σ\ σ\ 〇 l> σ\ σ\ σ\ σ\ 1 ω ο ο 〇 o o 〇 〇 ο o ο 〇 矽酸質肥料的化學組成（質量％) CM X C? •Η ω 1 U) V£) LO rH CN 00 I> σ> 00 m CN rH CN ΓΟ ΓΟ \~1 m 寸 CN U) CM CN m m 寸 VD m rH ro CO 寸 〇 Α12〇3 KD m cn o\ CN rH 00 ο 寸 CO \D ΓΟ 寸 LO \> 寸 ΓΟ 寸 m m 寸 (ϋ CN CM ro 00 oo LO LD LO Εη ΓΟ V£) ro 寸 ro 寸 寸 寸 Μη〇 00 00 00 Γ0 CO If) 寸· LO if) CN LO CN Γ0 〇g 寸 寸 寸· 寸· 寸 MgO ι~1 Ch 1~1 id CM LO rH i~i CN Γ0 r- Γ Ο rH ΓΟ \—1 rH ϋΊ σ\ KD 〇 \—1 r- CN Ca〇 η 〇 CM Γ0 Γ0 ι> m 寸 00 σ» OQ ο Γ〇 tH Γ0 03 寸 cy\ Γ0 CN LO LO CN σ\ CN LD Γ0 σ\ CN 寸 CN] 〇 c? •Η ω 寸 m o o Γ0 t"·1 寸 Γ0 LD CO \D LD U1 tH 1~1 rH rn CM cn rH LO Γ ΟΟ if) 00 〇 爐渣之冷卻 條件*1 徐冷 徐冷 徐冷 徐冷 徐冷 急冷 急冷 急冷 徐冷 急冷 急冷 實施例1 實施例2 實施例3 實施例4 實施例5 實施例6 實施例7 實施例8 實施例9 實施例10 實施例11 fN〇TS/〇fduΓη-Κτκιφ/ροτ :变# •伥φ/ροτ :资· 越滕菝变^酲筠11侧1|£00〇070 0 2迄劍鹦^荽回1^ 200300134 (實施例1 2 ) 就實施例 3、4、6、8的矽酸質肥料與由高爐高壓水 粉碎爐渣所得之矽酸質肥料於中性域的溶解性加以調 查。將各矽酸質肥料1 g，於由磷酸一銨與磷酸二銨所調 製成的0 · 2 Μ磷酸鹽溶液（p Η 7 ) 1 5 ◦ m 1中振動萃取出。此 萃取係於3 (TC下進行1小時，由濾液中的矽酸濃度求出 在中性域的矽酸之溶解率。其結果示如表2。 如表2所示般，在中性域（p Η 7 )的溶解率，相對於由 高爐高壓水粉碎爐渣所製得之矽酸質肥料爲〇 . 1 %，於本 發明之矽酸質肥料，得到 Q . 9〜4 · 3 %的高數値。又，其 中尤以由在1 3 0 ◦ ~ 1 0 ◦ 0 °C的溫度區域間以1 ◦ °C /分以上 的冷卻速度進行冷卻（急速冷卻）所得之爐渣所成者，可 得到高的溶解率。13 ◦ ◦ ~ 1 ◦ The slag obtained by cooling (rapid cooling) at a cooling rate of 10 ° C / min or more between the temperature range of Q0 ° C, in particular, can obtain a high dissolution rate. The above-mentioned silicic acid fertilizer is made of silicic acid, which is a binder-like silicic acid-based silicic acid fertilizer raw material for invention, which can be used directly as a raw material 'or after being subjected to the chipping treatment and / Or whole grain (size adjustment) solid fertilizer. In addition, the raw materials for the silicic acid fertilizer, especially the raw materials for the silicic acid fertilizer of lotus and / or whole grain, are preferably made of the silicic acid fertilizer through the granulation step of Shiqu, which is not easy to occur when fertilizing Scattered, flowing due to rainwater 19 200300134, obstructing water permeability and air permeability of the ground. In addition, since the shape is regular and nearly spherical, and has no edges and corners, it is easy to use. Further, the raw material for silicic acid fertilizer of the present invention may be blended with other added ingredients as silicic acid fertilizer. Next, a method for producing a raw material for siliceous fertilizer according to the present invention will be described. Fig. 4 shows an embodiment of a method for manufacturing a raw material for siliceous fertilizer according to the present invention. The equipment shown in the figure is a desilication processing equipment for molten iron. A pot-type molten iron container 1 for containing molten iron 2 flowing from a blast furnace (not shown) is mounted on a trolley 3 and can be transferred to a desilication treatment facility shown in FIG. 4. This desilication treatment equipment is provided with an oxygen pipe 6 and a jet pipe 7 blown from above. The oxygen pipe 6 and the jet pipe 7 blown from above are movable up and down, and can be inserted into a molten iron container 1 for use. Powdery solid oxygen source 5 from storage tank 10, powdery slagging agent 8 (C a 0 slagging agent) from storage tank 1 1 and powdery components from storage tank 12 The regulator 9 is supplied to each of the above-mentioned injection pipes 7. These powders can be supplied to the injection pipe 7 via nitrogen gas as a transport gas in a single or mixed state, and blown into the molten iron 2 from the front end to be added. In this case, if the front end position of the injection pipe 7 is adjusted, the granules can be blown into the desilication slag 4. Further, it may be added by arranging the tip of the injection pipe 7 at a specific height above the desilication slag 4 and projecting the granular material onto the surface of the desilication slag 4. 13 to 15 in the figure are storage tanks for releasing powder from lift tanks 10 to 12 20 200300134, and 16 is a dispenser (d i s p en n s e r). The solid oxygen source 5 in the storage tank 10, the slag-forming agent 8 in the storage tank 11 and the component adjusting agent 9 in the storage tank 1 2 can be controlled independently through the storage tanks 1 to 15 The molten iron 2 may be blown by adding the blowing time, and the molten iron 2 may be stirred by blowing nitrogen alone from the spray pipe 7. Here, "the above-mentioned solid oxygen source 5 is used to oxidize silicon in the molten iron 2 and the adder" may be an iron oxide such as a mill scale or iron ore. The slag-forming agent 8 is added for the purpose of reducing the melting point of the generated desalination slag 4 by forming compounds with the silicic acid formed by burying the desiliconization site. Generally, C a 0 is used. In addition, in some cases, limestone is added in order to obtain a stirring effect or to suppress slag foaming. The upper cover component adjuster 9 is added to adjust the components of the desiliconized slag 4 to be generated. For example, when the silicic acid fertilizer contains Fe203, Mg0, and core 0, iron ore can be used. , Reburned magnesia (magnesia ^ ker), manganese ore, and other substances containing the desired components are added as a component adjustment: agent 9 and added. By this means, the generated desilication slag 4 can be made into a spoon. When it is desired to increase the amount of the s 1 02 component, a material containing SiO 2 such as yam or silica can be added as the component modifier 9. In this way, the component adjusting agent 9 can be used as a main component of one or more kinds of P% 03, Mg0, Mn0, Si02, etc. according to the required purpose. In the sand removal processing equipment, it is further advanced ~ a step is provided by a funnel. 1 7 ~) q 9, the device for releasing the raw materials from these funnels 20 ~ η, release it. 21 200300134 Raw material (solid oxygen source, slag-forming agent, component adjusting agent) transfer device 2 3. Raw material supply equipment A consisting of a slanted tube 2 4 for filling raw materials into a molten iron container 1 The raw material supply device A can add the solid oxygen source 5 in the funnel 17, the slagging agent 8 in the funnel 18, and the component adjusting agent 9 in the funnel 19 to the molten iron container 1 from above. As the solid oxygen source 5, the slag-forming agent 8, and the component adjusting agent 9 added from the upper part, ordinary ones can be used. In the desiliconization equipment shown in FIG. 4, the supply of the solid oxygen source 5, the slag-forming agent 8, and the component adjusting agent 9 is supplied into the molten iron container 1, and the blowing and adding through the spray pipe 7 and the Either or both of them are added from above through the raw material supply equipment. Next, a method for desilication treatment of molten iron using the above desilication treatment equipment to produce a desilication slag of a raw material for silicic fertilizer will be described. Although the desilication treatment of the molten iron 2 is performed in the molten iron container 1, in order to accurately grasp the composition of the desilication slag 4 generated, it is necessary to grasp the existence before the desilication treatment before The amount and composition of the blast furnace slag is preferred. The amount of the blast furnace slag can be grasped by measuring the thickness of the slag or visually observing the area ratio of the slag covering the liquid surface of the molten iron 2. Although the composition of the slag can be grasped through chemical analysis, empirical understanding of its composition does not require chemical analysis. In the desiliconization process, for example, while adding a solid oxygen source 5 from the inclined pipe 24 to the molten iron container 1 from the upper part, blowing oxygen from the upper part 22 200300134 The pipe 6 blows oxygen to the liquid of the molten iron 2 Then, nitrogen is blown in from the spray pipe 7 to stir and mix the molten iron 2 and the solid oxygen source 5. By doing so, the oxygen in the solid oxygen source 5 will react with the silicon in the molten iron 2 to form silicic acid. The generated silicic acid is mixed and fused with the above-mentioned blast furnace slag, and a desilication slag 4 containing silicic acid as a main component is formed on the molten iron 2. In this case, in order to reduce the melting point of the generated desilication slag 4, it is preferable to add the slag-forming agent 8 through the injection pipe 7 or the inclined pipe 24. Alternatively, the solid oxygen source 5 may be blown through the injection pipe 7. In the case of using the powdered slag-forming agent 8 and the powdered solid oxygen source 5, the reaction interface area is increased compared with those using a block, and the desiliconization treatment can be performed quickly and stably. The composition of the desilication slag 4 is influenced by the amount of silicic acid produced. Therefore, the total amount of oxygen and solid oxygen source 5 to be used must be set according to the silicon concentration of the molten iron 2 before the desiliconization process and the target silicon concentration of the molten iron 2 after the desiliconization process. At this time, when oxygen is used, the temperature of the molten iron 2 rises. On the other hand, when using the solid oxygen source 5, the temperature of the molten iron 2 decreases. Therefore, the mixing ratio of oxygen to the solid oxygen source 5 is appropriate. Under the condition that the amount of the added oxygen component is the same, the temperature of the molten iron 2 is appropriately changed. For example, when the temperature condition is good, the solid oxygen source 5 may be used alone. In addition, the slag-forming agent 8 (C must be determined in such a way that the alkalinity of the generated desilication slag 4 falls within the above-mentioned preferred range, depending on the amount of silicic acid generated and the amount of blast furnace slag originally present. a 0-based slagging agent). Generally, if the alkalinity is less than 1 · 2 4, silicon with low alkalinity can be obtained. 23 200300134 Acidic fertilizer, but by adjusting the addition amount of slagging agent 8 to reduce the alkalinity of desilication slag 4, we can obtain Less alkaline siliceous fertilizer. When adjusting a component adjusting agent such as MgO, it is necessary to add a required component adjusting agent 9 through a spray pipe 7 or an inclined pipe 2 4. In this way, the desilication treatment of the molten iron 2 produces a desilication slag 4 composed of a siliceous fertilizer on the molten iron 2. After the desilication process is completed, the desilication slag 4 is taken out of the molten iron container 1 and allowed to cool and solidify. Cooling and solidification can be performed when the container 1 is taken out from the molten iron container, or after being contained in the container, it can also be performed when the container is taken out. As the cooling and solidifying method, as described above, when the melt is rapidly cooled in the temperature region of the supercooled liquid, for example, the generated slag 4 is sprayed with high-pressure air to be scattered, and the slag is cooled. A granulation method (high-pressure air pulverization method) is simultaneously performed; a granulation method (high-pressure water pulverization method) is performed while cooling the slag while spraying the generated desilication slag 4 with high-pressure water to disperse it. ; A method of flowing the generated slag 4 onto a thick steel plate, and cooling the slag by forced cooling of the thick steel plate and exothermic heat into the air; In the case of cooling, the slag is contained in a slag dish, and then discharged to the slag treatment plant. After such cooling and solidification, a desilication slag of a raw material for siliceous fertilizer can be obtained. In addition, although the embodiment described above is a desilication treatment in the molten iron container 1, the desilication treatment is not limited to the above embodiment, and the molten iron delivered from the blast furnace may be removed by a removing machine and Blast furnace slag 24 200300134 Desiliconization of molten iron 2 in the separated blast furnace caster barrel or pouring barrel by adding oxygen or a solid oxygen source. However, in this case, since the mixing amount of blast furnace slag cannot be grasped in real time, it is necessary to determine the addition amount of the slagging agent based on the amount of blast furnace slag mixing that can be grasped empirically. In addition, although the embodiment described above is a desilication treatment using a pot-shaped molten iron container 1, the molten iron container 1 is not limited to the above-mentioned pot type, and a mixed iron car (torpedo car) and any other molten iron container. The details of the desilication processing equipment and the method of blowing the agitated gas are not limited to the above-mentioned embodiments. Further, the molten iron subjected to desiliconization treatment may be a person who has been subjected to desulfurization treatment in advance. If the particle size of the silicic acid fertilizer produced by the above-mentioned method is appropriate, it can be directly used as silicic acid fertilizer. If the shape after cooling and solidification is lumpy, etc., it must be crushed and / Or whole grain (size adjustment through sieve etc.) to make silicic fertilizer. In addition, if necessary, other additives can also be used to make silicic acid fertilizer. The method for crushing (pulverizing) the raw material for siliceous fertilizer is not particularly limited, and any method can be adopted. For example, a pulverizing process may be performed using a pulverizer such as a jaw pulverizer, a rod honing machine, a wheel mill, and an impeller pulverizer. In addition, the whole granules can be processed by any sieving device, or the raw materials for silicic fertilizer can be crushed and then granulated. In addition, the raw material for the silicic acid fertilizer after the chipping treatment and / or the whole granule is preferably made into a silicic acid fertilizer through a granulation step using an appropriate binder, and the silicic acid fertilizer granulated in this way, Scattering during fertilization is difficult to occur, 25 200300134 The outflow due to rainwater, and the problems of water permeability and air permeability of the ground are hindered. In addition, since the shape is regular and nearly spherical, there are no edges and corners, so it is easy to use. The granulation method is not particularly limited, and a general granulation method can be adopted. For example, a granulator obtained by mixing the pulverized material obtained through the above-mentioned pulverization treatment with a binder and adding an appropriate amount of water to the granulator can be used A granulation process is performed and then a drying process is performed. As the granulator, it can be used by ordinary users, such as a rotary dish granulator, a rotary cylindrical granulator, etc., so that those that have not entered the desired particle size range after granulation can be directly or pulverized. A continuous granulation method in which the mixer is reused as a part of the raw materials after processing is preferred. FIG. 5 shows an example of the granulation process of the raw material for silicic acid fertilizer according to the present invention. The crushed product (raw material for silicic acid fertilizer) 2 obtained through the above-mentioned pulverizing treatment is loaded into a hopper 2 6 through a bucket machine or the like The measured pulverized material 2 5 is supplied from the hopper 2 6 to the barrel-type rotary granulator 2 8 through the conveyor belt 2 7. And the adhesive 2 9 stored in the container 3 G is supplied to the barrel rotary granulator 2 8 ′ to the barrel rotary granulator 2 8 via the rotation of the barrel rotary granulator 28 The pulverized material 25 and the binder 29 are mixed and granulated. Then, the granulated material is dried with a dryer 31, and is supplied to a screening device 33 through a lifter 32 to be screened, and then cooled with a cooler: 3 4 to be granulated fertilizer. In addition, after the cooler 34 is cooled, it may be sieved to produce granulated fertilizer. FIG. 6 shows another example of the granulation step of the raw material for silicic acid fertilizer according to the present invention. The pulverized material 25 obtained through the above-mentioned pulverizing treatment is charged into the funnel 3 6 and the measured pulverized material 25 is from the funnel 3 6 Load into mixer 26 200300134 3 9. Further, the binder 37 stored in the container 38 is also quantitatively charged into the mixer 39. Then, the pulverized material 25 and the binder 37 are mixed in a mixer 39, and the mixture is supplied to a dish granulator 40, and granulated in the dish granulator 40. The granulated material granulated in the dish-shaped granulator 40 is placed on a conveyor belt 41, and thereafter, dried in a dryer 31 as in the procedure of FIG. 5 and supplied through an elevator 32. It is screened in the screening device 3 3, and then cooled in a cooler 34 to make granulated fertilizer. The binder used in the granulation step is not particularly limited. For example, a binder selected from the group consisting of phosphoric acid, clay, bentonite, polyvinyl alcohol, carboxymethyl cellulose, polyacrylic acid, molasses, lignin, magnesium sulfate, and starch can be used. One or more of them are used alone or in combination. However, in consideration of granulation and disintegration of fertilizer particles after fertilization, starch, magnesium sulfate, and lignin are suitable. One of these is selected from these. The above is preferably used as the main component of the adhesive. In the case of manufacturing fertilizers for granulated materials that are granulated with raw materials for silicic fertilizers, the characteristics required for the binder include: Φ can obtain excellent granulation properties; ② Fertilizer particles after fertilization (Granulated matter) can easily disintegrate and disperse into the soil; ③ have appropriate hardness, can not disintegrate in the manufacturing method and the operation from self-sale to fertilization; ④ the binder component adjuster for containing soil The environment will not have adverse effects. The above-mentioned starch, magnesium sulfate, and lignin can fully satisfy these characteristics. Among them, starch is particularly used, and the hardness of the granulated fertilizer particles is particularly high, and starch dissolves in rainwater and moisture in the soil, and disintegrates the fertilizer particles at a moderate rate, which is particularly preferable. In addition, since starch can be gelatinized by adding water, and then dried and solidified, it has excellent granulation properties and can be decomposed by microorganisms in the soil, so it does not adversely affect plants and the environment. Examples of the starch used as a binder include those made from corn, cassava, wheat, potato, and rice. Among these starches, the proportion of amylose (d-glucose-linked amylose) and amylopectin (d-glucose-linked component dendrite) as constituents varies depending on raw materials, such as glutinous rice and black corn. The proportion of amylose is large. In addition, as the kind of starch, raw raw starch or processed starch processed by heat or acid, alkali, salt, enzyme, etc. may be used. These starches, regardless of their type, have gelatinizing properties and are suitable as granulation binders. The average particle size of the silicic acid fertilizer granulated in this way is 0. 5 ~ 6 mm is better. If the average particle size is less than Q. 5 mm, it will be blown by the wind during fertilization, resulting in poor usability. On the other hand, if it exceeds 6 mm, it will be difficult to spread uniformly. A more preferred particle size is 1 to 5 m TTI. In addition, the slag of the raw material for siliceous fertilizer according to the present invention does not need to be subjected to special treatment in the molten iron preliminary processing step (for example, a potassium raw material is added in the case of manufacturing potassium fertilizer, or the potassium raw material is melted Ancillary steps), only need to perform the original molten iron pre-treatment step. EXAMPLES (Example 1) Using the desilication treatment equipment shown in FIG. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing 28 200300134 slag to obtain silicic acid. Quality fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of molten iron is 15 ◦ tons. The composition of molten iron is: carbon: 4.5% by mass, silicon: 0. 25% by mass, phosphorus: 0. 1Q5 mass%, sulfur: 0. 032% by mass, and the molten iron temperature was 1 1 4 1 ° C. The blast furnace slag (C a 0: 4 2 mass%, S i 0 2: 33 mass%, MgO: 7 mass%, Al203: 15 mass%) obtained in the previous step flows into a molten iron container, and the blast furnace The amount of slag is estimated from the measurement result of the thickness of the slag to be 360 kg. With 0. 0.3% by mass is used as the target concentration of silicon in the molten iron after desiliconization to determine the amount of iron ore sintering powder added to oxygen and solid oxygen sources. The total amount of oxygen is set to 1 5 QN m 3. Iron ore The total amount of sintered powder is set to 19 ◦ 0 kg. And start with Q. 5 5 As the objective of the alkalinity of the generated desilication slag, the amount of quicklime used as a slagging agent was determined, and the amount of quicklime was set to 300 kg. Desiliconization, the oxygen pipe blown from the upper part is used to continuously blow oxygen (oxygen flow: 9 0 ~ 9 2 ◦ N m 3 / hr) to the molten molten iron surface, and iron ore is continuously added from the upper part Sintering powder (adding speed of iron ore sintering powder: 180 ~ 200kg / min), and quicklime (adding speed of quicklime: 20 ~ 40kg / min) as a slagging agent is continuously blown into the molten iron through a spray pipe with nitrogen Desiliconization was completed in 10 minutes. The silicon concentration in the molten iron after desiliconization is Q. 〇 3 mass%, the temperature range of the molten iron after desiliconization is 138 Q ° C. Then, the generated desilication slag was scraped into a cast steel pan (hereinafter referred to as a cast steel pan) by a scraper. Then, the desilication slag was flowed into the facility 29 200300134 and placed in the construction house. The bottom and side iron boxes were constructed with thick steel plates with a thickness of 15 to 20 mm, and were allowed to solidify and cool to obtain 1 3 4 2 kg blocks. Slag (raw material for siliceous fertilizer). This massive slag is crushed to a particle size of 2 mm or less to make a silicic acid fertilizer. The composition analysis of this silicic fertilizer is shown in Table 1. As shown in Table 1, the obtained siliceous fertilizer is S i 〇 2 content: 5 5. 4% by mass, basicity: 0 · 5 5, solubility of silicic acid (proportion of total silicic acid content of soluble silicic acid: S-S i 0 2 / S i 0 2): 39% by mass. (Example 2) ′ Using the desilication treatment equipment shown in FIG. 4, desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing slag was produced to produce a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of molten iron is 150 tons, the composition of molten iron is, carbon: 4. 7 mass%, silicon: 0. 24% by mass, phosphorus: 0. 103 mass%, sulfur ... It is 042 mass% and the molten iron temperature is 1 3 9 5 ° C. The blast furnace slag (C a 0: 4 4 mass%, Si 0 2: 35 mass%, MgO: 6 mass%, A 1 2 03: 13 mass%) obtained in the previous step flows into the molten iron container The blast furnace slag amount is estimated to be 4 QQ kg from the measurement result of the thickness of the slag. With 0. 12% by mass was used as the target concentration of silicon concentration in the molten iron after the desiliconization process to determine the amount of iron ore sintering powder added to oxygen and solid oxygen sources. The total amount of oxygen was set to 7 4 N m3, and iron sintering was performed. The total amount of flour was set at 1 10 Q kg. And start with Q. 7 5 As the target of the alkalinity of the generated desilication slag, the amount of quicklime used as a slagging agent was determined. The amount of quicklime 30 200300134 was set to 220kg. Desiliconization is performed by freely blowing oxygen pipes from the upper part to continuously blow oxygen (oxygen flow rate: 8 50 ~ 9 50 N m 3 / hr) to the molten molten iron surface, and iron ore is continuously added from the upper part. Sintering powder (adding speed of iron ore sintering powder: 200 ~ 24Qkg / min), and quicklime (adding speed of quicklime: 4 G ~ 50 kg / min) as a slagging agent is continuously blown together with nitrogen through a spray pipe In the molten iron, the desilication treatment is completed in 5 minutes. The silicon concentration in the molten iron after desilication treatment is 0. 12% by mass. The temperature range of the molten iron after desiliconization was 1 3 3 7 X :. Then, the generated desilication slag was scraped into a cast steel pan with a scraper. Then, the desilication slag was poured into an iron box constructed on the bottom and sides of a thick steel plate with a thickness of 15 to 20 mm, which was installed in the construction house, and solidified and cooled to obtain a bulk slag (silicon) of 955 kg. Raw materials for acid fertilizers). This massive slag was crushed to a particle size of 2 mm or less to make a siliceous fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1, the obtained siliceous fertilizer is S i 0 2 content: 4 1. 3% by mass, alkalinity: 0.75, silicic acid solubility: 81% by mass. (Example 3) Using a desilication treatment facility shown in Fig. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing the slag to obtain a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of the molten iron is 15 Q tons, and the composition of the molten iron is: carbon: 4 · 4 mass%, silicon: 〇. 20% by mass, 0 · 100% by mass, sulfur: 0. 030 mass%, melting 31 200300134 melting iron temperature is 1 4 Q Q t :. The blast furnace slag obtained in the previous step (C a 〇: 4 2% by mass, S i 〇 2: 33% by mass, M g 〇 · 6% by mass, A 1 2 〇3 * 13% by mass) flows into the molten iron container. The amount of the blast furnace slag in the container is estimated to be 370 kg from the measurement result of the thickness of the slag. With 0. 12% by mass is used as the target concentration of silicon concentration in the molten iron after desiliconization to determine the amount of iron ore sintering powder added to oxygen and solid oxygen sources. The total amount of oxygen is set to 5 5 N m3, and iron sintering is performed. The total amount of flour was set at 700 kg. And start with 1. 0 3 As the target of the alkalinity of the generated desiliconized slag, the amount of quicklime used as a slagging agent was determined. The amount of quicklime was set to 225kg °. Oxygen flow: 6 Q 0 ~ 6 50 N m 3 / hr) Continuously blown to the molten molten iron surface, and continuously add iron ore sintered powder from the top (Iron ore sintered powder adding speed: 120 ~ 140kg / The quicklime (addition speed of quicklime: 40-50 kg / min) as a slagging agent is continuously blown into the molten iron through a spray pipe together with nitrogen, and the desilication treatment is completed in 5 minutes. The silicon concentration in the molten iron after desilication treatment is 0. 12% by mass. The temperature range of the molten iron after desiliconization was 1 37 ° C. Then, the generated desilication slag was scraped into a cast steel pan with a scraper. Then, the desiliconized slag was poured into an iron box constructed on the bottom and sides of thick steel plates with a thickness of 15 to 20 mm, which was installed in the construction house, and allowed to solidify and cool to obtain a bulk slag (silicon) of 7 6 8 kg. Raw materials for acid fertilizers). This massive slag was crushed to a particle size of 2 mm or less to make a siliceous fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1, 32 200300134, the resulting siliceous fertilizer is si 0 2 Content: 4 1. 0% by mass, alkalinity: 1.03, soluble rate of silicic acid: 76% by mass. (Example 4) Using a desilication treatment facility shown in Fig. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing the slag to obtain a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of the molten iron is 150 tons, the composition of the molten iron is, carbon: 4.5% by mass, silicon: 0. 24% by mass, phosphorus: 0.105% by mass, sulfur: Q. 041% by mass, and the molten iron temperature was 1 3 9 2 ° C. The blast furnace slag obtained in the previous step (C a 〇: 4 4 mass%, S i 〇 2: 36 mass%, Mg 0: 6 mass%, A 1 2 03: 13 mass%) flows into the molten iron container The slag amount of this blast furnace is estimated to be 4 5 Q kg from the measurement result of the thickness of the slag. With 0. 12% by mass was used as the target concentration of silicon concentration in the molten iron after the desiliconization process to determine the amount of iron ore sintering powder added to oxygen and solid oxygen sources. The total amount of oxygen was set to 7 4 N m3, and iron sintering The total amount of flour was set at 1 10 Q kg. And start with 1. 3 As a target for the alkalinity of the generated desilication slag 値 Determine the amount of quicklime to be added as a slagging agent, and set the amount of quicklime to 513kg. Desiliconization is performed by freely blowing oxygen pipes from the upper part to continuously blow oxygen (oxygen flow rate: 8 5 ◦ to 9 50 N m 3 / hr) to the molten molten iron surface, and iron ore is continuously added from the upper part. Sintering powder (adding speed of iron ore sintering powder: 200 ~ 240kg / min), and while adding 250 kg of quicklime as slagging agent from the top, add the remaining quicklime (fastlime 200200134 speed: 4 0 ~ 5 5 kg / min) is continuously blown into the molten iron through a spray pipe together with nitrogen, and the desilication treatment is completed in 5 minutes. The silicon concentration in the molten iron after desilication treatment is 0. 12% by mass. The temperature range of the molten iron after desiliconization was 1 3 37 ° C. Then, the generated desilication slag was scraped into a cast steel pan with a scraper. Then, the desilication slag was poured into an iron box constructed on the bottom and sides of thick steel plates with a thickness of 15 to 20 mm installed in the construction house, and solidified and cooled to obtain a block slag of 1280 kg ( Raw materials for siliceous fertilizers). This massive slag was crushed to a particle size of 2 mm or less to prepare a silicic acid fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1, the obtained siliceous fertilizer is S i 〇 2 content: 3 1. 0% by mass, basicity: 1. 2 7. Soluble rate of silicic acid: 78% by mass. (Example 5) Using a desilication treatment facility shown in Fig. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, and a desilication slag was thus prepared to obtain a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of the molten iron is 15 Q tons, and the composition of the molten iron is: carbon: 4 · 4 mass%, silicon: 0. 14 mass%, phosphorus: Q. 1Q5 mass%, sulfur: 0. 040% by mass and molten iron temperature was 14 0 ° C. The blast furnace slag obtained in the previous step (C a 0: 4 3% by mass, S i 〇 2: 34% by mass, MgO: 6% by mass, A12〇3: 12% by mass) flows into a molten iron container, and the blast furnace The amount of slag is estimated to be 380 kg from the measurement result of the thickness of the slag. Take Q. Q 7 mass% is used as the concentration of silicon in the molten iron after desilication treatment. 34 200300134 The standard is to determine the amount of iron ore sintered powder added to oxygen and solid oxygen sources. The total amount of oxygen is 4 7 N m3, iron The total amount of sintered ore powder is set at 60 4 kg. And start with 1. 6 As the target of the alkalinity of the generated desilication slag, determine the amount of quicklime used as a slagging agent, and set the amount of quicklime to be 400kg °. Flow: 5 50 ~ 5 7 0 N m 3 / h 3 :) Continuously blow to the molten molten iron surface and continuously add iron ore sintering powder from the top (iron ore sintering powder adding speed: 110 ~ 13Qkg The quicklime (addition speed of quicklime: 70 ~ 90kg / min) as a slagging agent is continuously blown into the molten iron through a spray pipe together with nitrogen, and the desilication treatment is completed in 5 minutes. The silicon concentration in the molten iron after desiliconization is Q. Q is 7 mass%, and the temperature range of the molten iron after desiliconization is 138 ° C. Then, the generated desilication slag was scraped into a cast steel pan with a scraper. Then, the desiliconized slag was poured into an iron box constructed on the bottom and sides of thick steel plates with a thickness of 15 to 20 mm installed in the construction house, and solidified and cooled to obtain 9 4 1 kg of block slag (silicon Raw materials for acid fertilizers). This massive slag was crushed to a particle size of 2 mm or less to make a siliceous fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1, the obtained silicic acid fertilizer is Si 02 content: 3 2 _ 3 mass%, alkalinity: 1. 6 2. Soluble rate of silicic acid: 83% by mass. (Example 6) Using the desilication treatment equipment shown in FIG. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing 35 200300134 slag to obtain a siliceous fertilizer. . The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of molten iron is 150 tons, the composition of molten iron is, carbon: 4. 2% by mass, silicon: 0. 26 mass%, phosphorus: Q. 10Q% by mass, sulfur: 0. . 038% by mass, and the molten iron temperature is 1 4 1 ◦ t :. The blast furnace slag obtained in the previous step (Ca 0: 4 2 mass%, Si 02: 34 mass%, MgO: 7 mass%, A 1 2 03: 15 mass%) flows into a molten iron container The blast furnace slag amount is estimated to be 4 Q 0 kg from the measurement result of the thickness of the slag. With 〇. Q 7% by mass is the target amount of silicon concentration in the molten iron after desilication treatment. The amount of iron ore sintered powder for oxygen and solid oxygen source is determined. The total amount of oxygen is set to 1 3 1 N m3, iron ore. The total amount of sintered powder was set at 1689kg. In addition, in order to increase the MgO content of the siliceous fertilizer to 7% by mass or more, a dolomite (dolomite) of 189 kg was added as a component adjusting agent, and the desiliconized slag was produced using ◦ · 5. The goal of alkalinity is to determine the amount of quicklime added as a slagging agent, and the amount of quicklime is set to 1 kg. Desiliconization is performed by continuously blowing oxygen (oxygen flow rate: 7 0 ~ 9 0 0 Nm3 / hr) to the molten molten iron surface with an oxygen pipe blown from the upper part, and continuously adding iron ore sintered powder from the upper part (Addition rate of iron ore sintered powder: 160 ~ 18 Q kg / min), and quicklime as slag-forming agent (addition rate of quicklime: 10kg / min) and roasted dolomite powder as component modifier (Addition rate of roasted dolomite powder: 18 ~ 20kg / min.) It is continuously blown into the molten iron through a spray pipe together with nitrogen, and the desilication treatment is completed in 10 minutes. The silicon concentration in the molten iron after the desiliconization treatment was 〇_〇7 36 200300134% by mass, and the temperature region of the molten iron after the desiliconization treatment was 138 ° C. In the 189 kg of roasted dolomite, Mg0 part was 79 kg and Ca0 part was 110 kg. Then, the generated desilication slag was scraped into a cast steel pan with a scraper, and then, The high-pressure air pulverization method was used to cool and solidify to obtain 1 2 6 kg of granular slag (raw material for siliceous fertilizer) with a particle diameter of 3 mm or less, which was directly used as the siliceous fertilizer. The composition analysis of this siliceous fertilizer is shown in Table 1 above. As shown in Table 1, the obtained siliceous fertilizer is Si02 content: 51. 1% by mass, alkalinity: 0. 50. Silicic acid solubility: 64% by mass. (Example 7) Using a desilication treatment facility shown in Fig. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing the slag to obtain a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of the molten iron is 150 tons, and the composition of the molten iron is: carbon: 4 · 2 mass%, sand: 0. 25% by mass, phosphorus: 0. 1Q0 mass%, sulfur: 0. 038% by mass and the molten iron temperature was 14 0 ° C. The blast furnace slag (CaO: 42 mass%, Si02: 34 mass%, MgO: 7 mass%, Al203: 15 mass%) obtained in the previous step flows into the molten iron container, and the amount of this blast furnace slag, From the measurement result of the thickness of the slag, it was estimated to be 400 kg. Take Q. 0 7 mass% is used as a target for the silicon concentration in the molten iron after the desiliconization process to determine the amount of iron ore sintering powder added to the oxygen and solid oxygen sources. The total amount of oxygen is set to 4 3 9 N m3, iron ore. The total amount of sintered powder is set to 37 200300134 1 5 8 2 kg. In addition, in order to increase the M g 0 content of the silicic fertilizer to 10% by mass or more, sintered dolomite 3 4 3 k g is added as a component adjusting agent, and the content is adjusted to 0. 6 6 As a target of the alkalinity of the generated desilication slag 値 Determine the amount of quicklime added as a slagging agent, and set the amount of quicklime to 100 kg. Desiliconization, the oxygen pipe blown from the upper part is used to continuously blow oxygen (oxygen flow rate: 1 47 0 ~ 1 4 8 QN m 3 / hr) to the molten molten iron surface, and iron ore is continuously added from the upper part Stone sintering powder (addition rate of iron ore sintering powder: 310 ~ 32Qkg / min), and quicklime (slagging lime addition rate: 2Qkg / min) as a slagging agent and sintered dolomite powder as a component regulator are passed together with nitrogen The spray pipe was continuously blown into the molten iron, and the desilication treatment was completed in 5 minutes. The silicon concentration in the molten iron after desilication treatment is 0. 〇 7 mass%, the molten iron temperature range after desiliconization is 1380 ° C. In the 343 kg of roasted dolomite, Mg0 was 143 kg and Ca0 was 200 kg. Then, the generated desilication slag was scraped into a steel casting pan with a scraper. Then, it was cooled and solidified by a high-pressure air pulverization method to obtain 1 446 k g of granular slag (raw material for silicic fertilizer) having a particle diameter of 3 mm or less, and used it directly as a silicic fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1 above, the obtained silicic acid-based fertilizer was Si02 content: 4 4 · 4 mass%, and alkalinity: 0.1. 6 6. Soluble rate of silicic acid: 99% by mass. (Example 8) Using a desilication treatment facility shown in FIG. 4, a desilication section of molten iron 38 200300134 was used to produce a desilication slag as a raw material for siliceous fertilizer, and silicic acid was obtained from the desilication slag. fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of the molten iron is 125 tons, and the composition of the molten iron is: carbon: 4 · 2 mass%, silicon: 0. 18% by mass, phosphorus: 0. 105 mass%, sulfur: 0. 038% by mass and the molten iron temperature was 139 ° C. The blast furnace slag (C a 0: 4 3 mass%, Si 02: 34 mass%, MgO: 7 mass%, Al203: 12 mass%) obtained in the previous step flows into the molten iron container, and the blast furnace The amount of slag is estimated from the measurement result of the thickness of the slag to be 4 QQ kg. Take Q. 〇7 mass% is the target amount of silicon concentration in the molten iron after desilication treatment to determine the amount of iron ore sintering powder added to oxygen and solid oxygen source. The total amount of oxygen is set to 66 N m3, and iron sintering The total amount of powder is set to 8 to 52 kg. In order to increase the Mg0 content of Shixi Acid Sour Moonbread to 10% by mass or more, 2 5 7 kg of roasted dolomite is added as a component modifier, and . 9 5 As the target of the alkalinity of the desiliconized slag to be generated 値 Determine the amount of quicklime to be added as a slagging agent, and set the amount of quicklime to 100 kg. Desiliconization is performed by freely blowing oxygen piping from the upper part to continuously blow oxygen (oxygen flow rate: 8 0 ~ 9 0 0 N m 3 / hr) to the molten molten iron surface, and iron ore is continuously added from the upper part. Sintering powder (adding speed of iron ore sintering powder: 160 ~ 18Qkg / min), and quicklime (adding speed of quicklime: 20 kg / min) as slagging agent and roasted dolomite powder (cultivation) Adding speed of dolomite powder: 4Q ~ 6Qkg / min) together with nitrogen is continuously blown into the molten iron through a spray pipe, and the desiliconization treatment is completed in 5 minutes 39 200300134. The silicon concentration in the molten iron after desiliconization was 〇. 〇7% by mass, the temperature range of the molten iron after desiliconization was 138 ° C. In the 257 kg of roasted dolomite, 107 g of Mg0 and 150 kg of Ca0 were obtained. Then, the generated desilication slag was scraped into a cast steel pan with a scraper. Then, it was cooled and solidified by a high-pressure air pulverization method to obtain 1 Q 5 3 k g of granular slag (raw material for silicic fertilizer) having a particle diameter of 3 mm or less, and directly used it as a silicic fertilizer. The composition analysis of this siliceous fertilizer is shown in Table 1 above. As shown in Table 1, the obtained siliceous fertilizer is Si02 content: 37. 3% by mass, alkalinity: 0. 95. Solubility of silicic acid: 99% by mass. (Example 9) Using the desilication treatment equipment shown in Fig. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing slag was produced to produce a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of molten iron is 125 tons, the composition of molten iron is, carbon: 4. 2% by mass, silicon: 0. 26 mass%, phosphorus: 0. 105 mass%, sulfur: 0. 038% by mass, and the temperature of the molten iron is 139 (TC. The blast furnace slag obtained in the previous step (C a 0: 4 4% by mass, S i 0 2: 35% by mass, MgO: 7% by mass, A 1 2 〇3 : 1 2 mass%) into the molten iron container, the amount of blast furnace slag was estimated to be 40 Q kg from the measurement result of the thickness of the slag. 0 7 mass% is the target amount of silicon concentration in the molten iron after desilication treatment to determine the amount of iron ore sintered powder added to the oxygen and solid oxygen source. 40 200300134 The total amount of oxygen is set to 1 Q 9 N m3, iron The total amount of sintered ore powder was set at 1407 kg. In addition, in order to increase the M g 0 content of the siliceous fertilizer to 10% by mass or more, the roasted dolomite 257 k g was added as a component adjusting agent, and the content was adjusted to 0. 6 6 As the target of the alkalinity of the generated desilication slag, the amount of quicklime used as a slagging agent was determined. The amount of quicklime was set to 100kg. Oxygen flow: 1 2 Q 0 ~ 1 4 0 QN m 3 / hr) is continuously blown to the molten molten iron surface, and iron ore sintering powder is continuously added from above (addition speed of iron ore sintering powder: 260 ~ 3QQkg / Min), and slag-forming lime (addition rate of quicklime: 2 ϋ kg / min) and sintered dolomite powder (addition rate of sintered dolomite powder ~ 60kg / min) as a component adjuster together with nitrogen through the spray The pipe was continuously blown into the molten iron, and the desilication treatment was completed in 5 minutes. The silicon concentration in the molten iron after desiliconization is Q. 〇 7 mass%, the temperature range of the molten iron after desiliconization was 139 Qt. Also, in 257 kg of roasted dolomite, 107 parts of Mg0 and 150 parts of Ca0 were obtained. Then, the generated desilication slag was scraped into a steel casting pan with a scraper. Then, the desilication slag was poured into an iron box constructed on the bottom and sides of a thick steel plate with a thickness of 15 to 20 mm, which was installed in the construction house, and solidified and cooled to obtain a block slag of 1 2 8 2 kg ( Raw materials for siliceous fertilizers). This massive slag was crushed to a particle size of 2 mm or less to prepare a silicic acid fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1, the obtained siliceous fertilizer is S i 0 2 content: 4 5. 5 quality 41 200300134 amount%, alkalinity: 0. 66. Silicic acid soluble rate: 70% by mass. (Example 10) Using a desilication treatment apparatus shown in Fig. 4, a desilication treatment of molten iron was performed to produce a desilication slag as a raw material for siliceous fertilizer, and a siliceous fertilizer was obtained from the desilication slag. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of molten iron is 150 tons, the composition of molten iron is, carbon: 4 · 7% by mass, silicon: 0. 24% by mass, phosphorus: Q. 103 mass%, sulfur: 0. It is 042 mass% and the molten iron temperature is 1 3 9 5 ° C. The blast furnace slag obtained in the previous step (Ca 0: 43% by mass, Si02: 35% by mass, MgO: 7% by mass, Al203: 12% by mass) flows into a molten iron container, and the blast furnace slag The amount is estimated from the measurement result of the thickness of the slag to be 4 ◦ 0 kg. With 0. 0.9% by mass is used as the target concentration of silicon in molten iron after desiliconization to determine the amount of iron ore sintered powder added to oxygen and solid oxygen sources. The total amount of oxygen is set to 1.04 N m3, iron ore. The total amount of sintered powder is set to 1 3 3 3 kg. The amount of quicklime to be added as a slagging agent was determined by using 0.51 as the target of the alkalinity of the desiliconized slag to be generated, and the amount of quicklime was set to 145 kg. Desanding treatment, the oxygen pipe blown from the upper part is used to continuously blow oxygen (oxygen flow: 1 2 0 ~ 1 3 0 0 N m 3 / h 3Γ) to the molten molten iron surface, and continuously added from the upper part Iron ore sintered powder (addition rate of iron ore sintered powder: 25 300kg / min), and quicklime (addition rate of quicklime: 25 ~ 35kg / min) as a slagging agent is continuously blown together with nitrogen through a spray pipe Into the molten iron, the desilication process is completed in 5 minutes. The silicon concentration in the molten iron after desilication treatment is 0. 〇 9 mass%, the temperature range of the molten iron after desiliconization was 139 Q ° C. Then, the generated desilication slag was scraped into a cast steel pan with a scraper, and then cooled and solidified by a high-pressure air pulverization method to obtain a granular slag having a particle size of 3 mm or less (1 kg) Silicate fertilizer raw materials), directly use it as silicic fertilizer. The composition analysis of this siliceous fertilizer is shown in Table 1 above. As shown in Table 1, the obtained siliceous fertilizer is Si02 content: 48. 8 mass%, testability: 0. 51. Shi Xi Acid soluble rate: 99% by mass. (Example 11) A desilication treatment apparatus shown in Fig. 4 was used to perform desilication treatment of molten iron to produce a desilication slag as a raw material for siliceous fertilizer, thereby desiliconizing slag to obtain a siliceous fertilizer. The molten iron obtained from the blast furnace is transferred to a desilication treatment facility. The weight of the molten iron is 150 tons, and the composition of the molten iron is: carbon: 4 · 4 mass%, silicon: 0. 16% by mass, phosphorus: 0. 100% by mass, sulfur: 0. 030% by mass and the molten iron temperature was 14 00 t :. The blast furnace slag obtained in the previous step (C a 0: 4 3% by mass, Si02: 34% by mass, MgO: 7% by mass, A 1 2 0 3 · 12% by mass) flows into a molten iron container, and The amount of blast furnace slag is estimated to be 400 kg from the measurement result of the thickness of the slag. Take Q. Q 7 mass% is used as the target concentration of silicon in molten iron after desiliconization to determine the amount of iron ore sintered powder added to oxygen and solid oxygen sources. The total amount of oxygen is set to 62Nm3 and the total amount of iron sintered powder. It is set at 800 kg. Again, with 0. 9 9 As the alkalinity of the generated desilication slag 43 200300134 The amount of quicklime used as a slagging agent is determined according to the standard, and the amount of quicklime is 25Qkg. Desanding treatment, the oxygen pipe blown from the upper part is used to continuously blow oxygen (oxygen flow rate: 7 ◦◦ ~ 8 ◦ 0 N m 3 / hr) to the molten molten iron surface, and iron ore is continuously added from the upper part Sintering powder (adding speed of iron ore sintering powder: 150 ~ 17Qkg / minute), and quicklime (adding speed of quicklime: 4Q ~ 60kg / minute) as a slagging agent is continuously blown into the molten iron through a spray pipe together with nitrogen. , Complete the desilication process in 5 minutes. The silicon concentration in the molten iron after desiliconization is Q. Q was 7 mass%, and the temperature range of the molten iron after desiliconization was 1 3 8 CTC. Then, the generated desilication slag was scraped into a cast steel pan with a scraper, and then cooled and solidified by a high-pressure air pulverization method to obtain 910 kg of granular slag having a particle diameter of 3 mm or less. (Raw material for silicic fertilizer), use it directly as silicic fertilizer. Table 1 shows the composition analysis of this siliceous fertilizer. As shown in Table 1, the obtained silicic acid fertilizer was Si02 content: 40.6% by mass, alkalinity: 0.99, and the solubility of silicic acid: 99% by mass. 44 200300134 Basicity ΓΟ • X LD LT) if) m m 〇r- CN] rH CM \ o 〇LO LD σ \ KD 1 ~ 1 L0 Ch 〇ο t ~ 1 rH 〇〇〇〇〇ο CN • Η CO / Si〇2 σ \ η rH 00 V £) O 00 Γ0 00 V £) Ch σ \ σ \ σ \ 〇l > σ \ σ \ σ \ σ \ 1 ω ο ο 〇oo 〇〇ο ο 〇Chemical composition (mass%) of silicic fertilizer CM XC? • Η ω 1 U) V £) LO rH CN 00 I > σ > 00 m CN rH CN ΓΟ ΓΟ \ ~ 1 m inch CN U) CM CN mm Inch VD m rH ro CO inch 〇Α12〇3 KD m cn o \ CN rH 00 ο inch CO \ D ΓΟ inch LO \ > inch ΓΟ inch mm inch (ϋ CN CM ro 00 oo LO LD LO Εη ΓΟ V £) ro inch ro inch inch inch Μη〇00 00 00 Γ0 CO If) inch · LO if) CN LO CN Γ0 〇g inch inch · inch · inch MgO ι ~ 1 Ch 1 ~ 1 id CM LO rH i ~ i CN Γ0 r- Γ Ο rH ΓΟ \ —1 rH ϋΊ σ \ KD 〇 \ —1 r- CN Ca〇η 〇CM Γ0 Γ0 ι > m inch 00 σ »OQ ο Γ〇tH Γ0 03 inch cy \ Γ0 CN LO LO CN σ \ CN LD Γ0 σ \ CN inch CN] 〇c? • Η ω inch moo Γ0 t " · 1 inch Γ0 LD CO \ D LD U1 tH 1 ~ 1 rH rn CM cn rH LO Γ ΟΟ if) 00 〇 Cooling condition of slag * 1 Xu Leng Xu Leng Xu Leng Xu Leng 7 Example 8 Example 9 Example 10 Example 11 fN〇TS / 〇fduΓη-Κτκιφ / ροτ: Variable # • 伥 φ / ροτ: Assets, Yueteng 菝 酲 筠 侧 11 side 1 | £ 0000 0 0 2 So far Sword parrot ^ 荽 回 1 ^ 200300134 (Example 1 2) The dissolution of the siliceous fertilizer of Examples 3, 4, 6, 8 and the siliceous fertilizer obtained by crushing slag from high-pressure water in a blast furnace in the neutral region Sex to investigate. 1 g of each siliceous fertilizer was extracted by shaking in a 0.2 M phosphate solution (p Η 7) 1 5 ◦ m 1 prepared from monoammonium phosphate and diammonium phosphate. This extraction was performed at 3 ° C for 1 hour, and the dissolution rate of silicic acid in the neutral domain was determined from the silicic acid concentration in the filtrate. The results are shown in Table 2. As shown in Table 2, in the neutral domain (P Η 7), the dissolution rate, relative to the siliceous fertilizer produced by blast furnace high-pressure water crushing slag is 0. 1%, in the siliceous fertilizer of the present invention, Q is obtained. 9 ~ 4 · 3% high number 値. Among them, the slag obtained by cooling (rapid cooling) at a cooling rate of 1 ◦ ° C / min or more in a temperature range of 1 3 0 ◦ to 1 0 ◦ 0 ° C can obtain a high temperature. Dissolution rate.
46 200300134 CN3撇 鹼性度 *2 ro 〇 r—1 r- 03 γΗ ο LD 〇 LT) CPi 〇 LT) CM \—1 中性域溶 解率（％) (%) Ch 〇 寸 rH γΗ CN Γ0 寸1 rH Ο 矽酸質肥料的化學組成（質量％) 中性溶解性 Si02 Γ- ΓΟ o Γ0 〇 Γ Ο rH 〇 VD »—1 CO 〇 ο Al2〇3 Γ0 LO σ\ Ι> τΗ 〇 VO \—1 Q) Η ΓΟ 00 00 寸 LO 寸 CM 〇 MnO CO OJ ΓΟ η 寸 if) 寸 03 〇 Mg〇 LD CNI ΙΓι γΗ Γ0 1> P0 rH rH CO VD Ca〇 CN CN 寸 η σ\ ΓΟ 1> LD CN 寸 LD m 寸 \—! 寸 CN 〇 •H U) 〇 rH ο γΗ ΓΟ t~1 rH LD m ο m i—1 m m 爐渣之 冷卻條件*1 徐冷 徐冷 急冷 急冷 急冷 / 實施例3 實施例4 實施例6 實施例8 高爐高壓水 粉碎爐渣 OJ〇TS/〇fduz +^κιφ/ροτ :变# •伥φ/οοτ :资錐 侧_昂变^酲鏐11鹋||^000〇1~002^鄕缨^婪回1^ 200300134 產業上之可利用忡 本發明之矽酸質肥料用原料，可溶性矽酸之含有量多且鹼 性份少’並可直接利用熔融鐵預備處理步驟中所回收之爐 渣’故可用以廉價地製得矽酸質肥料。因此，於製造廉價且 具有優異的肥料特性之矽酸質肥料上甚爲有用。又，本發明 之矽酸質肥料用原料之製造方法，由於可安定地製造上述爐 渣，故作爲廉價且具有優異的肥料特性之矽酸質肥料之製造 方法甚爲有用。 圖式之簡單說明 圖1爲顯示脫矽爐渣的鹼性度與矽酸可溶率的關係之曲線 圖。 圖2爲顯示脫矽爐渣的鹼性度與可溶性矽酸含有量的關係 之曲線圖。 圖3爲顯示將圖2的鹼性度（Ca0/Si02):〇.3~〇.7的範圍 擴大之曲線圖。 圖4爲顯示依據本發明之矽酸質肥料用原料之製造方法的 一實施形態之說明圖。 圖5爲顯示本發明之矽酸質肥料用原料的造粒步驟的一例 之說明圖。 圖6爲顯示本發明之矽酸質肥料用原料的造粒步驟的其他 例之說明圖。 元件符號說明 1 溶融鐵裝盛容器 2 熔融鐵 48 200300134 3 台車 4 脫矽爐渣 5 固體氧源 6 氧氣配管 7 噴射配管 8 造渣劑46 200300134 CN3 Hydrophobicity * 2 ro 〇r—1 r- 03 γΗ ο LD 〇LT) CPi 〇LT) CM \ -1 Neutral domain dissolution rate (%) (%) Ch 〇 inch rH γΗ CN Γ0 inch 1 rH Ο Chemical composition (mass%) of silicic fertilizer Neutral solubility Si02 Γ- ΓΟ o Γ0 〇Γ Ο rH 〇VD »—1 CO 〇ο Al2〇3 Γ0 LO σ \ Ι > τΗ 〇VO \ — 1 Q) Η ΓΟ 00 00 inch LO inch CM 〇MnO CO OJ ΓΟ η inch if) inch 03 〇Mg〇LD CNI ΙΓι γΗ Γ0 1 > P0 rH rH CO VD Ca〇CN CN inch η σ \ ΓΟ 1 > LD CN Inch LD m Inch \ —! Inch CN 〇 • HU) 〇rH ο γΗ ΓΟ t ~ 1 rH LD m ο mi—1 mm Slag cooling conditions * 1 Xu Leng Xu Leng Quenching Quenching / Example 3 Example 4 Implementation Example 6 Example 8 Blast furnace high-pressure water crushing slag OJ〇TS / 〇fduz + ^ κιφ / ροτ: 变 # • 伥 φ / οοτ: information cone side_Ang change ^ 酲 镠 11 鹋 || ^ 000〇1 ~ 002 ^鄕 缨 ^ 婪 回 1 ^ 200300134 Industrially available 原料 The raw material for silicic acid fertilizer of the present invention has a large content of soluble silicic acid and a low alkaline content, and can be directly processed using molten iron. The recovered slag 'it can be used to inexpensively obtain silicate fertilizers. Therefore, it is particularly useful for manufacturing a siliceous fertilizer which is inexpensive and has excellent fertilizer characteristics. In addition, the method for producing a raw material for siliceous fertilizer according to the present invention can stably produce the slag described above, so it is useful as a method for producing a siliceous fertilizer which is inexpensive and has excellent fertilizer characteristics. Brief Description of the Drawings Figure 1 is a graph showing the relationship between the alkalinity of desilication slag and the solubility of silicic acid. Figure 2 is a graph showing the relationship between the alkalinity of desilication slag and the content of soluble silicic acid. FIG. 3 is a graph showing an enlargement of the range of alkalinity (Ca0 / Si02): 0.3 to 0.7 of FIG. 2. Fig. 4 is an explanatory view showing an embodiment of a method for producing a raw material for siliceous fertilizer according to the present invention. Fig. 5 is an explanatory diagram showing an example of a granulation step of a raw material for a siliceous fertilizer according to the present invention. Fig. 6 is an explanatory view showing another example of a granulation step of the raw material for a siliceous fertilizer according to the present invention. Component symbol description 1 molten iron container 2 molten iron 48 200300134 3 trolley 4 desilication slag 5 solid oxygen source 6 oxygen piping 7 jet piping 8 slagging agent
9 成分調整劑 10,11,12 貯藏槽 1 3 , 1 4 , 1 5 貯糟 1 6 酉己料器(dispenser) 17 ,18, 19, 26, 36 漏斗 20,21,22 原料釋出裝置 23 移送裝置 2 4 斜管 2 5 粉碎物9 Ingredient modifier 10, 11, 12 Storage tank 1 3, 1 4, 1 5 Storage tank 1 6 Dispenser 17, 18, 19, 26, 36 Funnel 20, 21, 22 Raw material release device 23 Transfer device 2 4 Inclined tube 2 5 Ground material
27 輸送帶 28 桶式旋轉造粒機 2 9 黏合劑 3 〇 容器 3 1 乾燥機 3 2 升降機 33 篩別裝置 34 冷卻器 3 7 黏合劑 49 200300134 3 8 容器 3 9 混合機 4 0 皿形造粒機 4 1 輸送帶 A 原料供給設備27 Conveyor belt 28 Barrel rotary granulator 2 9 Binder 3 〇 Container 3 1 Dryer 3 2 Elevator 33 Screening device 34 Cooler 3 7 Binder 49 200300134 3 8 Container 3 9 Mixer 4 0 Dish pellet Machine 4 1 Conveyor A Raw material supply equipment
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