TWI280951B - Fluidized-bed process drain treatment system - Google Patents
Fluidized-bed process drain treatment system Download PDFInfo
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1280951 九、發明說明： ® 【翻臓之撕領域】 本發明大致係有關於工業製程水溶液或排放廢液之一種處 理系統，特別是有關於在最佳反應條件下，利用最小流體化床 ^ 反應器進行快速製程水溶液或廢液處理之一種系統。 ^ 【先前技術】 各種工業製程廢液的排放，在環境保護意識高張的今日， ^ 已受到環保規章的嚴格規範。為符合廢液排放標準，針對不同 產業的不同性質廢液，常須使用一定繁複程度的處理設備，以 使排放水及殘餘污泥分別符合排放及掩埋標準。以流體化床反 φ 應器為基礎的處理設備，基於其特性本質，亦應用於多種諸如 移除廢液中之鹵素(諸如氟)，鹼土金屬(鈣及鎂等)，重金屬(鎳， 鎘及鉻等)，以及有機物等的處理系統之中。另一方面，各種工 業製程所需含不问濃度之上述金屬非金屬兀素或離子的水溶 ^ 液，同樣亦需使用類似定繁複程度的處理設備，以使水溶液符 合製程需求標準。 ’ 不過，習知技術之流體化床反應器為基礎之處理系統，其 ^ 設計並未考量其使用目的之最佳化。若進流液之濃度變化較 大，便無法達到其最快速之反應速率。其結果是系統中的處理 液，由於反複循環處理之故而使處理總體積加大，反應時間延 ® 長，設施場地需求加大。所有這些不利因素皆直接轉換成為運 1280951 作成本的增加。處理液量加大表示需要對等較大動力的泵，而 ® 較大尺寸體積的設施則需要相對較大的設施場地空間。有時， 由於進流液之濃度變動超越原設計的狹小範圍，更可能會使系 統完全無法操作。 ^ 此外，許多製程排液之中事實上内含了有價值的物質。由 、 於回收此些有用物質的商業價值，時常無法合理彌補回收所需 要增加製程設備的成本因此便被含在排放水或傾倒/掩埋污泥 • 中而排放丟棄。傳統上，附帶副產品的回收只是製程排液處理 的次要目標，次於廢水及污泥排放掩埋符合規章的主要處理目 標。 Φ 習知技藝的處理系統之中，縱然其使用目標之處理有某操 作條件達到了最佳化，但通常其他的操作條件則無法同時亦達 |成最佳化。習知技藝以流體化床反應器為基礎的處理系統，其 •設計時並未將符合於使用目的之系統性最佳化列入主要考 • 量。簡言之，習知的流體化床處理系統離系統複雜度，最快反 應速率，以及副產物的產出等使甩條件同時最佳化的達成，有 ， 相當遙遠的距離。 【發明内容】 因此，有需要提供可以達成系統性操作條件最佳化之一種 流體化床製程水溶液處理系統以減低處理系統之建造及運轉 12809511280951 IX. INSTRUCTIONS: ® [Tearing field of tumbling] The present invention relates generally to a treatment system for aqueous solutions or waste liquids for industrial processes, in particular for the use of minimum fluidized bed reactions under optimal reaction conditions. A system for rapid process aqueous or waste treatment. ^ [Prior Art] The discharge of various industrial process waste liquids, today in the awareness of environmental protection, has been strictly regulated by environmental regulations. In order to comply with the waste discharge standards, it is often necessary to use a certain degree of processing equipment for different types of waste liquids in different industries, so that the discharged water and residual sludge meet the discharge and landfill standards respectively. Treatment equipment based on fluidized bed anti-φ reactors, based on its characteristic nature, is also used in a variety of halogens such as fluorine (such as fluorine), alkaline earth metals (calcium and magnesium, etc.), heavy metals (nickel, cadmium). And chromium, etc., and processing systems such as organic matter. On the other hand, various industrial processes require water-soluble liquids containing the above-mentioned metal non-metal alkaloids or ions, regardless of the concentration, and similarly complex processing equipment is required to make the aqueous solution meet the process requirements. However, the fluidized bed reactor-based processing system of the prior art does not consider the optimization of its intended use. If the concentration of the influent changes greatly, the fastest reaction rate cannot be achieved. As a result, the treatment liquid in the system is increased in total volume due to repeated cycle treatment, the reaction time is extended, and the demand for the facility site is increased. All of these unfavorable factors are directly converted into an increase in the cost of shipping 1280951. An increase in the amount of treatment fluid indicates that a pump with a relatively large power is required, while a larger size facility requires a relatively large facility space. Sometimes, because the concentration of the incoming fluid changes beyond the narrow range of the original design, it is more likely that the system will be completely inoperable. ^ In addition, many process liquids actually contain valuable substances. By recovering the commercial value of these useful substances, it is often impossible to make up for the cost of the process equipment. The cost of the process equipment is increased and therefore discarded in the discharge water or dumping/buried sludge. Traditionally, the recovery of incidental by-products is only a secondary goal of process drainage, and is secondary to the main treatment targets for wastewater and sludge discharge burial. Φ In the processing system of the prior art, even if the operating conditions of the target are optimized, some other operating conditions cannot be optimized at the same time. Conventional techniques are based on fluidized bed reactors, which are not designed to incorporate systemic optimization for the intended use. In short, the conventional fluidized bed processing system achieves a relatively long distance from the system complexity, the fastest reaction rate, and the by-product output, which simultaneously optimize the enthalpy conditions. SUMMARY OF THE INVENTION Accordingly, there is a need to provide a fluidized bed process aqueous solution treatment system that optimizes systemic operating conditions to reduce the construction and operation of the processing system.
另亦有需要提供可以達成系統性操作條件最佳化之一種流 體化床製程水溶液處理系統，達成最快可能之反應速率，以及 最小可能之設施空間需求。 另亦有需要提供可以達成系統性操作條件最佳化之一種流 體化床製程水溶液處理系紘以達成最清潔之排放水及最少之 污泥量。 另亦有需要提供可以達成系統性操作條件最佳化之一種流 體化床製程水溶液處理系統以由排液之中回收有商業價值之 物質。 為達成前述及其他目的，本發明提供工業製程水溶液處理 系統之一種流體化床反應器，該處理系統之一配管網路包含有 一處理液供應配管系及一反應劑供應配管系，可對該流體化床 反應器分別供應處理液及反應劑，以反應處理該工業製程水溶 液而排出淨水。該流體化床反應器包含有一反應段，由包含至 少一反應單元的一反應器核心組件所構成並接受該排出淨水 之一部份之輸入做為迴流水。該至少一反應單元内包含至少一 處理液饋入組件，包含有連接至該處理液供應配管系的一處理 液配管及其上散佈的複數個噴嘴，·與至少一反應劑供應組件， 包含有連接至該反應劑供應配管系的一反應劑配管及其上散 佈的複數個噴嘴；其中該些配管上之該些噴嘴之散佈可將該處 理液及該反應劑與該迴流水充份混合，且充份反應形成反應結 8 1280951 晶懸浮於該反應段内之處理液流中，以排出處理液為處理完成 之淨水。 本發明亦提供一種流體化床製程水溶液處理系統，用於工 業製程水溶液之處现其包含有一配管網路及一流體化床反應 器。該配管網路包含有一處理液供應配管系及一反應劑供應配 管系，可分別供應處理液及反應劑，以反應處理該工業製程水 溶液而排出淨水。該流體化床反應器包含有一反應段，由包含 至少一反應單元的一反應器核心組件所構成並接受該排出淨 水之一部份之輸入做為迴流水；該至少一反應單元内包含有至 少一處理液饋入組件，包含有連接至該處理液供應配管系的一 處理液配管及其上散佈的複數個噴嘴·，與至少一反應劑供應組 件，包含有連接至該反應劑供應配管系的一反應劑配管及其上 散佈的複數個噴嘴；其中該些配管上之該些噴嘴之散佈可將該 處理液及該反應劑與該迴流水充份混合，且充份反應形成反應 結晶懸浮於該反應段内之處理液流中，以排出處理液為處理完 成之淨水。 :實施方式】 本發明後面的說明文字之中係以製程水溶液來泛指包含工 業製程排放廢液及工業製程所需使用之原料水溶液。 圖1之透視圖顯示依據本發明一較佳實施例之製程水溶液 處理系統，其流體化床反應器(fluidized-bedreactor，此後簡稱 1280951 為FBR)之構造。依據本發明較佳實施例之一 FBR 1001,係為 大致1：立之一柱形構遙且其大致柱形之本體具有圓形之橫截 面。如同習於本技藝者所可以理解的，雖然非圓形橫截面亦屬 可行，但圓形的橫截面至少具有結構強度，體積最佳化，以及 反應均勻化等方面的優點。There is also a need to provide a fluidized bed process aqueous treatment system that optimizes systemic operating conditions to achieve the fastest possible reaction rate and the smallest possible facility space requirement. There is also a need to provide a fluidized bed process aqueous treatment system that achieves optimal system operating conditions to achieve the cleanest discharge water and the minimum amount of sludge. There is also a need to provide a fluidized bed process aqueous solution treatment system that optimizes systemic operating conditions to recover commercially valuable materials from the liquid discharge. To achieve the foregoing and other objects, the present invention provides a fluidized bed reactor for an industrial process aqueous solution treatment system, wherein the piping network includes a treatment liquid supply piping system and a reactant supply piping system for the fluid The chemical bed reactor supplies a treatment liquid and a reactant, respectively, to react and treat the industrial process aqueous solution to discharge the purified water. The fluidized bed reactor comprises a reaction section formed by a reactor core assembly containing at least one reaction unit and receiving an input of a portion of the discharged purified water as reflux water. The at least one reaction unit comprises at least one processing liquid feeding assembly, comprising a processing liquid pipe connected to the processing liquid supply piping system and a plurality of nozzles dispersed thereon, and at least one reactant supply component, including a reactant pipe connected to the reactant supply piping system and a plurality of nozzles dispersed thereon; wherein the dispersion of the nozzles on the pipes can thoroughly mix the treatment liquid and the reaction agent with the reflux water, And fully reacted to form a reaction knot 8 1280951 crystal suspended in the treatment liquid stream in the reaction section, to discharge the treatment liquid as the treated purified water. The present invention also provides a fluidized bed process aqueous solution treatment system for use in industrial process aqueous solutions which now includes a piping network and a fluidized bed reactor. The piping network includes a processing liquid supply piping system and a reactant supply piping system for separately supplying a processing liquid and a reactant to react the industrial process water solution to discharge the purified water. The fluidized bed reactor comprises a reaction section comprising a reactor core assembly comprising at least one reaction unit and receiving an input of a portion of the discharged purified water as reflux water; the at least one reaction unit comprising At least one processing liquid feed-in assembly, comprising a processing liquid pipe connected to the processing liquid supply piping system and a plurality of nozzles dispersed thereon, and at least one reactant supply assembly including a reagent supply piping a reagent pipe and a plurality of nozzles dispersed thereon; wherein the spraying of the nozzles on the pipes can thoroughly mix the treatment liquid and the reactant with the reflux water, and fully react to form reaction crystallization Suspended in the treatment liquid stream in the reaction section, the treatment liquid is discharged as the treated purified water. : Embodiments In the following description of the present invention, a process aqueous solution is used to refer to an aqueous solution containing raw materials for industrial process discharge and industrial processes. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a perspective view showing a configuration of a process aqueous solution processing system in which a fluidized-bed reactor (hereinafter referred to as 1280951 is FBR) according to a preferred embodiment of the present invention. According to one of the preferred embodiments of the present invention, the FBR 1001 is substantially a columnar cylindrical body and has a substantially cylindrical body having a circular cross section. As will be appreciated by those skilled in the art, although a non-circular cross section is also possible, the circular cross section has at least the advantages of structural strength, volume optimization, and uniformity of the reaction.
圖1中所顯示之FBR 1001之較佳實施例係包含有一反應段 (reaction section) 1100。順著其所處理之製程水溶液由下向上 之流動方向，其亦可包含有一主迴流饋注段(main recycle flow feed section) 1400，一反應穩定段(settlement section) 1200，以 及一緩衝段(buffer section) 1300。圖中以虛線沿著液流方向大 致區分FBR 1001的此些構造區段。 反應段1100事實上是為本發明FBR 1001的主要反應構 件，其係由反應器核心組件(reactor core assembly) 1101所構 成。在本發明之較佳實施例之中，反應器核心組件1101可包 含一或多組的反應單元(reactionunits)如圖1中所顯示之二組 反應單元1110及1120。每一反應單元各包含有至少一處理液 饋入組件(process solution influent feed assembly)及至少一反應 劑供應組件(reagent supply assembly)。例如，圖1之實施例中 顯示反應段1100之反應單元1110包含有一處理液饋入組件 1111及一反應劑供應組件1114。反應單元1120則包含有一處 理液饋入組件1121及一反應劑供應組件1124。 1280951The preferred embodiment of FBR 1001 shown in Figure 1 includes a reaction section 1100. The process aqueous solution processed therewith may be flowed from bottom to top, and may also include a main recycle flow feed section 1400, a reaction section 1200, and a buffer section (buffer). Section) 1300. The structural sections of the FBR 1001 are largely distinguished by a dashed line along the flow direction. Reaction section 1100 is in fact the primary reaction component of FBR 1001 of the present invention, which is comprised of reactor core assembly 1101. In a preferred embodiment of the invention, reactor core assembly 1101 may comprise one or more sets of reaction units such as two sets of reaction units 1110 and 1120 as shown in FIG. Each of the reaction units each includes at least one process solution influent feed assembly and at least one reagent supply assembly. For example, the reaction unit 1110 showing the reaction section 1100 in the embodiment of Fig. 1 includes a treatment liquid feedthrough assembly 1111 and a reactant supply assembly 1114. The reaction unit 1120 includes a treatment liquid feed assembly 1121 and a reactant supply assembly 1124. 1280951
每一處理液饋入組件係由一組連接至FBR 1001本體之外 的配管及配管上所適當分佈的多個噴嘴所構成的。例如，處理 液饋入組件1111包含了配管1111T及沿其管路排列的多個處 理液噴嘴1111N，處理液饋入組件1121則包含了配管1121T 及多個處理液噴嘴1121N。 另一方面，每一反應劑供應組件則是由一組亦連接至FBR 1001本體之外的配管及配管上所適當分佈的多個噴嘴所構 成。例如，反應劑供應組件1114包含了配管1114T及沿其管 路排列的多個反應劑噴嘴1114Ν,反應劑供應組件1124則包 含了配管1124Τ及多個反應劑噴嘴1124Ν。 注意到圖中所顯示的配管係為單圈圓形配管，但如同可以 理解的，只要有助於處理液與反應劑的充份混合，任合形狀的 配管以及噴嘴分佈形態，皆是屬可行的作法。此外，每一反應 單元中的個別處理液饋入組件係可用以分別對反應器供應不 同濃度的處理液。如此，本發明之反應器便可以適用於濃度範 圍極大的處理原液之處理應用用途。一般性的原則是，較低濃 度的處理液可由位處較下游(即較上方)的組件來供應，而較高 濃的處理液則應由較上游(較下方)的組件供應。此種作法可令 較高濃度的處理液流經相對較長的流路，以便有機會充份與反 應劑供應組件所供應的反應劑進行化學反應。 反應穩定段1200基本上是一段沿著主體流路方向逐漸增加 1280951Each of the processing liquid feedthrough modules is composed of a plurality of pipes connected to the outside of the FBR 1001 body and a plurality of nozzles appropriately distributed on the pipes. For example, the processing liquid feeding unit 1111 includes a pipe 1111T and a plurality of processing liquid nozzles 1111N arranged along the piping thereof, and the processing liquid feeding unit 1121 includes a pipe 1121T and a plurality of processing liquid nozzles 1121N. On the other hand, each of the reactant supply modules is constituted by a group of pipes which are also connected to the outside of the body of the FBR 1001 and a plurality of nozzles which are appropriately distributed on the pipes. For example, the reactant supply unit 1114 includes a pipe 1114T and a plurality of reactant nozzles 1114A arranged along the tube thereof, and the reactant supply unit 1124 includes a pipe 1124A and a plurality of reactant nozzles 1124A. Note that the piping shown in the figure is a single-circle circular piping, but as can be understood, as long as it contributes to the sufficient mixing of the treatment liquid and the reactants, any shape of the piping and the nozzle distribution form are feasible. Practice. In addition, individual treatment fluid feed components in each reaction unit can be used to supply different concentrations of treatment fluid to the reactor, respectively. Thus, the reactor of the present invention can be applied to treatment applications in which the concentration of the raw liquid is extremely large. The general rule is that a lower concentration of treatment fluid can be supplied from a downstream (i.e., higher) component, while a higher concentration treatment fluid should be supplied from an upstream (lower) component. This practice allows a higher concentration of treatment fluid to flow through a relatively long flow path to provide an opportunity to chemically react with the reactants supplied by the reagent supply assembly. The reaction stabilization section 1200 is basically a section that gradually increases along the direction of the main body flow path 1280951
流路面積的柱狀管體圖1之實施例中顯示其反應穩定段1200 係具有圓錐體的一個段落的形狀。此種構造可令流經其中的處 理液順著流路的方向，由於流路面積加大而逐漸減緩其流速。 緩衝段1300之作用係在為經化學反應後的處理液，提供排 出FBR 1001之前的一段緩衝距離，其基本上可以是一段單純 的圓柱形管體。本發明之製程水溶液處理系統，其主要反應單 元FBR 1001係屬一種高效能最佳化之反應單元，系統中之處 理液只須流經反應單元一次，不需重覆循環回到反應單元，便 能獲得完全的處理效果。在圖1之實施例之中，FBR 1001的 主要處理反應，如伺前述，主要係於反應段1100所涵蓋之反 應區(reaction zone) 1100A之中進行並完成的。殘餘的反應可 以在反應穩定段1200中充份進行。若因上游製程條件的變 動，處理液本身的成份亦大符變動，緩衝段1300便可以提供 緩衝，確保通過緩衝段1300後排出的處理液能夠保持一定的 處理水準。 主迴流饋注段1400,如圖1之實施例所顯示的，係為連接 於FBR 1001本體最下端的一段向下縮小的錐形構造。在本發 明之處理系統之中，主迴流饋注段1400係為整個FBR 1001 内流通的處理液的主要供應來源。在典型的廢液處理應用之較 佳實施例之中，主迴流饋注段1400可能會提供多達六分之五 的回流水的流量。 12 1280951Columnar Tube of Flow Path Area The embodiment of Figure 1 shows that its reaction stabilizing section 1200 has the shape of a section of a cone. This configuration allows the treatment liquid flowing therethrough to follow the direction of the flow path, and gradually slows down the flow rate due to the increased flow path area. The buffer section 1300 functions as a buffering distance for the chemically treated treatment fluid prior to discharge of the FBR 1001, which may be substantially a simple cylindrical tubular body. In the process aqueous solution treatment system of the invention, the main reaction unit FBR 1001 belongs to a high-efficiency optimization reaction unit, and the treatment liquid in the system only needs to flow through the reaction unit once, and does not need to be repeatedly recycled back to the reaction unit. Can get complete processing results. In the embodiment of Figure 1, the primary treatment reaction of FBR 1001, as previously described, is primarily carried out and carried out in a reaction zone 1100A covered by reaction zone 1100. The residual reaction can be carried out in sufficient portions in the reaction stabilization section 1200. If the composition of the treatment liquid itself changes greatly due to the change of the upstream process conditions, the buffer section 1300 can provide a buffer to ensure that the treatment liquid discharged through the buffer section 1300 can maintain a certain level of treatment. The main return feed section 1400, as shown in the embodiment of Figure 1, is a downwardly tapered conical configuration attached to the lowermost end of the body of the FBR 1001. In the processing system of the present invention, the main return feed section 1400 is the primary source of supply of processing liquid throughout the FBR 1001. In a preferred embodiment of a typical waste treatment application, the main return feed section 1400 may provide up to five-sixths of the flow of reflux water. 12 1280951
注意到主迴流饋注段1400與反應段1100之間係以反應器 底板1105實質地互相隔開。底板1105以下的空間1400A係作 為迴流分配區，而反應器底板1105上則適當地分佈配置有多 個迴流液分配噴嘴1108。透過此些迴流液噴嘴1108,系統可 以經由主迴流饋注段1400其錐形構造錐尖底部的重力逆止閥 (checkvalve) 1411,將FBR 1001本身將其緩衝段1300所輸出 之迴流液饋注回到主處理液流之中。 主迴流饋注段1400的此種迴流饋入，至少有兩個主要目 的。其一係在於適當地稀釋系統所要處理，即經由處理液饋入 組件(1111等)而饋入系統内之處理液，以使系統得以在最佳條 件之下操作。另一目的係在於維持適當之處理液流速，以使處 理反應所形成之晶粒，得以相對對地零速度而實質地懸浮於反 應單元1100内的反應區;1100A之内。如同可以理解者，要形 成晶粒懸浮的反應區1100A，則晶粒的沉降速度須與處理液之 流速達成平衡。 主迴流饋注段1400的迴流饋入，至少亦可有另一目的，即 對處理液加入其他必要的化學反應劑與/或其他有助於主反應 的，諸如輔助攪拌混合的物理作用氣體，例如空氣，或用於殺 菌用的臭氧等。如同後面將說明的，透過一個與主迴流液供應 管路混合的供應管，便可以在控制之下供應此些調節氣/劑/ 液。當然，在不進行此些額外的調節時，該個混合管道是關閉 13 1280951 的。主迴流饋注段1400在其錐形構造的錐尖底部的逆止閥 1411，除了隨需求而供應調結液之外，亦可以，例如，於FBR 1001進行維修時，用於排空FBR 1001本體内的處理液。 圖1之實施例FBR 1001，於反應段1100的接近底部之處， 可以裝設一根反應產物排放管(reaction product discharge port) 1109。製程水溶液經過與反應劑進行化學反應之後所形成之結 晶體，可經由此反應產物排放管排出。視結晶物之性質而定， 此排出之反應產物可以經過再處理，而成為有價值之原料，或 成為適於掩埋的無害底泥。 另一方面，FBR 1001亦可在主迴流饋注段1400的柱體上 接近底部之處裝設一根汙泥排放管1421。FBR 1001的持續長 時間反應所累積於主迴流饋注段1400内的底汙泥，可以經由 此汙泥排放管1421而排出。 圖2顯示本發明較佳實施例之製程水溶液處理系統，其流 體化床反應器内外之液流系統。FBR 1001作為本發明流體化 床製程水溶液處理系統之反應單元，係由反應段1100中所安 排之多組反應單元(諸如圖1中所顯示之多組反應單元1110及 1120等)來供應處理流體及必要之化學反應劑。有必要時，主 迴流饋注段1400亦可對FBR 1001中之主流體供應必要之調節 性的反應劑，或其他諸如增進攪拌混合作用的氣體等。 製程水溶液，作為本發明系統之處理液，係在FBR 1001的 14It is noted that the main reflux feed section 1400 and the reaction section 1100 are substantially separated from each other by the reactor bottom plate 1105. A space 1400A below the bottom plate 1105 serves as a return distribution zone, and a plurality of reflux liquid dispensing nozzles 1108 are appropriately disposed on the reactor bottom plate 1105. Through the reflux nozzles 1108, the system can feed the backflow of the buffer section 1300 by the FBR 1001 itself via a gravity check check valve 1411 at the bottom of the conical tip of the main recirculation feed section 1400. Return to the main treatment stream. This return feed of the main return feed section 1400 has at least two main purposes. The first is to properly treat the system to be processed, i.e., feed the treatment liquid into the system via the treatment fluid feed assembly (1111, etc.) to allow the system to operate under optimal conditions. Another object is to maintain a suitable flow rate of the treatment fluid so that the grains formed by the treatment reaction are substantially suspended in the reaction zone within the reaction unit 1100 at a relative zero velocity; within 1100A. As can be understood, to form the reaction zone 1100A in which the grains are suspended, the sedimentation velocity of the crystal grains must be balanced with the flow rate of the treatment liquid. The reflux feed of the main reflux feed section 1400 may have at least another purpose of adding other necessary chemical reactants to the treatment liquid and/or other physical interaction gases which contribute to the main reaction, such as assisted agitation mixing, For example, air, or ozone for sterilization. As will be explained later, these conditioning gases/agents/liquids can be supplied under control through a supply line that is mixed with the main reflux supply line. Of course, the mixing pipe is closed 13 1280951 without these additional adjustments. The main return feed section 1400 has a check valve 1411 at the bottom of the conical tip of the tapered configuration, in addition to supplying the conditioning liquid as needed, for example, for servicing the FBR 1001 when the FBR 1001 is being serviced. The treatment solution in the body. In the embodiment of Fig. 1, FBR 1001, a reaction product discharge port 1109 can be installed near the bottom of reaction section 1100. The crystal formed by the aqueous solution of the process is subjected to a chemical reaction with the reactant, and can be discharged through the reaction product discharge pipe. Depending on the nature of the crystallized material, the discharged reaction product can be reprocessed to become a valuable raw material or a harmless sediment suitable for burial. On the other hand, the FBR 1001 can also be provided with a sludge discharge pipe 1421 near the bottom of the column of the main return feed section 1400. The bottom sludge accumulated in the main reflux feed section 1400 of the FBR 1001 for a long period of time can be discharged through the sludge discharge pipe 1421. Figure 2 shows a process aqueous solution processing system in accordance with a preferred embodiment of the present invention, with a liquid flow system inside and outside the fluidized bed reactor. The FBR 1001 is a reaction unit of the fluidized bed process aqueous solution processing system of the present invention, which is supplied with a plurality of sets of reaction units (such as the plurality of sets of reaction units 1110 and 1120 shown in FIG. 1) arranged in the reaction section 1100. And the necessary chemical reactants. The main return feed section 1400 may also supply the necessary conditioning reactants to the primary fluid in the FBR 1001, or other gases such as those which promote agitation mixing, if desired. The process aqueous solution, as the treatment liquid of the system of the present invention, is in the FBR 1001 14
1280951 反應段1100内進行主要的化學反應。當處理液上流至反應穩 定段1200時，由於液流截面積加大，流速減緩，故而有機會 充份完成化學反應，以便在緩衝段1300的緩衝距離之下，確 保處理後排出的水質能夠符合要求。 圖2顯示一個配管系統150Q包含處理液供應配管系1510 及反應劑供應配管系1520,係透過一個控制閥系統而分別對 每一組的反應單元1110，1120，…及1130供應處理液及反應 劑。例如，處理液供應配管系1510可分別通過受控的閥1116, 1126, ···及1136而分別對各反應單元(1110, 1120等)的處理 液饋入組件1111，1121,…及1131供應處理液。另一方面， 反應劑供應配管系1520則可分別通過受控的閥111δ 112δ ... 及1139而分別對各反應單元的反應劑供應組件1114 1124 ··· 及1134供應反應劑。 控制閥系統中的每一個控制閥，即圖中之1116, 1126, ... 及1136，1129，以及m9，1129···及1139等，係可依處理液 的實際狀態，立用真時控制而即時地分別個別開啟，關斷或適 當地控制流量，以便以最佳配方為每一個反應單元1110, 1120, ...及1130供應比例適量之處理液及反應劑。如此即可 以確保每一個反應單元1110, 1120,…及1130的個別反應區 域内皆得以達成反應的最佳化。閥系統的開啟及關斷控制可利 用後面所將詳細說明的即時感應監控系統進行最佳化控制。 15 1280951 配管系統1500更包含有一個回流水配管系1530及一個放 流水配管系1540。注意到回流水配管系1530及放流水配管系 1540係分別由FBR 1001的緩衝段1300的頂端接管。如此便 可以在有需要時接引良好水質的回流水來進行處理液的稀釋。 圖3之橫截面圖顯示本發明製程水溶液處理系統其流體化 床反應器之反應單元之一較佳實施例構造。如同圖1及2中所 顯示的，本發明流體化床製程水溶液處理系統之中心，即反應 器核心組件1101，係可由多個結構相同的反應單元/沿著反 應器内處理液的基本液流上下游方向串接而成。依據系統所需 處理之能量而定，反應器核心組件使用單獨一個反應單元，亦 可以串接二個以上的反應單元，端視每一個別反應單元的單位 處理能量而定。例如，圖1所顯示之反應器核心組件1101即 使用了二個反應單元1110及1120。 如圖3之截面圖所顯示的，反應單元1110在其柱形(較佳者 為圓柱形)的槽體1102之内包含有兩種組件，即處理液及反應 劑之饋入供應組件。圖3之實施例之中，處理液之饋入組件包 含有組件1111，1112,…及1113等，而反應劑供應組件則包 含有1114及1115等。如同圖1中所說明的，每一個處理液饋 入組件及反應劑供應組件各係由一個供應管格及多個適當分 佈於管格上的供應噴嘴所構成的。 處理液及反應劑的所有此些饋入及供應組件，如圖所示， 16 12809511280951 The main chemical reaction takes place in reaction zone 1100. When the treatment liquid flows up to the reaction stabilization section 1200, since the cross-sectional area of the liquid flow is increased and the flow velocity is slowed down, there is an opportunity to fully complete the chemical reaction so as to ensure that the water discharged after the treatment can be met under the buffer distance of the buffer section 1300. Claim. 2 shows a piping system 150Q including a treatment liquid supply piping system 1510 and a reactant supply piping system 1520 for supplying a treatment liquid and a reactant to each of the reaction units 1110, 1120, ..., and 1130 through a control valve system. . For example, the treatment liquid supply piping system 1510 can supply the treatment liquid feed components 1111, 1121, ..., and 1131 of the respective reaction units (1110, 1120, etc.) through the controlled valves 1116, 1126, ..., and 1136, respectively. Treatment fluid. On the other hand, the reactant supply piping system 1520 can supply the reactants to the reactant supply units 1114 1124 ··· and 1134 of the respective reaction units through the controlled valves 111δ 112δ ... and 1139, respectively. Each control valve in the control valve system, that is, 1116, 1126, ... and 1136, 1129, and m9, 1129··· and 1139 in the figure, can be used according to the actual state of the treatment liquid. The flow is controlled, and individually turned on, turned off, or appropriately controlled, so that an appropriate amount of the treatment liquid and the reactant are supplied to each of the reaction units 1110, 1120, ..., and 1130 in an optimum formulation. This ensures that the reaction is optimized in the individual reaction zones of each of the reaction units 1110, 1120, ... and 1130. The valve system's opening and closing control can be optimally controlled using an instant sensing monitoring system as described in more detail below. 15 1280951 The piping system 1500 further includes a return water piping system 1530 and a discharge water piping system 1540. It is noted that the return water piping system 1530 and the discharge water piping system 1540 are respectively taken over by the tip end of the buffer section 1300 of the FBR 1001. In this way, it is possible to dilute the treatment liquid by receiving reflux water of good water quality when necessary. BRIEF DESCRIPTION OF THE DRAWINGS Figure 3 is a cross-sectional view showing the construction of a preferred embodiment of a reaction unit of a fluidized bed reactor of the aqueous solution processing system of the present invention. As shown in Figures 1 and 2, the center of the fluidized bed process aqueous solution processing system of the present invention, i.e., the reactor core assembly 1101, can be comprised of a plurality of identically configured reaction units/substantial flow of processing liquid along the reactor. The upstream and downstream directions are connected in series. Depending on the energy required to be processed by the system, the reactor core assembly may use a single reaction unit or two or more reaction units in series, depending on the unit processing energy of each individual reaction unit. For example, the reactor core assembly 1101 shown in Figure 1 utilizes two reaction units 1110 and 1120. As shown in the cross-sectional view of Fig. 3, the reaction unit 1110 contains two components, a feed solution and a feed supply component of the reactant, within its cylindrical (preferably cylindrical) tank body 1102. In the embodiment of Fig. 3, the feedthrough component of the treatment liquid contains components 1111, 1112, ..., 1113, etc., and the reagent supply component contains 1114, 1115, and the like. As illustrated in Figure 1, each of the process fluid feed assembly and the reactant supply assembly is comprised of a supply manifold and a plurality of supply nozzles suitably disposed on the manifold. All of these feed and supply components for the treatment and reagents, as shown, 16 1280951
係沿著反應單元1110内之處理液流方向，依適當間隔而安裝 於槽體1102之内β在圖3之實施例之中，處理液饋入組件 1111, 1112,…及1113等係安裝於反應單元m〇内由下向上 液流的上游，而反應劑供應組件1114及1115等則相對安裝於 下游。反應單元1110内之兩種組件可以依任何適當的間插或 群組集中的方式排列於槽體1102之内。其排列方式主要的考 量係在於可令各噴嘴所噴出之處理液及反應劑達成最大亂 流，以便在FBR系統的主迴流饋注段1400所饋注的大流量迴 流液之中使兩者充份混合，達成最大程度的化學反應。 例如，圖4之橫截面圖顯示具有一高濃度1111及一低濃度 處理液饋入組件1112之一反應單元110之實施例構造。處理 液饋入組件1111可對反應單元1110饋入較高濃度的處理液， 而組件1112則用以饋入較低濃度之處理液。如同前述，此種 設計可令較高濃度的處理液得以行經較長的流路，有機會充份 形成亂流，以與反應劑供應組件1114所供應的反應劑達成最 大程度的化學反應。圖4中之反應單元設計可使本發明之系統 有能力適應處理液的，由低濃度到高濃度的較大濃度變動範 {J 圍。 圖5之橫截面圖顯示具有多層連結反應單元ιιια ιΐ2α… 及1130之反應器核心組件1101之實施例構造。此反應器核心 組件1101係由多個與圖4所示者相似之反應單元所串接組 17 1280951 成。圖5中之反應器核心組件1101之處理能量，實質上係為 其每一個單位反應單元之處理能量的總和。由於主迴流饋注段 1400所饋注的迴流液係為整體處理液流的主要流量部份，因 此每一反應單元内的流速，雖依上下游位置而有所不同，但其 差異不大。其間之流速差異，事實上有助於反應晶粒在整個反 應區1100A内的充份移動，有助於晶粒之形成。 圖6顯示依據本發明較佳實施例之一流體化床製程水溶液 處理系統。圖中大致以參考標號1000標示之製程水溶液處理 系統包含有一個流體化床反應器FBR 1001。圖中未顯現的某 種工業製程設施，做為製程水溶液之來源，對此反應器1001 饋入處理液。 FBR 1001係連結至一個配管網路1500上，透過數個混接 配管的混合器(mixer) 1562及1564等，整個系統1000的操作 係利用數個控制閥來進行控制調節。如同後面所將說明的，此 些控制閥可以依附於動力泵161G 162G 1631及1632等之上 泵的發動即同時開啟其所依附之閥，泵的關斷則同時將閥關 閉。 圖6所顯示本發明流體化床製程水溶液處理系統之實施例 之中，1610係裝設於處理液供應配管系1510上，泵1620係 裝設於反應劑供應配管系1520上，而泵1631及1632則係裝 設於回流水配管系1530上，分別通過混合器1562及1564而 18 1280951Installed in the tank body 1102 at appropriate intervals along the direction of the treatment liquid flow in the reaction unit 1110. In the embodiment of Fig. 3, the treatment liquid feed modules 1111, 1112, ..., and 1113 are installed. The reaction unit m〇 is upstream from the bottom to the upper flow, and the reactant supply modules 1114 and 1115 are relatively installed downstream. The two components within reaction unit 1110 can be arranged within tank 1102 in any suitable intervening or grouped manner. The main consideration of the arrangement is that the treatment liquid and the reactants sprayed from the nozzles can achieve maximum turbulence, so that the two flow can be charged in the large flow reflux of the main return feed section 1400 of the FBR system. Mix and mix to achieve the maximum chemical reaction. For example, the cross-sectional view of Figure 4 shows an embodiment configuration having a high concentration 1111 and a low concentration processing fluid feedthrough assembly 1112. The treatment fluid feed assembly 1111 can feed a higher concentration of treatment fluid to the reaction unit 1110, and the assembly 1112 can be used to feed a lower concentration of treatment fluid. As previously mentioned, this design allows a higher concentration of treatment fluid to pass through the longer flow path, providing the opportunity to fully create turbulent flow to achieve the maximum degree of chemical reaction with the reactants supplied by the reactant supply assembly 1114. The reaction unit design of Figure 4 allows the system of the present invention to be adapted to the processing fluids from a low concentration to a high concentration. Figure 5 is a cross-sectional view showing an embodiment configuration of a reactor core assembly 1101 having a plurality of layers of reaction units ιιια ι 2α... and 1130. The reactor core assembly 1101 is composed of a plurality of reaction units 17 1280951 which are similar to those shown in Fig. 4. The process energy of reactor core assembly 1101 in Figure 5 is essentially the sum of the process energy of each unit of reaction unit. Since the reflux liquid fed by the main reflux feed section 1400 is the main flow rate of the overall treatment liquid flow, the flow rate in each reaction unit varies depending on the upstream and downstream positions, but the difference is not large. The difference in flow rate between them actually contributes to the sufficient movement of the reaction grains in the entire reaction zone 1100A, contributing to the formation of crystal grains. Figure 6 shows a fluidized bed process aqueous solution processing system in accordance with a preferred embodiment of the present invention. The process aqueous treatment system, generally designated by the reference numeral 1000, contains a fluidized bed reactor FBR 1001. An industrial process facility not shown in the figure is used as a source of the process aqueous solution, and the reactor 1001 is fed with a treatment liquid. The FBR 1001 is coupled to a piping network 1500, through a plurality of mixing mixers 1562 and 1564, etc., and the operation of the entire system 1000 is controlled by a plurality of control valves. As will be explained later, these control valves can be attached to the power pump 161G 162G 1631 and 1632, etc., and the pump can be opened simultaneously, and the valve can be closed at the same time. In the embodiment of the fluidized bed process aqueous solution processing system of the present invention, the 1610 is installed in the treatment liquid supply piping system 1510, and the pump 1620 is installed on the reactant supply piping system 1520, and the pump 1631 and 1632 is installed on the return water piping system 1530, respectively through the mixers 1562 and 1564 and 18 1280951
對處理液供應配管系1510内的原始處理液及主迴流饋注段 1400的供水進行稀釋調節。 在圖6之議統之中，如同前述，混合器1564可用以在必要 時供應調節反應所需之氣液及劑等。例如，透過混合器1564, 用以殺菌或將低總有機碳(TOC, total organic content)量之臭氧 可以進入主迴流之中。此外，混合器1562則容許系統之主處 理液在進入FBR 1001之前，得以先行調節其濃度。 圖7顯示依據本發明較佳實施例，以流體化床為基礎，並 以即時控制系統應用回收水進行處理之一製程水溶液處理系 統之流路圖。如圖所示，系統1〇〇〇包含有一反應控制器1700, 利用分別配置於每一動力泵1610, 1620, 1631及1632等之處 的感應器1610S，1620S，1631S及1632S而分別收集各對應 配管1510, 1520, 1531及1532上的水質資料。所有收集到的 感應器資料係透過控制感應配線電路1701而傳回反應控制器 1700。反應控制器1700根據預先設定之反應設計條件，便可 以利用此些資料進行計算。依據計算結果，反應控制器Π00 便可以透過控制配線1702而分別利用各動力泵1610, 1620, 1631 及 1632 上的控制器 1610C，1620C, 1631C 及 1632C, 而分別控制各動力泵，以進行啟動或關斷的控制。在典型的實 施例之中，各動力栗1610，1620，1631及1632可以是利用變 頻馬達區動的泵，利用變頻控制，動力泵的泵動流量即得以精 19 1280951The raw treatment liquid in the treatment liquid supply piping system 1510 and the water supply of the main return feed section 1400 are diluted and adjusted. In the discussion of Fig. 6, as in the foregoing, the mixer 1564 can be used to supply the gas, liquid, and the like required for the adjustment reaction as necessary. For example, through the mixer 1564, ozone for sterilizing or reducing the total organic content (TOC) can enter the main reflux. In addition, the mixer 1562 allows the main process fluid of the system to adjust its concentration prior to entering the FBR 1001. Figure 7 is a flow diagram showing a process aqueous solution processing system based on a fluidized bed and using recycled water in an immediate control system in accordance with a preferred embodiment of the present invention. As shown in the figure, the system 1A includes a reaction controller 1700, and respectively collects corresponding signals by sensors 1610S, 1620S, 1631S and 1632S respectively disposed at each of the power pumps 1610, 1620, 1631 and 1632. Water quality data on piping 1510, 1520, 1531 and 1532. All collected sensor data is transmitted back to the reaction controller 1700 via the control sensing wiring circuit 1701. The reaction controller 1700 can perform calculations using such data based on pre-set reaction design conditions. According to the calculation result, the reaction controller Π00 can separately control each power pump through the control wiring 1702 by using the controllers 1610C, 1620C, 1631C and 1632C on the respective power pumps 1610, 1620, 1631 and 1632 for starting or Shutdown control. In a typical embodiment, each of the power pumps 1610, 1620, 1631, and 1632 can be a pump that uses a variable frequency motor to operate. With variable frequency control, the pumping flow of the power pump can be refined. 19 1280951
確控制。當泵速為零，泵停機時，即實質等於關斷了流路上的 閥。 本發明之流體化床製程水溶液處理系統，其操作方法之基 本原理，如同前述，係以系統之中各個關鍵位置所裝設之各種 相關流量，濃度，及酸鹼度等監測感應儀器收集各個操控資 訊。利用收集到的資訊，即可以應用預定之數學模式進行分析 計算，並根據分析計算結果，利用裝設於系統中之對應節點上 的各種泵，閥與/或混合器等流量控制元件，進行處理液及反 應劑/液的流量，濃度及酸鹼度等的調節，以進行即時的反應 最佳化控制。本發明系統此種操控方法之結果，便可以達成整 體系統的最佳化操作狀態。當然，隨著操作目的之不同，系統 最佳化的目標可能是最少用水量，最少用劑量，或最大反應結 晶速率，甚或其中的數個參數的最佳組合。例如，以後面所將 說明描述之系統為例，在半導體元件製造廠的情況之中，系統 所追求的最佳化可能是最少的用水量。 圖8之流程圖即顯示依據：φ:發明一較佳實施例，用於處理 諸如半導體，液晶顯示板(LCD，liquid crystal display)，以及鋼 鐵廠等製程設施所排放之含氟廢水之一處理系統2000之處理 流程。在此應用例之中，本發明類如圖7中之系統可以做為工 廠2800含氟製程排液之處理系統的核心1000。此工廠2800 典型地可為，例如，排出高、中、低濃度的含氟廢液，分別收 20 1280951Do control. When the pump speed is zero, when the pump is stopped, it is essentially equal to shutting off the valve on the flow path. The basic principle of the operation method of the fluidized bed process aqueous solution processing system of the present invention, as described above, collects various control information by monitoring various inductive instruments such as various related flow rates, concentrations, and pHs installed at various key positions in the system. Using the collected information, the predetermined mathematical model can be applied for analysis and calculation, and according to the analysis and calculation results, various pumps, valves and/or mixers, etc., installed at corresponding nodes in the system are used for processing. The flow rate, concentration and pH of the liquid and the reagent/liquid are adjusted to perform immediate reaction optimization control. As a result of this control method of the system of the present invention, an optimized operating state of the overall system can be achieved. Of course, depending on the purpose of the operation, the goal of system optimization may be the least amount of water, the minimum dose, or the maximum reaction crystallization rate, or even the optimal combination of several of these parameters. For example, in the case of the system described later, in the case of a semiconductor component manufacturer, the optimization sought by the system may be the least amount of water. Figure 8 is a flow chart showing the basis of: φ: a preferred embodiment of the invention for processing one of the fluorine-containing waste water discharged from a process facility such as a semiconductor, a liquid crystal display (LCD), and a steel plant. Process flow of system 2000. Among the application examples, the system of the present invention as shown in Fig. 7 can be used as the core 1000 of the processing system for the 2800 fluorine-containing process liquid discharge. This plant 2800 can typically be, for example, discharged high, medium and low concentrations of fluorine-containing waste liquid, respectively, 20 1280951
集於高、中及低濃度含氟廢水儲槽2802, 2803及2804之中。 此些不同濃度的含氟廢水在控制之下先於pH值調節槽2515 内進行pH值的調控，之後再進入調勻槽2510内充份混合調 勻。調勻後的處理液便可作為本發明系統1000的原料處理 液，依前述方法進行處理。 另一方面，本發明之流體化床反應系統用於廢液除氟之用 途時所須使用之典型反應劑，即選定濃度之氯化鈣(CaCl2)溶 劑，可由氯化鈣濃度調節槽2520供應。調節濃度後之氯化鈣 溶液可以直接供應給本發明之系統1000。氯化鈣濃度調節槽 2520内的氯化鈣溶液則可利用工廠的回收水儲槽2801,適當 地混合由氯化鈣原料儲槽2525所供應的反應劑原料，以調製 所需濃度的氯化鈣溶劑供本發明之系統1000處理所用。 例如，圖9顯示依據本發明較佳實施例，以流體化床為基 礎，用於處理諸如圖8中之工廠含氟廢水之一處理系統。圖9 中之系統3000係與圖7中之系統1000相似同樣運用了以微 電腦控制系統為荸礎的反應控制器1700,以便進行即時控制， 使系統之處理隨時維持在最佳反應條件之下，達成系統操作之 最佳化。 在本發明之流體化床製程水溶液處理系統應用於含氟製程 排液之氟化鈣結晶除氟應用用途之一較佳實施例之中，系統的 典型FBR係具有0.6~3m的内徑，4~8m的高度，其中之含氟 21 1280951It is concentrated in high, medium and low concentration fluorine-containing wastewater storage tanks 2802, 2803 and 2804. The fluorine-containing wastewater of different concentrations is controlled under the control of the pH adjusting tank 2515, and then mixed into the mixing tank 2510 to be thoroughly mixed and adjusted. The homogenized treatment liquid can be treated as a raw material treatment liquid of the system 1000 of the present invention by the above method. On the other hand, the fluidized bed reaction system of the present invention is used for the use of a waste liquid for the purpose of fluorine removal, that is, a typical concentration of calcium chloride (CaCl 2 ) solvent, which can be supplied by the calcium chloride concentration adjusting tank 2520. . The calcium chloride solution after adjusting the concentration can be supplied directly to the system 1000 of the present invention. The calcium chloride solution in the calcium chloride concentration adjusting tank 2520 can utilize the recycled water storage tank 2801 of the factory to appropriately mix the reactant raw materials supplied from the calcium chloride raw material storage tank 2525 to prepare a desired concentration of chlorination. The calcium solvent is used in the treatment of the system 1000 of the present invention. For example, Figure 9 shows a treatment system for treating a fluorine-containing wastewater such as the plant of Figure 8 based on a fluidized bed in accordance with a preferred embodiment of the present invention. The System 3000 in Figure 9 is similar to the System 1000 in Figure 7 in that a reaction controller 1700 based on a microcomputer control system is used for immediate control so that the processing of the system is maintained under optimal reaction conditions at all times. Achieve the optimization of system operation. In the preferred embodiment of the fluidized bed process aqueous solution treatment system of the present invention applied to the fluorine fluoride crystal fluoride defluoridation application of the fluorine-containing process liquid discharge, the typical FBR system of the system has an inner diameter of 0.6 to 3 m, 4 ~8m height, of which fluorine 21 1280951
處理液的原液濃度約在0.8〜2kg/hi>m2之間，其在FBR反應區 内的流速係控制在30〜120m/hr的範圍，且系統中的Ca/F莫耳 比(mole ratio)約在 0.6〜2.0。 雖然本發明已配合圖式以較佳賨施例揭示如上，然其並非 用以限定本發明。例如，本發明之說明雖然以含氟廢水為例進 行詳細說明,但本發明之流體化床製程水溶液處理系統及其方 法，如同可以理解的，同樣亦可適用於其他諸如含重金屬或有 機物製程排液或廢液之處理。例如，雖然含氟離子及重金屬離 子的處理液之處理其最佳化控制須包含反應段中流速的精確 控制以例固形結晶反應物之懸浮，但有含有機物處理液之處理 則可令其氣態反應tl由反應器之處理液液面直接消散出來。因 此，任何熟習此技藝者，在不脫離本發明之精神和範圍之情況 下，當可進行此類更動與變化，因此本發明之保護範圍當以後 附之申請專利範圍所界定者為準。 【圖式簡單說明】 本發明之其他目的、特徵及優點將配合所附圖式，利用較 佳但非限定本明範疇之實施例進行詳細說明。圖式之中： 圖1之透視圖顯示依據本發明一較佳實施例之製程水溶液 處理系統，其流體化床反應器之構造； 圖2顯示本發明較佳實施例之製程水溶液處理系統，其流 體化床反應器内外之液流系統； 22 1280951 圖3之橫截面圖顯示本發明製程水溶液處理系統其流體化 # 床反應器之反應單元之一較佳實施例構造； 圖4之橫截面圖顯示具有一高濃度及一低濃度處理液饋入 組件之一反應單元之實施例構造； . 圖5之橫截面圖顯示具有多層連結反應單元之反應器核心 組件之實施例構造r * 圖6顯示依據本發明較佳實施例之一流體化床製程水溶液 φ 處理系統； 圖7顯示依據本發明較佳實施例，以流體化床為基礎，並 以即時控制系統應用回收水進行處理之一製程水溶液處理系 統之流路圖； • 圖8為一流程圖，其中顯示依據本發明一較佳實施例，用 _ 於處理工廠製程設施所排放之含氟廢水之一處理系統之處理 流程；與 圖9顯示依據本發明較佳實施例，以流體化床為基礎，用 於處理含氟廢水之一處理系統。 【主要元件符號說明】 ^ 1000, 2000, 3000 • 1001The stock solution has a stock solution concentration of about 0.8 to 2 kg/hi>m2, and the flow rate in the FBR reaction zone is controlled in the range of 30 to 120 m/hr, and the Ca/F mole ratio in the system is About 0.6~2.0. The present invention has been described above in terms of preferred embodiments, which are not intended to limit the invention. For example, although the description of the present invention is described in detail by taking fluorine-containing wastewater as an example, the fluidized bed process aqueous solution treatment system and method of the present invention, as can be understood, can also be applied to other processes such as heavy metal or organic processes. Treatment of liquid or waste liquid. For example, although the optimization of the treatment of the treatment liquid containing fluorine ions and heavy metal ions must include precise control of the flow rate in the reaction section to exemplify the suspension of the solid crystalline reactant, the treatment with the organic treatment liquid can make it gaseous. The reaction tl is directly dissipated from the liquid level of the treatment liquid of the reactor. Therefore, those skilled in the art will be able to make such changes and modifications without departing from the spirit and scope of the invention, and the scope of the invention is defined by the scope of the appended claims. BRIEF DESCRIPTION OF THE DRAWINGS Other objects, features and advantages of the present invention will be described in detail in conjunction with the appended claims. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a perspective view showing a configuration of a fluidized bed reactor in accordance with a preferred embodiment of the present invention; FIG. 2 shows a process aqueous solution processing system according to a preferred embodiment of the present invention. Fluid flow system inside and outside a fluidized bed reactor; 22 1280951 FIG. 3 is a cross-sectional view showing a preferred embodiment of a reaction unit of a fluidized #bed reactor of the aqueous solution processing system of the present invention; An embodiment configuration showing a reaction unit having a high concentration and a low concentration treatment liquid feedthrough assembly; Figure 5 is a cross-sectional view showing an embodiment of a reactor core assembly having a plurality of coupled reaction units. A fluidized bed process aqueous solution φ treatment system according to a preferred embodiment of the present invention; FIG. 7 shows a process aqueous solution based on a fluidized bed and using an instant control system for the treatment of recycled water in accordance with a preferred embodiment of the present invention; Flow diagram of the processing system; • Figure 8 is a flow chart showing the processing of a factory process facility in accordance with a preferred embodiment of the present invention Process for treating one of the discharged fluorine-containing wastewater treatment systems; and Figure 9 shows a treatment system for treating fluorine-containing wastewater based on a fluidized bed in accordance with a preferred embodiment of the present invention. [Main component symbol description] ^ 1000, 2000, 3000 • 1001
1100, 1100A 1101 Φ 1102 流體化床製程水溶液處理系統 FBR，流體化床反應器 反應段，反應區 反應器核心組件 反應器核心組件槽體 23 12809511100, 1100A 1101 Φ 1102 Fluidized bed process aqueous solution treatment system FBR, fluidized bed reactor Reaction section, reaction zone Reactor core components Reactor core component tank 23 1280951
1105 反應器底板 1108 迴流液分配噴嘴 1109 反應產物排放管 1110, 1120, 1130 反應單元 1111， 1112, 1113 處理液饋入組件 1111N，1112N，1113N 處理液分配噴嘴 1111T, 1112T, 1113T 處理液供應管格 1114, 1115 反應劑供應組件 1114N，1115N 反應劑分配噴嘴 1114T，1115T 反應劑分配管格 1116, 1117, 1118 處理液饋入控制閥(高，中，低濃度) 1119 反應劑供應控制閥 1121，1122, 1131，1132 處理液饋入組件 1125, 1135 反應劑供應組件 1200, 1200A 反應穩定段，反應穩定 1300, 1300A 緩衝段，緩衝區 1400,1400A 主迴流饋注段，迴流分配區 1411 逆止閥 1421 污泥排放管 1500 配管網路，配管系統 1510 處理液供應配管系 1511 處理液供應管 1520 反應劑供應配管系 24 1280951 15211105 Reactor bottom plate 1108 Recirculation dispensing nozzle 1109 Reaction product discharge pipe 1110, 1120, 1130 Reaction unit 1111, 1112, 1113 Treatment liquid feed assembly 1111N, 1112N, 1113N Treatment liquid distribution nozzle 1111T, 1112T, 1113T Treatment liquid supply pipe 1114, 1115 Reagent supply unit 1114N, 1115N Reagent distribution nozzle 1114T, 1115T Reagent distribution tube 1116, 1117, 1118 Treatment fluid feed control valve (high, medium, low concentration) 1119 Reagent supply control valve 1121, 1122 , 1131, 1132 treatment fluid feed assembly 1125, 1135 reactant supply assembly 1200, 1200A reaction stabilization section, reaction stability 1300, 1300A buffer section, buffer 1400, 1400A main return feed section, return distribution zone 1411 check valve 1421 Sludge discharge pipe 1500 piping network, piping system 1510 treatment liquid supply piping system 1511 treatment liquid supply pipe 1520 reactant supply piping system 24 1280951 1521
反應劑供應管 回流水配管系 主迴流供應管 調節液供應管 放流水配管系 (配管)混合器 泵 1530 1531 1532 1540 1562,1564 1610, 1620,1631，1632 1700 反應控制器Reagent supply pipe Return water piping main reflux supply pipe Regulating fluid supply pipe Discharge water piping system (pipe) mixer Pump 1530 1531 1532 1540 1562, 1564 1610, 1620, 1631, 1632 1700 Reaction controller
1701 感應配線電路 1702 控制配線電路1701 Inductive Wiring Circuit 1702 Control Wiring Circuit
2525
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| TW92112800A TWI280951B (en) | 2003-05-12 | 2003-05-12 | Fluidized-bed process drain treatment system |
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| TW92112800A TWI280951B (en) | 2003-05-12 | 2003-05-12 | Fluidized-bed process drain treatment system |
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| TWI280951B true TWI280951B (en) | 2007-05-11 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9650266B2 (en) | 2014-10-14 | 2017-05-16 | Institute Of Nuclear Energy Research, Atomic Energy Council, Executive Yuan | Method of treating suspended solids and heavy metal ions in sewage |
| US11773028B2 (en) | 2019-12-20 | 2023-10-03 | Industrial Technology Research Institute | Composite material and method of removing fluoride ion in waste liquid |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108794291B (en) | 2017-04-27 | 2020-11-27 | 中国科学院大连化学物理研究所 | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and toluene |
| CN108786672B (en) | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by using methanol and/or dimethyl ether and benzene |
| CN108786670B (en) | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and toluene |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9650266B2 (en) | 2014-10-14 | 2017-05-16 | Institute Of Nuclear Energy Research, Atomic Energy Council, Executive Yuan | Method of treating suspended solids and heavy metal ions in sewage |
| US11773028B2 (en) | 2019-12-20 | 2023-10-03 | Industrial Technology Research Institute | Composite material and method of removing fluoride ion in waste liquid |
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