MODEL RESEARCH BASED ON LIQUID/SOLID TWO PHANSE FLOWS IN METALLURGY STIRRED TUBULAR REACTOR

Μέγεθος: px

Εμφάνιση ξεκινά από τη σελίδα:

Download "MODEL RESEARCH BASED ON LIQUID/SOLID TWO PHANSE FLOWS IN METALLURGY STIRRED TUBULAR REACTOR"

Δορκάς Σπυρόπουλος
6 χρόνια πριν
Προβολές:

1 Ø 46 Ø 8 Vol.46 No µ Ø Ú ACTA METALLURGICA SINICA Aug pp ÆÙ ± /» Ã Á Â À (ß ¼ Ö ², Ò ËÀ ËÚ Ð, ÇÓ ) ÅÊ Å ÑÆ«º, Î Æ«ß/ ÑÐÕ Ê, ¾ Õ Å º Ñ µ µô, Ñ Á±Í. Á Ð, ßÆ«Ã È, ÑÏ, ±³Í¼ÑÐÛº, ¼Æ«150 r/min, Ñ Ð 1.58 m/s; Æ«150 È 250 r/min, Ê, Ô (25 r/min) È (50 r/min) ³Ì Ê; ¼ Å 2% È 7.5%, 5 È 8 r/min. ß,, Æ«, Å Đ TG249 ¹ºÜ A ¹ Û (2010) MODEL RESEARCH BASED ON LIQUID/SOLID TWO PHANSE FLOWS IN METALLURGY STIRRED TUBULAR REACTOR ZHAO Qiuyue, ZHANG Ting an, CAO Xiaochang, LIU Yan, JIANG Xiaoli Key Laboratory of Ecological Utilization of Multi metal Intergrown Ores of Ministry of Education, School of Materials and Metallurgy, Northeastern University, Shenyang Correspondent:ZHANG Ting an, professor, Tel: (024) , zta2000@16.net Supported by Research Fund for the Doctoral Program of Higher Education (No ) and Science and Technology Talents Fund for Excellent Youth of Liaoning Province (No ) Manuscript received , in revised form ABSTRACT The computational fluid dynamics (CFD) method was used to research the velocity and concentration fields in the multiphase flow tubular stirred reactor. A mathematical model of liquid/solid two phase flow was established and the simulated results obtained by using this model are in better agreement with the experimental ones. The results show that the maximum velocity of solid liquid phase flow is 1.58 m/s when the rotation speed is 150 r/min and there is no flow dead zone in the tubular stirred reactor because that turbulent flow is strengthened by the stirring action. Radial mixture is better when the rotation speeds are 150 and 250 r/min than when the rotation speeds are 25 and 50 r/min, a proper rotation speed is need to obtain the prefered mixture. The critical impeller speeds are 5 and 8 r/min when the solid concentration are 2% and 7.5%, respectively. KEY WORDS metallurgy, tubular reactor, stir, simulation ³ÆÅ, À Al Ð Õ Al 2 O Í ÉÙÓØ. ½ Al 2 O Í Ã É, ÃÅ Ì, Â½ É ÂÕ «, Ç, ÉÁ Í Ã Ð ²Î [1]. ³, [2] Ë Å Í Ð * ¹ ÒÁ² Û È Ï Ø ½ Â : , : Ô :,, 1978 Ì, Å, ² DOI: /SP.J ÃÆ, Æ T ËÜ Ð«Ò Æ. ½ Ð Æ / Ò Å º, ÒÝ Ä ÆÐÒ«, È ÆÐ, ÃÈ Û ½Ò«É, Ò«± Ò«º. «Ê, ÆË Æ / Ò Ð Ë ÕÉ»Á ÌÕ. Æ Ð ËÃ Ã Æ Á ÐÏ Ë É Á Ð Ë 2».» [,4], Ï ËÃ Å ÆÎ Õ, Ë Ð Å, «Ê, ½» Á Ð Ë Ð Õ

t (φ iρ i ) + (φ i ρ i u i ) = 0 (1) t (φ lρ l u l ) + (φ l ρ l u l )u l = φ l p + τ l + È φ l ρ l g + K sl ( u s u l ) (2) t (φ sρ s u s ) + (φ s ρ s u s ) u s = φ s p p s + τ s + φ s ρ s g + K sl (

2 Ø 8 µµñ : Ö Å Þ/ ÐĐ ¹ 1005»Ï Á Ð Ë. ² [5 8] Ð» Â, É ËÃ ÐÆ ĐÎ½ ºÐ Õ, Ë ĐÐ Ò Â, Â º. «Ê, Õ Æ Ò Õ Ë ²ÎÖ. Khopkar Ó [9] Ã ½ Õ «««½ÐÜ, Yamazaki Ó [10] Ù Ï «Ò Â² Î, Ö «/ Æ Ï ËÃ.» É Ð Ü Æ ²Î, ²ÄÕÐÆË Æ / ÒÐ»ÀÂ. Õ½» [11] Ð Å, ÆË Æ É ¹ Î ÐÉ¼ ( ¾ºÐ Ç Õ Ë Ó) ²ÎÖ, ± Ò Â Õ,» Æ Ð ¾Ò É¼ÉÒ., ½ Ð Æ Ò Õ ËÂ ÂÐÕ, ²Ð µ³æë Æ ÌÕ. 1 ²¾ ¼ ² Eulerian Eulerian ÜÐ Ò«Ë [12], Ï Ô Æ / ÒÐ Å. «ÚÐ Ð É. t (φ iρ i ) + (φ i ρ i u i ) = 0 (1) t (φ lρ l u l ) + (φ l ρ l u l )u l = φ l p + τ l + È φ l ρ l g + K sl ( u s u l ) (2) t (φ sρ s u s ) + (φ s ρ s u s ) u s = φ s p p s + τ s + φ s ρ s g + K sl ( u l u s ) () Ü. ½³ ËÉ, Ð ÆÊ ÇÐ Æ, Õ Ò«Ê Ð«Æ, Ó Ò«ĐÐ Đ, ²Ò«ÆÙ Ä. «Ê, ³ Ë½ Ò / ÒÐÖ «É Å ÐÆ. Ò«ËÐ Ü, ½ Ü Â Ð Á, ²Õ ÐÅ: (1) Æ, Î Ð Đ, Ò É Å«2 ÊÒ«; (2) 2 ÊÒ«Ò ¼ Ð Å ; () Ò«Ó Ò ; (4) Ð Æ Ð Ðµ «; (5) É Ò«. 2 Ú Å² «ÄÐÆË Æ, É Ü T Ë, Ü Đ Åß 90 ½ Ï, 16 Ü. Ü ÐÕ, ½Ì² Æ ËÐ»,. Æ Ð ÌÕÁÏ 1. Ü ¹½Ð ¾É Ö : Ü 1 10 kg/m, Pa s, Ò 1.8 m /h; Ü kg/m, 0.1 mm, «Ò Ö 2% É 7.5%; Ð 25, 50, 150, 250 É 50 r/min. Í FLUENT ÆÐ ÆÊ Gambit Ï Ë±Í Ø, ½ «Ì ½, Æ» É»,» Ö ½, ³» Ò«Đ Ü ;» µ Ö ½. ± º,» Õ» Ý ß«Ð º, «Â 2( ½ Ð Ðº ) [12]. ÏÉ Þ, ÇË ß (Wall); Æ (Inlet) Æ Ò ; Ã Æ (Outlet) Ã ; Þ µ ß. Í CFD FLUENT 6. Ð «Ò Å È, ³» Ò Ü ÐÆÊ ß É, φ i «Ò Ö; ρ i Ü, kg/m ; u i Ð, m/s; τ i Æ, Pa s; i l É s, É ; p, Pa; K sl «Ö; t Đ, s; g Ì Ð, m/s 2. Eulerian Ë Ö «ĐÐ, ¹ ÕÕ Ð Ð Ò¹, Ü ÐÅ / Đ Æ ÉÙ, É Ð, É, ĐÐ Õ Ã É Õ ½ ÐÝ ÅÜ. Ò«ËÐ Ü Ô «ĐÐ Õ Á. ³ Ë ¾ß Ó Æ É ÐÄ, ± ÐÐÆ ÆÊ ÉÒ«, ² Ë 1 Fig.1 Structure chart of a new tubular reactor (unit: mm) 2 Õ Å ¹ Fig.2 Schematic of grids used for simulating the tubular stirred reactor

$m a 1006 M r. > jy1 r l x ~_ Wen Yu S, _ T 4 >1 (MRF) M N R x l _^ /, n n~ z n~, FM GlQ{B } fyts l SIMPLE ~, P E. b, B l5< k [ : 10.$ . a A = K, Q B b Æ, n N : nb, n~ Dk }J, RZ-N l Y B. b A = K, NS `L l B b Æ, l q, n ~G 6, fs#d, #`b> Qu. N SB b Æ ( b) 8 Æ ( c) l }?

$4 ^} 150 r/min Z CFD lwd {Q,DQP {l}?. A, </ ^>n >}? ( 4a) `>n > }? ( 4b) 1-fG>', S} [HM=, ^>niilm[} 1.58 m/s, " E `>n l 1.46 m/s I+.$

3 m a 1006 M r. > jy1 r l x ~_ Wen Yu S, _ T 4 >1 (MRF) M N R x l _^ /, n n~ z n~, FM GlQ{B } fyts l SIMPLE ~, P E. b, B l5< k [ : 10. t 46 7 [1] ( 8) 1 ^} # 4 Q 50 r/min l 5, Æ l Reynolds r :1 10 G, N 2 nb..1 } d K b&gn_ 1.8 m /h 5, ^ } 150 r/min Z, ( lq B b Æ QNSB b Æ, q 8 Æ l >}?. a A = K, Q B b Æ, n N : nb, n~ Dk }J, RZ-N l Y B. b A = K, NS `L l B b Æ, l q, n ~G 6, fs#d, #`b> Qu. N SB b Æ ( b) 8 Æ ( c) l }?>z, v~nsbb Æ ($ jb 8 Æ fsl x, & NSBb Æ k x:, * 1 W G, R, l :,Xq 8 Æ, =gns Bb Æ C N. S} [HG =, ( CYln } ~7+ u lq B b Æ ln n}, n}l + quzn~ Dl `A #`n~ NC lq7 QNKG. 4 ^} 150 r/min Z CFD lwd {Q,DQP {l}?. A, </ ^>n >}? ( 4a) `>n > }? ( 4b) 1-fG>', S} [HM=, ^>niilm[} 1.58 m/s, " E `>n l 1.46 m/s I+. R, n S x K 25, 50, 150, ' $ [14], r/min, P Aa MR\Æ Aa pæ 7 k > [14] Fig. Velocity fields in the traditional tubular reactor (150 r/min, 1.8 m /h flow) (a), the tubular stirred reactor (150 r/min, 1.8 m /h flow) (b) and tank stirred reactor (9 r/min)[14] (c) Y CFD k =m _=mkvc zp+cpo zk > Fig.4 Flow fields of liquid phase at axial (left) and vertical (right) section in two phases flow (a) and single phase flow (b) simulated by CFD at 150 r/min

4 Ø 8 µµñ : Ö Å Þ/ ÐĐ ¹ 1007 Ã, ½ Æ ÆÐÐ Đ Ü ÄÐ, Ð, «Ï²³Ò«ÐÐ, ½ ²³Æ ĐÃ, ±½ÐÞ Å ¹Æ½ Ð Ó, Ë Ð»Õ ÆË Æ Å Ð..2 ÐÞ 5 «2% Ð«½½ Ð Æ ÉĐ Ä Ð «Ò Ö., Ð 25 r/min, Ð À, º, ÏÉÈ» Î½; Ð 50 r/min, Öº Ü, ÉÈÆ Ä ; Ð 150 É 250 r/min, Æ Þ, ² Ù ³, Ê Æ»,, Ô ¼ «, ÉÈ Â; Ð 50 r/min, Æ ÐÝ Ö Î, ³» Æ½ Ü ²³, Ê ½ Ï» ÎÂ, Ð Í ÐÈÈ, Ò«½» Ã Ò ÐÇ, / Ð Ë Í. «ÊÆ ¾ Ð Ð ÄÈÈ Æ ËÐ±ß r/min Ð Æ Ï ß «Ò Â [12] Ð. Ã, Ä, Æ Ò«½Ï ÀÉ Æ ÒÐ Ü, ³ Ü ÆË Æ ÎÀ,» Æ Ü», ÒÂÕ. Æ Ë, Ú ½ÊÃ É ÌÕÕ. «Ð Ò Ð ÛÄ ³Ë, Æ Ð, ½ Ã³Ï ÐÐ ËÐ, Ð ß, ÒÉ Æ Ý, «ÐÎ½Ì² Æ ÆÐ Ë, ½ «É, Ù» «, ÂÖ «Ë ÕÐ Volume fraction Rotation speed 25 r/min 50 r/min 150 r/min 250 r/min 50 r/min Distance, m 5 ³ Æ«È Ã ÅÑ Õ ( Å 2%) Fig.5 Radial solid phase volume fraction at different rotation speeds in the middle of the tubular stirred reactor (solid concentration 2%) Đ Ò.. ½ ³ ÆË Æ ½ / «½ Ð, Ð²Î. 7 «Ü Ð Ð Ñ ««Ò ÖÐ¼. Ã, Ñ «Ò ÖÀ 0.52, «2% «½ Ð Ð½ 5 r/min Ó, «7.5% «½ Ð Ð½ 8 r/min Ó, Ð 5 É 8 r/min, Æ Æ ¾. Ð½ 50 r/min, Æ Ð «Ñ «Ò Ö Î¹, ½ «ÀÐ «2% «½, Î, Ú Ê, ÂÂ Þ, «ÈÈ Õ, º Ð Ò«Ü Ý ÆÀ Ò, «Õ, ÊÈÈ ÐÕ ½. «Ê, ÐÐ ¾Õ, 5 ÐÜ Â. 6 ³ Æ«µ Ô Ñ Á [12] Fig.6 Simulated (left) and tracer experimental [12] (right) f max concentration distributions at different times (rotation speed 150 r/min) (5, 0.52) (8, 0.52) Solid concentration 2% 7.5% Rotation speed, r/min 7 ³ Ð ÅÑ Õ Fig.7 Curves of maximum solid volume fraction (f max) vs rotation speed

5 1008 Ñ Ø 46» Â, ÆË Æ É Æ Ò É Æ ÐÄ Ð Ü, Ð Ë ÉÆÉ ÂÐ. 4 (1) ÆËØ «Ò Æ», Ï Æ Ð / Ò Ö Ë, Ö «Ð» Æ Ò ÐÐ Õ Ð, É Ð Ò Â ³Ë Æ. (2) ÄÐ Æ É Æ Ò ² Î½Ò Ü», ½ Ð 150 r/min, Ò ÐÑ Ð 1.58 m/s. () Ð 150 É 250 r/min, Ë, ½ «2% É 7.5%, Ð 5 É 8 r/min. Õ Ð (25 r/min) É Ð (50 r/min) Í Ë. Ý ¹º [1] Yuan H J, Huang F, Li Q Q, Xiang Y, Yuan Y. J Guizhou Ind Univ, 2002; 1: 16 (,, Ë³³, Ô,. Í¾Û. 2002; 1: 16) [2] Zhang T A, Zhao Q Y, Dou Z H, Liu Y, He J C. China Pat, ZL , 2005 (,, ĐÀÌ, , 2005), ÍÚ. È Ì, ZL [] Baldyga J, Pohorecki R. Chem Eng, 1995; 58: 18 [4] Kasat G R, Khopkar A R, Ranade V V, Pandit A B. Chem Eng Sci, 2008; 6: 877 [5] Kraume M. Chem Eng Technol, 1992; 15: 1 [6] Harrop K L, Spanfelner W H, Jahoda M, Otomo N, Etchells A W, Bujalski W, Nienow A W. Récents Progrés génie procédés, 1997; 52: 41 [7] Bujalski W, Takenaka K, Paolini S, Jahoda M, Paglianti A, Takahashi K, Nienow A W, Etchells A W. Chem Eng Res Des, 1999; 77: 241 [8] Michelletti M, Nikiforaki L, Lee K C, Yianneskis M. Ind Eng Chem Res, 200; 42: 626 [9] Khopkar A R, Kasat G R, Pandit A B, Ranade V V. Ind Eng Chem Res, 2006; 45: 4416 [10] Yamazaki H, Tojo K, Miyanami K. Powder Technol, 1986; 48: 205 [11] Zhao Q Y. PhD Thesis, Northeastern University, Shenyang, 2008 (. ² ±. ÈÔ, 2008) [12] Drew D A. Ann Rew Fluid Meth, 198; 15: 261 [1] Wen C Y, Yu Y H. Chem Eng Prog Symp Ser, 1966; 62: 100 [14] Chen T, Wu D Z, Du H X, Wang L Q, Li Z F. J Eng Thermophs, 2010; 1: 271 (,,, Æ³, ËÀ. ¾ É, 2010; 1: 271)

Σχετικά έγγραφα

ACTA MATHEMATICAE APPLICATAE SINICA Nov., ( µ ) ( (

35 Þ 6 Ð Å Vol. 35 No. 6 2012 11 ACTA MATHEMATICAE APPLICATAE SINICA Nov., 2012 È ÄÎ Ç ÓÑ ( µ 266590) (E-mail: jgzhu980@yahoo.com.cn) Ð ( Æ (Í ), µ 266555) (E-mail: bbhao981@yahoo.com.cn) Þ» ½ α- Ð Æ Ä