TW476661B - Impeller draft tube agitation for gas-liquid mixing using stirred tank reactor - Google Patents
Impeller draft tube agitation for gas-liquid mixing using stirred tank reactor Download PDFInfo
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- TW476661B TW476661B TW089126249A TW89126249A TW476661B TW 476661 B TW476661 B TW 476661B TW 089126249 A TW089126249 A TW 089126249A TW 89126249 A TW89126249 A TW 89126249A TW 476661 B TW476661 B TW 476661B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/20—Stationary reactors having moving elements inside in the form of helices, e.g. screw reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2334—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements provided with stationary guiding means surrounding at least partially the stirrer
- B01F23/23341—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements provided with stationary guiding means surrounding at least partially the stirrer with tubes surrounding the stirrer
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/86—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis co-operating with deflectors or baffles fixed to the receptacle
- B01F27/861—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis co-operating with deflectors or baffles fixed to the receptacle the baffles being of cylindrical shape, e.g. a mixing chamber surrounding the stirrer, the baffle being displaced axially to form an interior mixing chamber
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/91—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with propellers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
- B01J19/1875—Stationary reactors having moving elements inside resulting in a loop-type movement internally, i.e. the mixture circulating inside the vessel such that the upwards stream is separated physically from the downwards stream(s)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/15—Stirrers with tubes for guiding the material
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Mixers Of The Rotary Stirring Type (AREA)
Abstract
Description
476661 經濟部智慧財產局員工消費合作社印製 A7 ____-__B7___ 五、發明說明(1 ) 本發明係有關於一種於攪拌槽反應器中進行氣-液反 應之授動糸統的改良設计。特別地,本發明係關於《包括 一導流管、一或多個軸向葉輪和一或多個徑向葉輪的系統 。該新穎之攪動設計,提供了在該反應器内之液相和氣相 之間的改良接觸。 授拌槽反應器(STRs)在化學製程中,例如,發酵作用 、氫化作用、光氣化作用、中和作用、氣化作用和有機氧 化作用,係非常普及,在該攪拌槽反應器中,氣相和液相 緊密接觸以便質量傳遞。該STR的設計,在氣泡分散、界 面面積(“a”)、氣泡表面瞬態(bubble surface transience)和 質量傳遞係數“KL”上,具有重要的影響。該STR的設計, 亦對以一特定速率運轉該葉輪系統所需之功率(the power) ,具有影響力。 在習知技術中已發表過,許多不同之混合系統嘗試並 達成在該氣相和液相之間的最大質量傳遞。這些包括美國 專利第 4,231,974號、第 5,108,662號、第 5,371,283號、第 5,451,349號、第 5,523,474號、第 5,536,875號和第 5,696,285 號。這些習知之混合實驗可被改進,因為它們既沒有最佳 質量傳遞係數,亦無法使該功率需求減至最小。 本發明包括一導流管連同轴向葉輪和徑向葉輪兩者。 該(等)軸向葉輪係設置在由該導流管所形成之該圓筒的内 部’而該(等)徑向葉輪係設置在由該導流管所形成之該圓 筒的下面。此種系統之流體流和質量傳遞特性,乃優於習 知之攪動系統。 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) (請先閱讀背面之注意事項再填寫本頁) 訂--------線!476661 Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs A7 ____-__ B7___ V. Description of the Invention (1) The present invention relates to an improved design of a system for energizing gas-liquid reactions in a stirred tank reactor. In particular, the invention relates to a system comprising a draft tube, one or more axial impellers and one or more radial impellers. The novel agitation design provides improved contact between the liquid and gas phases within the reactor. Stirred tank reactors (STRs) are very popular in chemical processes such as fermentation, hydrogenation, phosgenation, neutralization, gasification and organic oxidation. In this stirred tank reactor, The gas and liquid phases are in close contact for mass transfer. The design of this STR has important effects on bubble dispersion, interface area ("a"), bubble surface transients, and mass transfer coefficient "KL". The design of the STR also has an impact on the power required to run the impeller system at a specific rate. It has been published in the art that many different mixing systems attempt and achieve maximum mass transfer between the gas and liquid phases. These include U.S. Patent Nos. 4,231,974, 5,108,662, 5,371,283, 5,451,349, 5,523,474, 5,536,875, and 5,696,285. These conventional hybrid experiments can be improved because they neither have the best mass transfer coefficient nor can they minimize this power requirement. The invention includes a deflector along with both axial and radial impellers. The (or) axial impeller train is disposed inside the cylinder formed by the deflector tube, and the (or) radial impeller train is disposed below the cylinder formed by the deflector tube. The fluid flow and mass transfer characteristics of such a system are superior to those of a conventional agitation system. This paper size applies to China National Standard (CNS) A4 (210 X 297 mm) (Please read the precautions on the back before filling this page) Order -------- Line!
I 4 476661I 4 476661
五、發明說明(2 ) 經濟部智慧財產局員工消費合作社印製V. Description of the invention (2) Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs
本發明另外的優點和特徵,將可從閱讀本發明之詳細 說明並參照以下的圖式而明顯可知。 圖式簡單說明 第1圖,係於對應於本發明之一裝置的橫戴面圖。 第2圖,係一在具有一導流管之系統中,三種不同攪 動速率之經觀測KLa對氣體流速的圖表。 第3圖’係一在不具有一導流管之系統中,三種不同 授動速率之經觀測KLa對氣體流速的圖表。 如在第1圖中所見,本發明包括一傳動軸1;附著於該 傳動轴1之至少一軸向葉輪2,以通常平行於該傳動軸丨丨的 方向來移動流體;附著於該傳動軸1之至少一徑向葉輪3, 以通常垂直於該傳動轴11的方向來移動流體;以及一導流 管4,形狀為一通常開放型圓筒。如在第1圓中清楚所示, 當該攪動系統5置放在一攪拌槽反應器1〇内,該傳動軸1延 伸經過該導流管4,且該一或多個轴向葉輪2係設置在該導 流管圓筒4内,且該一或多個徑向葉輪3係設置在該導流管 圓筒4之外部。 具有該攪動系統5之該攪拌槽反應器1〇必須以一直立 形式來設置,如在第1圖中所呈現者,使得該等徑向葉輪3 設置在該導流管4的下面。同樣地,如在第1圖中所示,該 導流管4的入口,較佳表傾斜偏離該傳動軸1,但這並非必 須如此不可。 當該傳動轴1繞著其轴11轉動時,該等轴向葉輪2乃以 通常平行於該傳動軸11的方向作動,將該反應器内容物向 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) . 11!11! - I _ I II I ! f請先閱讀背面之注意事項再填寫本頁) A7Further advantages and features of the present invention will be apparent from reading the detailed description of the present invention and referring to the following drawings. Brief Description of the Drawings Fig. 1 is a cross-sectional view of a device corresponding to the present invention. Figure 2 is a graph of the observed KLa versus gas flow rate for three different agitation rates in a system with a draft tube. Fig. 3 'is a graph of the observed KLa versus gas flow rate for three different actuation rates in a system without a diversion tube. As seen in FIG. 1, the present invention includes a transmission shaft 1; at least one axial impeller 2 attached to the transmission shaft 1 to move fluid in a direction generally parallel to the transmission shaft; and attached to the transmission shaft At least one radial impeller 3 of 1 moves the fluid in a direction generally perpendicular to the transmission shaft 11; and a deflector 4, which is a generally open cylinder. As clearly shown in the first circle, when the agitation system 5 is placed in a stirred tank reactor 10, the transmission shaft 1 extends through the flow guide tube 4, and the one or more axial impellers 2 are It is disposed in the duct tube 4, and the one or more radial impellers 3 are disposed outside the duct tube 4. The agitating tank reactor 10 having the agitating system 5 must be arranged in an upright form, as shown in FIG. 1, so that the radial impellers 3 are disposed below the guide tube 4. Similarly, as shown in Fig. 1, the inlet of the deflector 4 is preferably tilted away from the drive shaft 1, but this is not necessary. When the transmission shaft 1 rotates around its shaft 11, the axial impellers 2 are moved in a direction generally parallel to the transmission shaft 11 to apply the Chinese National Standard (CNS) A4 to the paper contents Specifications (210 X 297 mm). 11! 11!-I _ I II I! F Please read the notes on the back before filling this page) A7
五、發明說明(3 ) (請先閱讀背面之注意事項再填寫本頁) 下移動經過該導流管4。軸向葉輪係該技藝中所普遍已知 的且任何此種葉輪可用在本發明中。舉例而言,一雙螺 旋葉輪,例如美國專利第5,1〇8,662號所述者,或一翼型 葉片葉輪,例如美國專利第4,231,974號所述者,可用在 本發明中。其他適合之轴向葉輪,包括斜漿渦輪、高效率 葉輪(例如 Lightnin Mixing Co·之 A-310型號、Chemineer,V. Description of the invention (3) (Please read the notes on the back before filling in this page) and move through the guide tube 4. Axial impeller trains are generally known in the art and any such impeller can be used in the present invention. For example, a double spiral impeller, such as described in U.S. Patent No. 5,108,662, or an airfoil blade impeller, such as described in U.S. Patent No. 4,231,974, may be used in the present invention. Other suitable axial impellers include oblique blade turbines, high-efficiency impellers (such as the A-310 model of Lightnin Mixing Co., Chemineer,
Inc.之 HE-3 以及 ΕΚΑΤΟ Rueher 和 Mischtechnik GmbH 之Inc. HE-3 and ΕΚΑΤΟ Rueher and Mischtechnik GmbH
VlSC〇pr〇P)、單一螺旋或船用螺旋槳(例如Lightnin MixingVlSC〇pr〇P), single screw or marine propeller (such as Lightnin Mixing
Co·之 A-315 或 A-320、Chemineer,Inc.之 MT-4 或 MY-4)。 通常軸向葉輪的使用數目,係視該工作介質的黏度而定。 該工作介質愈黏,愈要更多的軸向葉輪。預期本發明可包 括1至數個軸向葉輪2,但較佳是兩個。 經濟部智慧財產局員工消費合作社印製 同時’當該傳動軸1繞著其軸π轉動時,該等徑向葉 輪3作動,以移動該反應器内容物遠離該傳動軸1和(當該 等徑向葉輪3設置在該導流管4下面時)向該導流管4之外面 。該(等)徑向葉輪之中心線必須在該導流管之端下面夠遠 處’以避免實質的干擾。通常此係在從該徑向葉輪直徑距 離之約1/8至該徑向葉輪直徑距離之約7/8的範圍内,在約 2/3是最佳的。徑向葉輪亦通常為習知技術所已知,且任 何設計可用於本發明中。一般適用於本發明之徑向葉輪包 括扁平葉片葉輪、羅斯通葉輪(Rushton lmpeliers)、凹盤 式渴輪(Smith 渦輪)SCABA(SRGT)葉輪和 Chemineer,Inc. 之BT-6型號。所使用之最適宜的徑向葉輪數目係視該液 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) 6Co. A-315 or A-320, Chemineer, Inc. MT-4 or MY-4). Usually the number of axial impellers depends on the viscosity of the working medium. The more viscous the working medium, the more axial impellers are required. It is contemplated that the present invention may include one to several axial impellers 2, but preferably two. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs at the same time when the transmission shaft 1 rotates around its axis π, the radial impellers 3 act to move the reactor contents away from the transmission shaft 1 and When the radial impeller 3 is disposed below the guide tube 4, the radial impeller 3 faces the outer surface of the guide tube 4. The centerline of the (etc.) radial impeller must be far enough below the end of the guide tube to avoid substantial interference. Usually this is in the range from about 1/8 of the radial impeller diameter distance to about 7/8 of the radial impeller diameter distance, and is preferably about 2/3. Radial impellers are also generally known in the art, and any design can be used in the present invention. Radial impellers generally suitable for the present invention include flat blade impellers, Rushton lmpeliers, SCABA (SRGT) impellers, and BT-6 models of Chemineer, Inc. The optimum number of radial impellers used depends on the liquid. The paper size is in accordance with China National Standard (CNS) A4 (210 X 297 mm) 6
發明說明( 經濟部智慧財產局員工消費合作社印製Description of the Invention (Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs
體南度與該槽直徑的比率而定。在大部份的情形下,單一 徑向葉輪將會在本發明中使用,但在一些反應器中,例如 高發酵槽,可使用多數徑向葉輪。 導流管和它們的變型亦是習知技術所廣知,且那些教 示文獻通常可應用至本發明。舉例而言,該導流管可被切 槽以提供液體回到該導流管的中心,如果該液面因某個原 因沒有超過該導流管的頂部。又,可有利地運用將直立導 流葉片使用在該導流管之内表面來改變切向流動的方向至 軸向流動。如果在該導流管中使用導流葉片,較佳是導流 葉片具有該導流管内直徑〇·8至01的寬度和該導流管内直 徑0.016至0.021的間隙。而且,將導流葉片使用在部份地 靠近由該導流管所形成之圓筒底部,係特別見於美國專利 第5,536,875號且亦可使用在本發明中。 雖然該導流管4的尺寸對本發明並不重要,已發現該 導流管的最佳半徑係該槽半徑的〇·7〇7。使用此半徑的導 流管使得在該導流管内部的該槽之橫截面面積相等於在該 導流管外部的該槽之橫截面面積。如在第1圖中所見,該 導流管4可選擇地含有一錐形漏斗式部份6,在該導流管的 入口端。咸信此部份將有助於導正該反應器内容物的流動 。該斜面角必須在30和60度之間,在45度為最佳。該斜邊 須不能太長,如此會限制圍繞該導流管頂部的流動。如果 該斜邊的長度是從〇至約該導流管内直徑之1/4為較佳,在 約1/12的長度為最佳。本發明可用於任何尺寸的攪拌槽反 應器。可使用附在該反應器壁之側結構支架來將該導流管 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公« ) I ^--------^» — — — — 1 — I 1^ (請先閱讀背面之注意事項再填寫本頁) 476661 A7 五、發明說明( 固持在適當的位置,如習知技術中所已知。又沿著該反應 器壁,可選擇地使用導流葉片,如習知技術中所通知。如 果使用導流葉片,較佳是彼此分開間隔約9〇。的四個導流 葉片。可藉由任何習知技術中已知之裝置來將該反應氣體 帶進該槽。這些包括環狀喷霧器和較佳管狀或喷嘴喷霧器 經濟部智慧財產局員工消费合作社印製 必須了解本發明結構的特定細節,例如材料、尺寸等 並不視為本發明的限制。反而,這些細節可依需求來調整 ,以產生用於任何特殊應用的較佳實施態樣。 本發明的效果可在以下的實施例中見到: 實施例 使用一瞬變技術來測定該質量傳遞係數。此動態放氣 技術由以純氮來喷射該反應器直到所有氧氣已從該工作介 質被解吸所成。之後該喷射氣體快速地從氮氣變成氧氣。 然後測量該瞬變氧氣濃度。之後可使用這些測量值來計算 該系統之體積質量傳遞係數(KLa)。如此之物理技術可應 用至一均勻混合系統和至小值之KLa,因溶解之氧氣探測 氣的緩慢感應時間。通常這些物理技術可應用在KLa <1/ r,其中τ:係該溶解之氧氣探測氣的感應時間。 使用一具有〇.45m内直徑(0.08m3)之ASME盤形底部 plexiglastm槽來進行該氣-液混合實驗。使用四個間隔 分開90°的扁平導流葉片來促進轴向混合。該攪動系統包 括兩個高效率向下泵送轴向葉輪(Lightnin Mixing Ltd.之 A-310型號)和一個徑向氣體分散Rushton圓盤渦輪 (請先閲讀背面之注意事項再填寫本頁) 訂--------線| _ -1· «I ^1 ^1 ϋ ·1 ϋ I n mmM9 ft— a—- 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公* ) 476661 A7 B7 五、發明說明(6 ) (Lightnin R-100)。透過設置在該徑向葉輪下之一環狀噴 霧器來噴射該氣體。使用去離子水作為該工作介質。該攪 動器速度和轉矩各藉由一接近流速計和測力計來測量,而 溶解於水中之氧漢度,以兩個氧氣感測器(電傳感DO探針 對95%飽和具有2秒之感應時間)。該攪動程度(充氣功率 (gassed power)為 0.26-2.6 watt/kg)足以產生一0.012-0.046 m/s(即1-5 VVM)表面氣體速度的均勻氣體分散。使用一 CAMILEtm 2000資料探測系統來收集所有的資料。首先測 定沒有一導流管之系統在不同氣體流動速率和傳動軸速度 (功率)之KLa。以非線性回歸(例如在統計套裝軟體中已知 為 JMP,由 SAS Institute,Cary,North Carolina,U.S.A.所有) 來使用標題為”在清潔水中之氧傳遞的測量”之ANSI/ASCE Standard 2-91,以測定在該質量傳遞係數KLa(l/sec)和表 面氣體速度Vsg(m/sec)之間的相互關係。這些結果示於第 1表中並圖解說明在第2圖中。 — — — — — — — — — — — — — ^ ·1111111 ^« — — — — — 1 — (請先閱讀背面之注意事項再填寫本頁) 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) 9 476661 Α7 Β7 五、發明說明(7 ) 經濟部智慧財產局員工消費合作社印製 第1表 沒有該導流管之質量傳遞係數 速度 N[rpm] 氣體流動速率 Q[scfm] 每質量功率 ε [w/kg] 表面氣體速度 Vsg[m/s] 質量傳遞係數 KLa[l/sec] 300 4 2.66 0.0122 0.063 300 6 2.30 0.0182 0.070 300 9 2.14 0.0274 0.077 300 12 2.21 0.0365 0.081 250 4 1.66 0.0122 0.057 250 6 1.55 0.0182 0.058 250 9 1.49 0.0274 0.068 250 12 1.52 0.0365 0.072 250 15 1.49 0.0456 0.074 200 4 1.06 0.0122 0.043 200 6 1.02 0.0182 0.046 200 9 0.95 0.0274 0.053 200 12 0.96 0.0365 0.064 200 15 0.94 0.0456 0.067 然後將具有内直徑0.3m之導流管(以達成在該導流管 内和圍繞該導流管之環形區域之大約相同的表面氣體速度) 放置在該混合系統内。再測定在不同氣體流動速率和傳動 轴速度(功率)之Κρ。具有該導流管之結果示於第2表中並 圖解說明在第3圖中。 ’ 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) JH0--------訂-!!!線,*------------------ (請先閱讀背面之注意事項再填寫本頁) 10 476661 A7 _B7_ 五、發明說明(8 ) 第2表The ratio of body southness to the diameter of the groove is determined. In most cases, a single radial impeller will be used in the present invention, but in some reactors, such as high fermentation tanks, most radial impellers can be used. Diversion tubes and their variations are also widely known in the art, and those teachings are generally applicable to the present invention. For example, the draft tube can be slotted to provide liquid back to the center of the draft tube if the liquid level does not exceed the top of the draft tube for some reason. In addition, it is advantageous to use an upright guide vane on the inner surface of the guide pipe to change the direction of the tangential flow to the axial flow. If a guide vane is used in the guide pipe, it is preferable that the guide vane has a width of the inner diameter of the guide pipe of 0.8 to 01 and a gap of the inner diameter of the guide pipe of 0.016 to 0.021. Moreover, the use of the deflector blades near the bottom of the cylinder formed by the deflector is particularly seen in U.S. Patent No. 5,536,875 and can also be used in the present invention. Although the size of the diversion tube 4 is not important to the present invention, it has been found that the optimal radius of the diversion tube is 0.707 of the groove radius. The use of a guide tube of this radius allows the cross-sectional area of the groove inside the guide tube to be equal to the cross-sectional area of the groove outside the guide tube. As can be seen in Figure 1, the guide tube 4 optionally contains a conical funnel section 6 at the inlet end of the guide tube. It is believed that this part will help direct the flow of the reactor contents. The bevel angle must be between 30 and 60 degrees, with 45 degrees being optimal. The hypotenuse must not be too long, as this restricts the flow around the top of the duct. It is preferred if the length of the hypotenuse is from 0 to about 1/4 of the inner diameter of the diversion tube, and a length of about 1/12 is most preferred. The invention can be used in stirred tank reactors of any size. A structural support attached to the side of the reactor wall can be used to adapt the guide tube to the paper size of China National Standard (CNS) A4 (210 X 297 male «) I ^ -------- ^» — — — — 1 — I 1 ^ (Please read the notes on the back before filling out this page) 476661 A7 V. Description of the invention (held in place, as known in the conventional technology. Along the wall of the reactor Alternatively, guide vanes may be used, as notified in the conventional technique. If guide vanes are used, four guide vanes spaced apart from each other by about 90 ° are preferred. Any known technique may be used. Devices to bring the reactive gas into the tank. These include ring sprayers and preferably tubular or nozzle sprayers. Printed by the Consumer Property Cooperative of the Intellectual Property Bureau of the Ministry of Economics. Specific details of the structure of the invention, such as materials, dimensions Etc. are not to be considered as a limitation of the present invention. Instead, these details can be adjusted as required to produce a preferred embodiment for any particular application. The effects of the present invention can be seen in the following examples: Example Use a transient technique to measure The mass transfer coefficient. This dynamic outgassing technique consists of injecting the reactor with pure nitrogen until all oxygen has been desorbed from the working medium. After that, the injected gas quickly changes from nitrogen to oxygen. The transient oxygen concentration is then measured. These measurements can then be used to calculate the volume mass transfer coefficient (KLa) of the system. Such physical techniques can be applied to a homogeneous mixing system and KLa to small values due to the slow induction time of the dissolved oxygen probe gas. Usually these Physical technology can be applied to KLa < 1 / r, where τ: is the induction time of the dissolved oxygen detection gas. An ASME disc bottom plexiglastm groove with an inner diameter of 0.045m (0.08m3) is used to perform the gas- Liquid mixing experiment. Four flat guide vanes spaced 90 ° apart are used to promote axial mixing. The agitation system includes two high-efficiency downward pumping axial impellers (Model A-310 of Lightnin Mixing Ltd.) and one Radial Gas Dispersion Rushton Disc Turbine (Please read the precautions on the back before filling this page) Order -------- Line | _ -1 · «I ^ 1 ^ 1 ϋ · 1 ϋ I n mmM9 ft — A—- The paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 male *) 476661 A7 B7 V. Description of the invention (6) (Lightnin R-100). Sprayed through a ring-shaped sprayer set under the radial impeller The gas. Deionized water was used as the working medium. The speed and torque of the agitator were measured by a proximity flow meter and a dynamometer, respectively, and the degree of oxygen dissolved in the water was measured by two oxygen sensors ( The electric sensing DO probe has a sensing time of 2 seconds for 95% saturation. The degree of agitation (gassed power is 0.26-2.6 watt / kg) is sufficient to produce a 0.012-0.046 m / s (that is, 1-5 VVM ) Uniform gas dispersion at surface gas velocity. A CAMILEtm 2000 data detection system was used to collect all data. First determine the KLa of a system without a duct at different gas flow rates and drive shaft speeds (power). Use ANSI / ASCE Standard 2-91 titled "Measurement of Oxygen Transfer in Clean Water" with non-linear regression (known as JMP in the statistical suite software, owned by SAS Institute, Cary, North Carolina, USA) In order to determine the correlation between the mass transfer coefficient KLa (l / sec) and the surface gas velocity Vsg (m / sec). These results are shown in Table 1 and illustrated graphically in Figure 2. — — — — — — — — — — — — — — ^ · 1111111 ^ «— — — — — 1 — (Please read the notes on the back before filling out this page) Printed on paper by Employees’ Cooperatives, Intellectual Property Bureau, Ministry of Economic Affairs Standards are applicable to China National Standard (CNS) A4 specifications (210 X 297 mm) 9 476661 Α7 Β7 V. Description of the invention (7) Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, Table 1. There is no mass transfer coefficient for the diversion tube Speed N [rpm] Gas flow rate Q [scfm] Power per mass ε [w / kg] Surface gas velocity Vsg [m / s] Mass transfer coefficient KLa [l / sec] 300 4 2.66 0.0122 0.063 300 6 2.30 0.0182 0.070 300 9 2.14 0.0274 0.077 300 12 2.21 0.0365 0.081 250 4 1.66 0.0122 0.057 250 6 1.55 0.0182 0.058 250 9 1.49 0.0274 0.068 250 12 1.52 0.0365 0.072 250 15 1.49 0.0456 0.074 200 4 1.06 0.0122 0.043 200 6 1.02 0.0182 0.046 200 9 0.95 0.0274 0.053 200 12 0.96 0.0365 0.064 200 15 0.94 0.0456 0.067 Then a diversion tube with an inner diameter of 0.3m (to achieve the annular area within and around the diversion tube Of about the same superficial gas velocity) disposed within the mixing system. Then measure κρ at different gas flow rates and drive shaft speed (power). The results with this diversion tube are shown in Table 2 and illustrated in Figure 3. '' This paper size applies to China National Standard (CNS) A4 (210 X 297 mm) JH0 -------- Order-!!! line, * ------------- ----- (Please read the precautions on the back before filling this page) 10 476661 A7 _B7_ V. Description of Invention (8) Table 2
N[rpm] Qfscfm] 300 4 300 6 300 9 300 12 300 15 250 4 250 6 250 9 250 12 250 15 200 4 200 6 200 9 200 12 200 15 具有該導流管之質量傳遞係數 速度氣體流動速率每質量功率表面氣體速度質量傳遞係數 ε [w/kg] Vsg[m/s] KLa[l/sec] 2.21 0.0121 0.075 1.85 0.0182 0.081 1.53 0.0273 0.094 1.50 0.0365 0.099 1.45 0.0456 0.099 1.28 0.0121 0.062 1.08 0.0182 0.069 0.90 0.0273 0.075 0.85 0.0365 0.083 0.88 0.0456 0.092 0.70 0.0121 0.045 0.65 0.0182 0.051 0.61 0.0274 0.059 0.60 0.0365 0.063 0.52 0.0456 0.069 — — — — — — — — — — — — — i — — — — — — ^ ·1111111 (請先閱讀背面之注意事項再填寫本頁) 經濟部智慧財產局員工消費合作社印製N [rpm] Qfscfm] 300 4 300 6 300 9 300 12 300 15 250 4 250 6 250 9 250 12 250 15 200 4 200 6 200 9 200 12 200 15 With the mass transfer coefficient speed of the guide tube gas flow rate per Mass power Surface gas velocity Mass transfer coefficient ε [w / kg] Vsg [m / s] KLa [l / sec] 2.21 0.0121 0.075 1.85 0.0182 0.081 1.53 0.0273 0.094 1.50 0.0365 0.099 1.45 0.0456 0.099 1.28 0.0121 0.062 1.08 0.0182 0.069 0.90 0.0273 0.075 0.85 0.0365 0.083 0.88 0.0456 0.092 0.70 0.0121 0.045 0.65 0.0182 0.051 0.61 0.0274 0.059 0.60 0.0365 0.063 0.52 0.0456 0.069 — — — — — — — — — — — — — — — — — — — ^ · 1111111 (Please read the first Please fill in this page for attention) Printed by the Consumer Cooperative of Intellectual Property Bureau of the Ministry of Economic Affairs
從這些結果可見,該導流管之存在,增加該KLa超過 一未有導流管之習知系統的KLa,增加該氣體滯留量並降 低該相同馬達速度所抽運之功率。 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) 11 476661 A7 _B7_ 五、發明說明(9 ) 元件標號對照 1…傳動轴 2…軸向葉輪 3…徑向葉輪 4…導流管 6…錐形漏斗式部份 10…攪拌槽反應器 11…轴 (請先閱讀背面之注意事項再填窵本頁) 經濟部智慧財產局員工消費合作社印製 V V· i aamm 1 ϋ ϋ >1·· I I ϋ ϋ ϋ ϋ -I I ϋ I ϋ >1 ϋ ϋ ϋ ϋ ϋ ϋ ^1 ϋ ϋ ϋ ϋ· ϋ ϋ . 本紙張尺度適用中國國家標準(CNS)A4規格(210 X 297公釐) 12From these results, it can be seen that the presence of the deflector increases the KLa beyond the KLa of a conventional system without a deflector, increases the gas holdup and reduces the power pumped by the same motor speed. This paper size is in accordance with Chinese National Standard (CNS) A4 (210 X 297 mm) 11 476661 A7 _B7_ V. Description of the invention (9) Component number comparison 1 ... drive shaft 2 ... axial impeller 3 ... radial impeller 4 ... guide Flow tube 6 ... Tapered funnel part 10 ... Stirred tank reactor 11 ... Shaft (Please read the precautions on the back before filling this page) Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs 1 i ϋ > 1 ·· II ϋ ϋ ϋ II -II ϋ I ϋ > 1 ϋ ϋ ϋ ϋ ϋ ϋ ^ 1 ϋ ϋ ϋ ϋ · ϋ ϋ. This paper size applies to China National Standard (CNS) A4 (210 X 297) Mm) 12
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EP2437874B1 (en) | 2009-06-05 | 2015-05-06 | F.Hoffmann-La Roche Ag | Device for cultivating cells |
CN103261181A (en) | 2010-09-30 | 2013-08-21 | 索尔维公司 | Derivative of epichlorohydrin of natural origin |
CN102773048B (en) * | 2011-05-09 | 2017-06-06 | 波利玛利欧洲股份公司 | Produce the Ammoximation reaction device of cyclohexanone oxime |
FI124934B (en) * | 2013-01-30 | 2015-03-31 | Outotec Oyj | The mixing tank reactor |
KR20200078221A (en) * | 2018-12-21 | 2020-07-01 | 한화솔루션 주식회사 | Batch reactor |
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Publication number | Priority date | Publication date | Assignee | Title |
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DE1967739U (en) * | 1966-07-04 | 1967-09-07 | Process Engineering Co | DEVICE FOR THE PREPARATION OF FINE MIXING OF GASEOUS AND LIQUID MATERIALS. |
JPS5796006A (en) * | 1980-12-05 | 1982-06-15 | Mitsui Toatsu Chem Inc | Production of rubber-modified styrene resin |
SU1115791A1 (en) * | 1982-12-27 | 1984-09-30 | Предприятие П/Я А-1785 | Mixer-reactor |
DE3516027A1 (en) * | 1985-05-04 | 1986-11-06 | Huels Chemische Werke Ag | STIRRING SYSTEM AND METHOD FOR FASTENING LIQUIDS |
JPS6269976A (en) * | 1985-09-24 | 1987-03-31 | Kansai Kagaku Kikai Seisaku Kk | Removal of tartar and apparatus therefor |
SU1632493A1 (en) * | 1989-04-25 | 1991-03-07 | Предприятие П/Я Р-6956 | Chemical reactor |
CA2149058C (en) * | 1994-05-11 | 1998-07-28 | Jeffrey Paul Kingsley | Enhanced oxidation of organic chemicals |
SE505871C2 (en) * | 1996-01-12 | 1997-10-20 | Kvaerner Pulping Tech | Mixing device for mixing black liquor from cellulose production with ash from flue gases obtained by combustion of black liquor |
US5972661A (en) * | 1998-09-28 | 1999-10-26 | Penn State Research Foundation | Mixing systems |
-
2000
- 2000-11-30 WO PCT/US2000/032586 patent/WO2001041919A1/en active Application Filing
- 2000-11-30 AU AU19356/01A patent/AU1935601A/en not_active Abandoned
- 2000-12-08 TW TW089126249A patent/TW476661B/en not_active IP Right Cessation
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN111944663A (en) * | 2020-10-10 | 2020-11-17 | 漯河医学高等专科学校 | A fermentation cylinder for producing licorice fermentation beverage |
Also Published As
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AU1935601A (en) | 2001-06-18 |
WO2001041919A1 (en) | 2001-06-14 |
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