(1) 1353886 九、發明說明 【發明所屬之技術領域】 本發明是關於一種由粉體狀的各種礦物、或在各種產 業之粉體狀中間製品或廢棄物中，利用靜電或磁力，將目 的物質予以分離回收或將不要成分予以分離去除之際，提 供有經濟性的分離回收率或除去率、或可充分實用等級的 目的成分濃縮率之方法。 【先前技術】 在於由成分或物質不同的粒子混合存在之粉體中，將 目的物質予以分離回收、或將不要物質予以除去、或進行 目的物質的濃縮之方法，以往以來具有利用磁力的特性（ 磁性）、電性（介電率、導電率、帶電性）等的物理或物理 化學特性之差異，予以進行比重分離、磁性分離、及靜電 分離等的各種方法。在這些的方法之選擇上，是根據欲分 ® 離回收或濃縮之目的物質與殘餘的不要物質之差異爲何， 來決定的。但，這些的方法，在以往多數的情況，目的物 質的分離回收效率或濃縮率低，在產業使用上具有界限》 另外，資源特別是有用礦物的枯竭問題或有效利用、 及來自於各種產業的副產物或廢棄物的再回收利用之殘存 有用物質的分離回收或濃縮，在近年極爲受到重視，被強 力期望確立，目的物質可充分地具有實用性之分離回收率 、濃縮率、及低的設備費以及運轉費之技術。 在這些之中，利用靜電分離之方法或磁性分離之方法 -4- (2) 1353886 ，設備的建設費與運轉費均低，且具有可使用於廣泛領域 之可能性，近年視爲有望之方法。但，在以往的技術，目 的物質的分離回收效率或濃縮率低，並未達到可實用之等 級。 例如，在利用靜電分離之方法，如專利文獻1及專利 文獻2所揭示之技術爲眾所皆知。 [專利文獻1]日本特開20〇4-243 154號公報 • [專利文獻2]國際公開2〇〇2/7662〇號說明書 【發明內容】 [發明所欲解決之課題] 本發明是在於，發現對目的物質的分離回收效率或濃 縮度等的分離效率造成壞影響而阻礙了實用化之大原因在 於以往以外所習知的常識以外，而考案出爲了使分離效率 大幅地提昇至可充分實用化，而打破該阻礙原因之具體的 _方案。 在靜電分離，對於粒子的表面導電性或接觸阻抗造成 影響的粒子表面之含水量或對其造成影響之空氣中的溼度 ，爲對目的物質的分離回收效率或濃縮度等的分離效率造 成影響之重要因子，需要在乾燥度高的狀態下進行的情事 爲眾所皆知。 但，實際上在乾燥狀態下進行實驗時，則一部分的粒 子會發揮較高之分離效率，但多數的粒子，其分離效率極 爲不充分，完全未能達到實用等級。 -5- (3) 1353886 [用以解決課題之手段] 因此，本發明者爲了找出除了水分或溼度以外，會造 成大幅影響之因素，而除了欲供給的氣體種類與溫度、氣 體流速、施加電壓、電場強度、磁力強度、磁力斜率、粉 體層的流動化狀態等之操作條件以外，針對粒度分佈、粒 子表面的化學成分或吸著物質等的影響，進行調查檢討。 • 其結果’發現在靜電分離、或磁性分離之任一情況，當在 特性不同的粒子之混合粉體中含有多數的球當量直徑 10 μ +m以下的微粉時，則分離效率會大幅度地降低。 這是由於當這樣的微粉多時則粒子的凝聚變得顯著， 在欲分離的性狀不同之粒子，即目的物質粒子與非目的物 質粒子混合之狀態下凝聚，造成分離效率變差之故。在發 明者所做的進一步檢討中，亦發現即使在直徑ΙΟμιη以下 的微粉爲目的物質粒子與非目的物質粒子的其中任一方粒 • 子’該微粉也因爲其呈微粉而附著凝聚力強，會附著於另 一方的性狀之大的粒子表面，無法進行有效率的靜電分離 ，使得分離效率大幅度地降低。 做爲這些之對策’發明者考案出以下之方法。即，將 欲供給至靜電分離裝置或磁性分離裝置之粒子的混合粉體 ，事先予以分散（將凝聚體分開，而作成目的物質粒子或 非目的物質粒子之單一形狀粒子），然後在其再凝聚之前 ，迅速地供給至分離裝置之方法。做爲具體之分散方法， 可採用下述1)〜4)之任一方法。 (4) (4)1353886 Ό將混合體供給至在計示壓力時之供給壓力爲1〇〇kPa 〜600kPa之氣體流中； 2) 將混合粉體供給至具有雷諾數爲12〇〇〇以上的氣體 流之管中； 3) 將混合粉體供給至安裝於旋轉軸的突起狀物以5m/s 以上的周速度旋轉之容器中； 4) 將混合粉體供給至塡充有球當量直徑爲lmin〜 60mm的分散媒體之容器’使分散媒體在容器中進行運動 [發明的效果] 根據本發明的話’形成能夠自目的物質粒子與非目的 物質粒子的混合粉體之中’以高純度（高濃縮度）且高回收 率來僅將目的物質粒子回收，其結果，能夠將回收的目的 物質粒子有效地加以活用，在資源的有效利用、及副產物 、廢棄物的有效利用之觀點上，在今後的地球規模之資源 的有效利用及環境對策的面，具有很大的貢獻。 【實施方式】 以下，說明本發明的具體方法。 第1方法： 事先分散的第1方法是在使欲分離的性狀之目的物質 粒子與非目的物質粒子混合存在之混合粉體（原料粉體）帶 電荷或磁性予以分離之前，在計示壓力爲lOOkPa〜600kPa (5) 1353886 、理想爲200kPa〜400kPa之壓力供給壓力來將空氣等的 氣體2供給至如圖1及圖2所例示的噴射器，將原料粉體3供 給至噴射器中的負壓部分或噴射器後方的噴射流中，使目 的物質粒子與非目的物質粒子，即具有不同電氣特性（介 電率或導電率）或磁力特性之粒子凝聚體充分地分散。再 者，在圖1及圖2中，1爲壓力計。 再者，氣體2的供給壓力，當過低時則分散會變得不 • 充分，而當過高時則會同時地引起部分粉碎，造成微粉增 力口，在分離效率上並不希望這些情事產生。又，在氣體2 的供給壓力過剩之情況，變得需要大型的壓縮機，在設備 及能量消耗的面上，並不具有經濟性。 第2方法： 事先分散的第2方法是在使欲分離的性狀之目的物質 粒子與非目的物質粒子混合存在之混合粉體（原料粉體）帶 ® 電荷或磁性予以分離之前，將原料粉體供給至具有雷諾數 爲12000以上、更期望爲40000以上的氣體流之管中，使目 的物質粒子與非目的物質粒子即具有不同電氣特性（介電 率或導電率）或磁力特性之粒子凝聚體充分地分散。 在此，雷諾數Re爲以下述的式子所定義的無因次數 ，顯示管內的亂流狀態，爲値變得越大則亂流越強之意。 D ' U、p、//的單位爲任意，所計算之Re形成無因次即 可 〇(1) 1353886 IX. Description of the Invention [Technical Field] The present invention relates to the use of static electricity or magnetic force from various minerals in powder form or in powdered intermediate products or wastes of various industries. When the substance is separated and recovered or the unnecessary component is separated and removed, an economical separation recovery rate or removal rate or a method of sufficiently enriching the target component concentration ratio can be provided. [Prior Art] A method in which a target substance is mixed and recovered, or an unnecessary substance is removed or a target substance is concentrated, in a powder in which particles having different components or substances are mixed, and a magnetic property is conventionally used ( Various methods such as specific gravity separation, magnetic separation, and electrostatic separation are performed for differences in physical or physicochemical properties such as magnetic properties and electrical properties (dielectricity, electrical conductivity, and chargeability). The choice of these methods is determined by the difference between the substance to be recycled or concentrated and the residual material. However, in many cases, the separation and recovery efficiency or concentration ratio of the target substance is low, and there is a limit in industrial use. In addition, resources, especially useful minerals are depleted or effectively utilized, and come from various industries. Separation, recovery, or concentration of the remaining useful substances in the recycling of by-products or wastes has been highly valued in recent years and is strongly expected to be established. The target substances can be sufficiently useful for separation and recovery, concentration, and low equipment. Fee and operating fee technology. Among these, the method of electrostatic separation or the method of magnetic separation -4- (2) 1353886, the construction cost and operating cost of the equipment are both low, and there is a possibility that it can be used in a wide range of fields, and it has been regarded as a promising method in recent years. . However, in the prior art, the separation efficiency of the target substance or the concentration ratio is low, and it has not reached a practical level. For example, in the method of utilizing electrostatic separation, the techniques disclosed in Patent Document 1 and Patent Document 2 are well known. [Patent Document 1] Japanese Laid-Open Patent Publication No. H20-243-154 (Patent Document 2) International Publication No. 2/7662 No. It has been found that the separation efficiency of the separation and recovery efficiency of the target substance or the degree of enrichment has a bad influence, and the reason for the practical use is that it is outside the conventional knowledge that has been conventionally known, and that the separation efficiency is sufficiently improved to be sufficiently practical. And break the specific _ plan for the cause of the block. In the electrostatic separation, the moisture content of the surface of the particle which affects the surface conductivity or contact resistance of the particle or the humidity in the air affects the separation efficiency of the separation or recovery efficiency or concentration of the target substance. Important factors that need to be carried out under conditions of high dryness are well known. However, in actuality, when a test is carried out in a dry state, a part of the particles exert a high separation efficiency, but the separation efficiency of most of the particles is extremely insufficient, and the practical grade is not fully achieved. -5- (3) 1353886 [Means for Solving the Problem] Therefore, the present inventors have found a factor that greatly affects in addition to moisture or humidity, in addition to the type of gas to be supplied, temperature, gas flow rate, and application. In addition to the operating conditions such as voltage, electric field strength, magnetic strength, magnetic gradient, and fluidization state of the powder layer, investigations are conducted on the effects of particle size distribution, chemical composition on the surface of the particles, and sorbent substances. • As a result, it was found that in the case of electrostatic separation or magnetic separation, when a mixed powder of particles having different characteristics contains a plurality of fine powder having a spherical equivalent diameter of 10 μ + m or less, the separation efficiency is greatly improved. reduce. This is because when such fine powders are large, the aggregation of the particles becomes remarkable, and the particles having different properties to be separated, that is, the particles of the target substance and the particles of the non-target particles are aggregated, and the separation efficiency is deteriorated. In the further review by the inventors, it was found that even if the fine powder having a diameter of ΙΟμηη or less is one of the target particles and the non-target particles, the fine powder adheres to the cohesive force because of its fine powder and adheres. On the other surface of the particle having a large trait, efficient electrostatic separation cannot be performed, and the separation efficiency is drastically lowered. As a countermeasure against these, the inventor has examined the following methods. In other words, the mixed powder of the particles to be supplied to the electrostatic separation device or the magnetic separation device is dispersed in advance (the aggregates are separated to form a single-shaped particle of the target substance particle or the non-target substance particle), and then re-agglomerated. Previously, the method of supplying to the separation device quickly. As a specific dispersion method, any of the following methods 1) to 4) can be employed. (4) (4) 1353886 供给 Supply the mixture to a gas flow at a pressure of 1 kPa to 600 kPa at the time of the gauge pressure; 2) Supply the mixed powder to a Reynolds number of 12 〇〇〇 or more 3) The mixed powder is supplied to the container in which the protrusion attached to the rotating shaft is rotated at a peripheral speed of 5 m/s or more; 4) The mixed powder is supplied to the filled ball equivalent diameter The container of the dispersion medium of 1 min to 60 mm 'moves the dispersion medium in the container. [Effects of the Invention] According to the present invention, 'the formation of a powder which can be obtained from the mixed powder of the target substance particles and the non-target substance particles is high purity ( Highly concentrated) and high recovery rate, only the target substance particles are recovered, and as a result, the recovered target substance particles can be effectively utilized, and the resources can be effectively utilized, and by-products and waste can be effectively utilized. It will contribute greatly to the effective use of resources on the scale of the earth and environmental measures in the future. [Embodiment] Hereinafter, a specific method of the present invention will be described. First method: The first method of dispersing in advance is to measure the pressure before the mixed powder (raw material powder) in which the target substance particles to be separated and the non-objective particles are mixed are charged or magnetically separated. lOOkPa to 600 kPa (5) 1353886, preferably a pressure supply pressure of 200 kPa to 400 kPa, to supply a gas 2 such as air to the ejector as illustrated in FIGS. 1 and 2, and supply the raw material powder 3 to the negative in the ejector In the jet portion or the jet flow behind the ejector, the target substance particles and the non-target substance particles, that is, the particle agglomerates having different electrical characteristics (dielectric constant or electrical conductivity) or magnetic properties are sufficiently dispersed. Further, in Fig. 1 and Fig. 2, 1 is a pressure gauge. Furthermore, when the supply pressure of the gas 2 is too low, the dispersion becomes insufficient, and when it is too high, partial pulverization is caused at the same time, causing the fine powder to increase the force, and these conditions are not desired in the separation efficiency. produce. Further, when the supply pressure of the gas 2 is excessive, a large compressor is required, and it is not economical on the surface of equipment and energy consumption. Second method: The second method of dispersing in advance is to separate the raw material powder by separating the charge (magnetic material) of the target material particles and the non-target material particles to be separated When it is supplied to a tube having a gas flow having a Reynolds number of 12,000 or more and more desirably 40,000 or more, the target substance particles and the non-target substance particles are particle aggregates having different electrical characteristics (dielectric rate or conductivity) or magnetic properties. Fully dispersed. Here, the Reynolds number Re is a number of unnecessary times defined by the following formula, and the turbulent flow state in the tube is displayed, and the turbulent flow is stronger as the enthalpy becomes larger. The unit of D ' U, p, / / is arbitrary, and the calculated Re forms no dimension.
Re = D.U. p I β -8- (6) 1353886 D :管的內徑 U:管內的氣體速度 P :氣體的密度 #:氣體的黏性係數 所供給的原料粉體3是在如圖3所示意地顯示之管中， 如雷諾數所示，藉由強力的亂流（在雷諾數爲30000以上則 形成亂流），在粒子彼此、或粒子與管壁之間產生強力的 ® 衝突，使得凝聚的粒子被分散。此時，管亦可爲複數個且 並列。又，管的斷面形狀不被特別限定，亦可爲圓形，亦 可爲矩形。且，將管的長度設計成：通過管內的氣體4之 滯留時間形成0.005秒以上即可。在圖3中，5爲流量計。 第3方法： 事先分散的第3方法是在使欲分離的性狀之目的物質 粒子與非目的物質粒子混合存在之混合粉體（原料粉體）帶 ® 電荷或磁性予以分離之前，將原料粉體連續地或分批地供 給至安裝於旋轉軸的突起狀物以5m/s以上、期望爲15〜 5 〇m/s以上的周速度旋轉之容器中，使目的物質粒子與非 目的物質粒子即具有不同電氣特性（介電率或導電率）或磁 力特性之粒子凝聚體充分地分散。 圖4式顯示藉由馬達9將以設置於旋轉板7的複數個葉 片6做爲突起狀物8來在容器內旋轉的構造之分散裝置。同 樣地’在圖5顯示馬達9將以設置於旋轉板7的複數個銷10 做爲突起狀物8來在容器內旋轉的構造之分散機。這些的 (7) 1353886 構造或形狀，可有很多的變化，但若爲藉由使所供給的原 料粉體3旋轉之葉片6或銷10以賦予衝擊力或剪斷力之構造 的話，則其形狀不被限定。例如，能夠將銷磨機或葉片磨 機等之高速旋轉衝擊粉碎機應用於本發明之分散。當葉片 或銷的速度過慢時則分散會變得不充分，而當過快時則會 同時地引起粉碎，造成微粉增加，在分離效率上均不希望 這些情事產生。又，在旋轉速度過剩之情況，在設備成本 • 及能量消耗的面上，並不經濟。 且，在圖4或圖5的構造之分散裝置，亦可在同軸上設 置至少2個旋轉軸，使安裝於各自的旋轉軸之突起狀物旋 轉，使得在各自的突起狀物相互最接近之部分的該突起狀 物彼此的旋轉之相對周速度，在該相對周速度形成最大之 位置時做成5m/s以上。 圖6是顯示設置有2個旋轉軸之銷磨機的例子。在圖6 中，軸11a與軸lib設置於同軸上，在軸11a安裝有銷l〇a ® 及l〇c，在軸lib安裝有銷10b。在「各自的突起狀物相互 最接近之部分」，「其（相對周速度）形成最大之位置」， 在圖6是指銷10a與銷10b之間，因此，使軸l〇a及l〇b旋 轉，使得銷l〇a與銷10b之相對周速度形成5m/s以上。在 此情況時，銷l〇b與銷10c之相對周速度形成較銷i〇a與 銷l〇b之相對周速度更小，在相對周速度形成最大的位置 ，即突起狀物最接近之部分，由旋轉軸起算之半徑位置爲 最外側，如在圖6中爲銷10a與銷10b之相對周速度爲5m/s 以上即可。軸11a與軸lib亦可相互地朝反方向旋轉，亦 -10- 1353886 ⑹ 可朝相同方向旋轉。又，分散裝置的形式不限於如圖6所 示的銷方式。安裝有個別地旋轉之至少2個旋轉軸、與安 裝於各自的旋轉軸之突起狀物即可，各自的突起狀物以相 對周速度5m/s以上旋轉即可。藉由將原料粉體投入這樣 的容器中’可獲得與前述相同之分散效果。 第4方法： • 事先分散的第4方法是在使欲分離的性狀之目的物質 粒子與非目的物質粒子混合存在之混合粉體（原料粉體）帶 電何或磁性予以分離之前’如圖7所示，在塡充有以球當 量直徑（設想體積相同的球時之該球的直徑）爲1mm〜60mm 期望爲5mm〜4〇mm的球做爲分散媒體之容器，藉由使容 器旋轉’或在容器內部使旋轉軸與和旋轉軸接合的攪拌翼 或攪拌棒旋轉’來使做爲分散媒體之球運動，對該容器連 續或分批地供給原料粉體，使目的物質粒子與非目的物質 ® 粒子即具有不同電氣特性（介電率或導電率）或磁力特性之 粒子凝聚體充分地分散。 根據攪拌翼或攪拌棒的不同，具有圖7(a)所示的螺旋 型、圖7(b)所不的圓盤型、圖7(c)所示的攪拌槽型、圖 7(d)所示的環型等β 此容器的形狀與旋轉軸的方向無特別限制，旋轉軸爲 水平或垂直均可。例如，能夠將球磨機或媒體攪拌磨機易 用於本發明的分散。球的直徑，當過小時，則原料粉體之 通過阻抗變大，變得不易連續供給，又，在分批式，不易 -11 - (9) 1353886 進行分散後之粉體排出（與球之分離）。另外，當球過大時 ’則由於球間之間隙變大，故原料粉體未被分散而直接通 過之比率變高，並且由於球的衝擊力變大，故也會產生使 微粉凝聚之作用，因此並不理想。又，當球變得更大時’ 則施加於軸之轉矩過剩，亦會產生軸不旋轉之情事。在此 ，塡充於容器的分散媒體，若球當量直徑與該球相同者的 話，其形狀未被特別限定。又，其材質可根據原料粉體之 • 凝聚強度，從木材、軟木塞、橡膠、塑膠、陶瓷、金屬等 來加以選擇。再者，原料粉體在該容器內之平均滯留時間 ，由於需要作成隨著粉碎動作進行而不會產生過剩的微粉 ，故期望爲10分鐘以內。 [實施例j 實施例1 : 由全國的發電所所產生的煤灰（飛灰），一年大約1000 ® 萬噸，從今後資源的有效活用之觀點來看，灰分多之低品 味碳的使用會增加，可預想到飛灰的產生量會更增加。在 這之中，大約60%爲在水泥製造，做爲其原料的一部分來 使用，其使用可能量，在做爲水泥之化學成分上，已到達 界限。殘餘的大部分被掩埋加以處分。此掩埋處分在環境 對策上非爲期望之動作。 在水泥領域爲了進一步增加飛灰的使用量，並非做爲 至今爲止之原料，而是在所產出之水泥，在JIS(日本工業 規格）所規定之範圍內加以添加混合。但，在現狀，由於 -12- (10) 1353886 殘存於飛灰中之未燃碳（在火力發電所燃燒煤時’未燃燒 之碳成分是殘存數％以上）會對於水泥或混凝土造成壞影響 ，故在現在，無法進行該添加混合。 因此，若可從這樣的飛灰，有效地分離除去未燃碳， 將飛灰中之未燃碳含有率作成〇·5 %左右以下的話，則能夠 進行對水泥之添加混合。 在這樣的背景當中，利用灰與碳的電氣特性之差異的 φ 靜電分級受到注目，但目的物質的濃縮率（灰分的濃縮率 ，即減少飛灰中的未燃碳含有率）與分離回收效率（飛灰的 良率）雙方均未達到實用等級。 因此，將顯示對本發明的效果進行實驗性調查之結果 ，顯示如下。 在此實施例1，在將未燃碳含有率3.2質量％之飛灰供 給至靜電分離裝置前，使用做爲分散裝置之如圖1所示的 噴射器，藉由空氣予以分散。再者，在進行了分散後，使 φ 用電極間隔65mm之靜電分離裝置，將施加電壓設爲30kV ，使用乾燥空氣（溫度70°C、相對溼度10%)來進行分離。 其結果的一部分如圖8所示。在此圖中，空氣的供給壓力 爲〇之數値是未使用此分散裝置即以往之情況。由圖可知 ，藉由使用噴射器，可使未燃碳含有率大幅減低，並且良 率也大幅度地上升。又，亦可知，空氣的供給壓力具有適 當的範圍。 藉此，已分離的低碳含有側（灰的濃縮側）之未燃碳含 有率達到可添加混合至水泥之値，另一方面，由於良率也 -13- (11) 1353886 大幅地提稱，故成爲廢棄對象之高碳含有側（碳的濃縮側） 之灰的量也急劇降低，使得碳含有率變高，因此亦暗示可 根據情況來做爲代替燃料來加以利用之可能性。 實施例2 : 在此實施例2，使用與實施例1相同之飛灰’以做爲分 散裝置之如圖3所示的管來進行分散，進行了相同的實驗 ® 。其結果的一部分顯示於圖9。 在此圖中，雷諾數爲1000以下的數値是與未使用此分 散裝置之情況大致相等的値。由圖可得知，藉由使用管， 可使未燃碳含有率大幅度地降低，且良率也提昇。 實施例3 : 在此實施例3，使用與實施例1相同之飛灰，試作如圖 5所示的銷式高速旋轉型分散裝置，進行了同樣的實驗。 • 其結果的一部分顯示於圖10。 在此圖中，銷的旋轉速度爲〇之數値是未使用此分散 裝置即以往之情況。由圖可知’藉由使用此分散裝置’可 使未燃碳含有率大幅減低’並且良率也大幅度地上升。又 ，亦可知，銷的旋轉速度具有適當的範圍。 實施例4 = 在此實施例3，使用與實施例1相同之飛灰，試作如圖 7(d)所示的環型分散裝置’進行了同樣的實驗。球的材質 -14- (12) 1353886 爲橡膠。其結果的一部分顯示於圖11。 雖未記載於此圖中，但未使用此分散裝置即以往之情 況的數値是與實施例1的供給壓力爲0之情況的値相同。由 圖可知，藉由使用此分散裝置，可使未燃碳含有率大幅減 低，並且良率也大幅度地上升。又，亦可知，在球的直徑 具有適當的範圍。 φ 實施例5 : 爲了將存在於以使用鐵製的粉碎媒體之球磨機所粉碎 的氮化矽粉末中之磨損鐵粉除去，而使用具有如圖5所示 的構造且內面均爲陶瓷製之銷的高速旋轉型分散裝置，進 行磁性分離之試驗者。其結果的一部分顯示於圖12。再者 ，在此，使用磁場強度5000e之滾筒型磁性分離裝置做爲 磁性分離裝置，以進行分離。 在圖12，銷的旋轉速度爲0之數値是未使用此分散裝 # 置即以往之情況。由圖可知，藉由此用此分散裝置，可大 幅地減低Fe含有率。又，亦可知，銷的旋轉速度具有適 當的範圍。 【圖式簡單說明】 圖1是顯示在此發明的第1方法所使用的噴射器之構造 的槪略圖。 圖2是顯示在此發明的第1方法所使用的其他噴射器之 構造的槪略圖。 •15- (13) 1353886 圖3是顯示在此發明的第1方法所使用的管之構造的槪 略圖。 圖4是顯示在此發明的第3方法所使用的葉片式分散裝 置之槪略圖。 圖5是顯示在此發明的第3方法所使用的銷式分散裝置 之槪略圖。 圖6是顯示在此發明的第3方法所使用的雙軸方式之銷 Φ 式分散裝置之槪略圖。 圖7是顯示在此發明的第4方法所使用的球塡充式分散 裝置之槪略圖。 圖8是顯示根據實施例1處理飛灰時的未燃碳含有率及 濃縮飛灰良率的圖。 圖9是顯示根據實施例2處理飛灰時的未燃碳含有率及 濃縮飛灰良率的圖。 圖10是顯示根據實施例3處理飛灰時的未燃碳含有率 • 及濃縮飛灰良率的圖。 圖11是顯示根據實施例4處理飛灰時的未燃碳含有率 及濃縮飛灰良率的圖。 圖12是顯示根據實施例5處理氮化矽粉末時的Fe含有 率的圖。 【主要元件符號說明】 1 :壓力計 2、4 :氣體 -16- (14)1353886 3 :原料粉體 5 :流量計 6 :葉片 7 :旋轉板 8 :突起狀物 9 :馬達 10 :銷Re = DU p I β -8- (6) 1353886 D : inner diameter of the tube U: gas velocity in the tube P: density of the gas #: viscosity coefficient of the gas supplied by the raw material powder 3 is as shown in Fig. 3 In the tube shown schematically, as shown by the Reynolds number, a strong turbulent flow (in the case of a Reynolds number of 30,000 or more, a turbulent flow) creates a strong® conflict between the particles, or between the particles and the tube wall. The agglomerated particles are dispersed. In this case, the tubes can also be plural and juxtaposed. Further, the cross-sectional shape of the tube is not particularly limited, and may be a circular shape or a rectangular shape. Further, the length of the tube is designed such that the residence time of the gas 4 in the tube is 0.005 seconds or longer. In Fig. 3, 5 is a flow meter. Third method: The third method of dispersing in advance is to separate the raw material powder before the mixed powder (raw material powder) in which the target substance particles to be separated and the non-objective particles are mixed and charged or magnetically separated. The target substance particles and the non-target substance particles are supplied to the container rotated at a peripheral speed of 5 m/s or more and desirably 15 to 5 〇 m/s or more in a continuous or batchwise manner. The particle agglomerates having different electrical characteristics (dielectric or electrical conductivity) or magnetic properties are sufficiently dispersed. Fig. 4 shows a dispersing device of a structure in which a plurality of blades 6 provided on the rotary plate 7 are rotated as a projection 8 in the container by a motor 9. Similarly, in Fig. 5, a disperser in which the motor 9 rotates a plurality of pins 10 provided on the rotary plate 7 as projections 8 to rotate in the container is shown. There may be many variations in the structure or shape of these (7) 1353886, but if the blade 6 or the pin 10 which rotates the supplied raw material powder 3 is given a structure for imparting an impact force or a shearing force, The shape is not limited. For example, a high-speed rotary impact pulverizer such as a pin mill or a vane mill can be applied to the dispersion of the present invention. When the speed of the blade or the pin is too slow, the dispersion becomes insufficient, and when it is too fast, the pulverization is caused at the same time, causing an increase in the fine powder, which is undesirable in the separation efficiency. Moreover, in the case where the rotational speed is excessive, it is not economical in terms of equipment cost and energy consumption. Moreover, in the dispersing device of the structure of FIG. 4 or FIG. 5, at least two rotating shafts may be disposed coaxially to rotate the protrusions attached to the respective rotating shafts so that the respective protrusions are closest to each other. The relative peripheral speed of the partial rotation of the projections is 5 m/s or more when the relative circumferential speed is at the maximum position. Fig. 6 is a view showing an example of a pin grinder provided with two rotating shafts. In Fig. 6, the shaft 11a and the shaft lib are disposed coaxially, and the pins 11a and l〇c are attached to the shaft 11a, and the pin 10b is attached to the shaft lib. In the "the portion where the respective protrusions are closest to each other", "the (relative circumferential speed) forms the largest position", and Fig. 6 refers to the pin 10a and the pin 10b, so that the axes l〇a and l〇 b is rotated such that the relative peripheral speed of the pin 10a and the pin 10b forms 5 m/s or more. In this case, the relative peripheral speed of the pin l〇b and the pin 10c is formed to be smaller than the relative peripheral speed of the pin i〇a and the pin l〇b, and the maximum position is formed at the relative peripheral speed, that is, the protrusion is closest to the same. In part, the radial position from the rotation axis is the outermost side, and as shown in Fig. 6, the relative circumferential speed of the pin 10a and the pin 10b is 5 m/s or more. The shaft 11a and the shaft lib can also rotate in opposite directions to each other, and the -10- 1353886 (6) can be rotated in the same direction. Further, the form of the dispersing device is not limited to the pin method as shown in Fig. 6. At least two rotating shafts that are individually rotated and protrusions that are mounted on the respective rotating shafts may be attached, and the respective protrusions may be rotated at a relative peripheral speed of 5 m/s or more. The same dispersion effect as described above can be obtained by putting the raw material powder into such a container. The fourth method: • The fourth method of dispersing in advance is to charge or mix the mixed powder (raw material powder) in which the target material particles and the non-target material particles to be separated are separated, as shown in Fig. 7 It is shown that a ball having a ball equivalent diameter (the diameter of the ball when a ball of the same volume is assumed) is 1 mm to 60 mm, and a ball of 5 mm to 4 mm is desirably used as a container for a dispersion medium by rotating the container' or The rotating shaft and the stirring rod engaged with the rotating shaft are rotated inside the container to move the ball as a dispersion medium, and the raw material powder is continuously or batch-treated to the container to make the target substance particles and non-target substances ® particles are particle agglomerates with different electrical properties (dielectric or electrical conductivity) or magnetic properties that are sufficiently dispersed. Depending on the stirring blade or the stirring rod, the spiral type shown in Fig. 7(a), the disc type shown in Fig. 7(b), the stirring tank type shown in Fig. 7(c), and Fig. 7(d) are provided. The ring shape or the like shown in the figure is not particularly limited in the shape of the container and the direction of the rotation axis, and the rotation axis may be horizontal or vertical. For example, a ball mill or a media agitating mill can be easily used for the dispersion of the present invention. When the diameter of the ball is too small, the passage resistance of the raw material powder becomes large, and it becomes difficult to continuously supply. Further, in a batch type, it is difficult to discharge the powder after dispersing -11 - (9) 1353886 (with the ball Separation). In addition, when the ball is too large, the gap between the balls becomes large, so that the ratio of the raw material powder that is not dispersed and directly passes through becomes high, and since the impact force of the ball becomes large, the effect of agglomerating the fine powder is also generated. Therefore it is not ideal. Also, when the ball becomes larger, the torque applied to the shaft is excessive, and the shaft does not rotate. Here, the shape of the dispersion medium to be filled in the container is not particularly limited if the ball equivalent diameter is the same as the ball. Further, the material can be selected from wood, cork, rubber, plastic, ceramic, metal, etc. depending on the cohesive strength of the raw material powder. Further, the average residence time of the raw material powder in the container is desirably 10 minutes or less because it is required to be formed so as not to cause excessive fine powder as the pulverization operation proceeds. [Example j: Example 1: Coal ash (fly ash) produced by power generation stations nationwide, about 1000 ton tons a year. From the viewpoint of effective utilization of resources in the future, the use of ash with low odor carbon Will increase, it is expected that the amount of fly ash will increase. Of this, about 60% are manufactured in cement and used as part of its raw materials, which are used in quantities that have reached the limit as a chemical component of cement. Most of the residue is buried and disposed of. This burial is not an expected action in terms of environmental countermeasures. In order to further increase the amount of fly ash used in the field of cement, it is not used as a raw material to date, but is added and mixed in the range specified by JIS (Japanese Industrial Standard). However, in the current situation, the unburned carbon remaining in the fly ash due to -12-(10) 1353886 (the unburned carbon component is more than a few percent when burning coal in a thermal power plant) will have a bad influence on cement or concrete. Therefore, at this time, the addition and mixing cannot be performed. Therefore, if the unburned carbon is effectively separated and removed from such fly ash, and the unburned carbon content in the fly ash is about 5% or less, the addition and mixing of the cement can be performed. In such a background, φ electrostatic classification using the difference in electrical characteristics of ash and carbon is attracting attention, but the concentration ratio of the target substance (concentration rate of ash, that is, reduction of unburned carbon content in fly ash) and separation and recovery efficiency (The yield of fly ash) neither of them reached the practical level. Therefore, the results of an experimental investigation of the effects of the present invention will be shown as follows. In the first embodiment, before the fly ash having an unburned carbon content of 3.2% by mass is supplied to the electrostatic separation device, the ejector shown in Fig. 1 as a dispersing device is used, and dispersed by air. Further, after the dispersion was carried out, an electrostatic separation device having a φ interval of 65 mm was used, and an applied voltage was set to 30 kV, and separation was performed using dry air (temperature: 70 ° C, relative humidity: 10%). A part of the result is shown in Fig. 8. In this figure, the supply pressure of the air is the number of enthalpy, which is the case where the dispersing device is not used. As can be seen from the figure, by using the ejector, the unburned carbon content can be greatly reduced, and the yield is also greatly increased. Further, it is also known that the supply pressure of air has an appropriate range. Thereby, the unburned carbon content of the separated low-carbon containing side (the concentrated side of the ash) reaches the enthalpy which can be added and mixed to the cement, and on the other hand, the yield is also greatly improved by the -13-(11) 1353886 Therefore, the amount of ash which is a high-carbon-containing side (concentrated side of carbon) to be discarded is also drastically lowered, and the carbon content rate is increased. Therefore, it is also suggested that it may be used instead of fuel depending on the situation. Example 2: In this Example 2, the same experiment was carried out by using the same fly ash as in Example 1 to disperse the tube as shown in Fig. 3 as a dispersing device. A part of the result is shown in Fig. 9. In this figure, the number of Reynolds numbers below 1000 is approximately equal to the case where the dispersing device is not used. As can be seen from the figure, by using the tube, the unburned carbon content can be greatly reduced, and the yield is also improved. [Example 3] In this Example 3, the same experiment was carried out by using the same fly ash as in Example 1 to test the pin type high-speed rotary type dispersing device shown in Fig. 5. • A portion of the results is shown in Figure 10. In this figure, the rotation speed of the pin is the number of turns, which is the case where the dispersing device is not used. As can be seen from the figure, by using the dispersing device, the unburned carbon content can be greatly reduced, and the yield is also greatly increased. Further, it is also known that the rotation speed of the pin has an appropriate range. [Example 4] In this Example 3, the same experiment was carried out using the same fly ash as in Example 1, and the ring type dispersing device shown in Fig. 7(d) was tried. The material of the ball -14- (12) 1353886 is rubber. A part of the result is shown in Fig. 11. Although not shown in the figure, the number of conventional cases in which the dispersing device is not used is the same as that in the case where the supply pressure of the first embodiment is zero. As can be seen from the figure, by using this dispersing device, the unburned carbon content can be greatly reduced, and the yield is also greatly increased. Further, it is also known that the diameter of the ball has an appropriate range. φ Example 5: In order to remove the worn iron powder present in the tantalum nitride powder pulverized by a ball mill using a pulverization medium made of iron, the structure shown in Fig. 5 was used and the inner surface was made of ceramic. A high-speed rotary type dispersing device for pins, which is a tester for magnetic separation. A part of the result is shown in Fig. 12. Further, here, a drum type magnetic separation device having a magnetic field strength of 5000 e is used as a magnetic separation device for separation. In Fig. 12, the rotation speed of the pin is 0, which is the case where the dispersion is not used. As can be seen from the figure, by using this dispersing device, the Fe content can be greatly reduced. Further, it is also known that the rotation speed of the pin has an appropriate range. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a schematic view showing the structure of an ejector used in the first method of the present invention. Fig. 2 is a schematic view showing the structure of another injector used in the first method of the invention. • 15-(13) 1353886 Fig. 3 is a schematic view showing the structure of a tube used in the first method of the present invention. Fig. 4 is a schematic view showing a vane type dispersing device used in the third method of the present invention. Fig. 5 is a schematic view showing a pin type dispersing device used in the third method of the invention. Fig. 6 is a schematic view showing a pin-type Φ type dispersing device of a two-axis type used in the third method of the present invention. Fig. 7 is a schematic view showing a ball-filling type dispersing device used in the fourth method of the present invention. Fig. 8 is a graph showing the unburned carbon content and the concentrated fly ash yield when the fly ash is treated according to Example 1. Fig. 9 is a graph showing the unburned carbon content and the concentrated fly ash yield when the fly ash is treated according to Example 2. Fig. 10 is a graph showing the unburned carbon content rate and the concentrated fly ash yield when the fly ash is treated according to Example 3. Fig. 11 is a graph showing the unburned carbon content and the concentrated fly ash yield when the fly ash is treated according to Example 4. Fig. 12 is a graph showing the Fe content in the case of treating tantalum nitride powder according to Example 5. [Main component symbol description] 1 : Pressure gauge 2, 4: Gas -16- (14) 1353886 3 : Raw material powder 5 : Flowmeter 6 : Blade 7 : Rotating plate 8 : Protrusion 9 : Motor 10 : Pin
11a〜lie:軸11a~lie: Axis
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