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WO2015080667A1 - Appareil de mélange - Google Patents

Appareil de mélange Download PDF

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Publication number
WO2015080667A1
WO2015080667A1 PCT/SG2014/000560 SG2014000560W WO2015080667A1 WO 2015080667 A1 WO2015080667 A1 WO 2015080667A1 SG 2014000560 W SG2014000560 W SG 2014000560W WO 2015080667 A1 WO2015080667 A1 WO 2015080667A1
Authority
WO
WIPO (PCT)
Prior art keywords
cone
mixing apparatus
reactor
mixing
shaft
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/SG2014/000560
Other languages
English (en)
Inventor
Wun Jern Ng
Antonius Yudi SENDJAJA
Youming TAN
Santosh PATHAK
Yan Zhou
Maszenan Bin ABDUL MAJID
Soon Keat TAN
Jian Lin Jerry LIU
Prannoy CHOWDHURY
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Nanyang Technological University
Sembcorp Industries Ltd
Original Assignee
Nanyang Technological University
Sembcorp Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Nanyang Technological University, Sembcorp Industries Ltd filed Critical Nanyang Technological University
Priority to CN201480065210.7A priority Critical patent/CN106061594B/zh
Priority to MYPI2016000995A priority patent/MY185698A/en
Publication of WO2015080667A1 publication Critical patent/WO2015080667A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • B01F23/50—Mixing liquids with solids
    • B01F23/53—Mixing liquids with solids using driven stirrers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F31/00—Mixers with shaking, oscillating, or vibrating mechanisms
    • B01F31/44—Mixers with shaking, oscillating, or vibrating mechanisms with stirrers performing an oscillatory, vibratory or shaking movement
    • B01F31/441—Mixers with shaking, oscillating, or vibrating mechanisms with stirrers performing an oscillatory, vibratory or shaking movement performing a rectilinear reciprocating movement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/30—Driving arrangements; Transmissions; Couplings; Brakes
    • B01F35/32—Driving arrangements
    • B01F35/325—Driving reciprocating or oscillating stirrers
    • 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
    • B01J19/0053—Details of the reactor
    • B01J19/0066—Stirrers

Definitions

  • This invention relates to a mixing apparatus, and in particular, a mixing apparatus for slurry-type fluid mixtures.
  • slurry-type fluid mixtures typically consist of a mixture of low-density water-type liquids and solid particles.
  • a potential problem in slurry mixing is that the solid components tend to accumulate at the bottom of the mixing vessel due to gravity.
  • One of the easiest and most common ways to achieve desirable mixing level inside the reactor is by using a mechanical mixer.
  • mechanical mixers There are several types of mechanical mixers which result in different mixing patterns, such as marine impellers, flat vertical blades, Rushton impellers, inclined blades, curved blades, and cage beaters.
  • mechanical mixers can be classified into radial impellers and axial impellers, which create patterns that encircle the rotational axis and along the line with the axis, respectively.
  • a draft tube which is a cylindrical housing around the impeller, can be used to improve mixing performance.
  • One of the drawbacks of the mechanical mixers described above is that they may create a vortex at the reactor surface. This problem usually occurs in low viscosity fluid mixing.
  • the vortex reduces the effective volume of the mixing tank which decreases operational efficiency, for example decreasing conversion in the stirred tank reactor.
  • the mixing tank is usually equipped with several vertical baffles near the tank's wall. These baffles disrupt mixing patterns and eliminate vortex formation in the reactor surface.
  • Other mixing strategies involve utilization of recirculation flow to create desirable mixing patterns inside the reactor. A compressed gas which enters from the bottom of the reactor is able to create upward mixing pattern to decrease grit accumulation. Another strategy utilizes recirculation of the fluid phase inside the reactor.
  • the present novel mixing apparatus utilizes longitudinal displacement of a mixing head in a mixing vessel or reactor, acting like a plunger as it moves up and down along the vertical axis of the reactor.
  • the mixing head is cone-shaped.
  • the cone-shaped mixing head creates a large turbulent area in the middle of reactor.
  • the cone-shaped mixing head leaves a cone-shaped trail on its way upwards and downwards.
  • the trail left by its upward and downward movements intersects in an area, which basically covers most of the reactor volume. It creates more turbulence in the corresponding "intersection" area which is beneficial for mixing.
  • the cone-shaped trail also promotes gas release where relevant. Installation of baffles for vortex prevention thus becomes unnecessary.
  • the displacement characteristic of the mixing apparatus which is oriented along the longitudinal axis of the tank, aims to alleviate the problem of solid accumulation problem.
  • the shape of the cone has more ability to break excessive flocculent material, which often occurs in slurry type fluid inside anaerobic reactors. While it is generally aimed at multiphase solid and liquid (with possibly gas bubbles included) mixing, it can also be used for single phase liquid mixing.
  • Utilization of linear motion mixing pattern as the main driving force allows a same level of mixing to be achieved by the mixing apparatus with less energy consumption when compared to mixing using mechanical impellers. Its downward and upward movements are driven by a pumpjack mechanism to facilitate further stroke length necessary to extend mixing area and volume inside the vessel. The downward movement creates more pressure near the wall, while upward movement builds pressure at the centre. In a gas producing vessel, such as an anaerobic reactor, the resulting pressure gradient has the potential to help with gas release from solution and thereafter gas-liquid separation.
  • the present invention has the potential to be used in various applications, in particular blending tank and stirred tank. Its cone-shaped head creates the potential to be used for multiphase solid-liquid system, such as anaerobic reaction of sludges and wastewater mixture. So far no such mixing head device has been developed for mixing applications.
  • a mixing apparatus for use in a reactor configured to contain a mixture, the mixing apparatus comprising: a vertically oriented shaft configured to be placed in the reactor; a cone-shaped mixer configured to be connected to a bottom end of the shaft within the reactor; and a rotary-to-linear motion converter mechanism configured to be connected to an upper part of the shaft and to create reciprocating vertical movement of the shaft and the cone-shaped mixer in the mixture.
  • the cone-shaped mixer may comprise an upper cone and a lower cone connected at their bases, their bases being identical.
  • the height of the upper cone may be smaller than the height of the lower cone.
  • the height of the upper cone may be 25% of the height of the lower cone.
  • the upper cone and the lower cone may be right circular cones.
  • Ratio of the height of the lower cone to the diameter of the base may be 0.5.
  • Ratio of the height of the upper cone to the diameter of the base may be 0.13.
  • Ratio of the diameter of the base to the diameter of the reactor may be 0.40.
  • the upper cone may have a rounded profile.
  • the upper cone may be a truncated cone and the bottom end of the shaft may be attached to the truncated top of the upper cone.
  • Ratio of the stroke length of the reciprocating vertical movement to the height of the reactor may be 0.8.
  • the mixture may comprise liquid and solid particles, and the conical tip at a lower part of the cone- shaped mixer may be configured for breaking agglomerated solid particles in the mixture.
  • the rotary-to-linear motion converter mechanism may comprise a pumpjack mechanism.
  • Fig. 1 is a schematic diagram of a mixing tank with an exemplary cone-shaped mixing apparatus of the present invention.
  • Fig. 2 is a schematic diagram of a pumpjack.
  • Fig. 3 is a simulation velocity contour inside the mixing tank.
  • Fig. 4 is a simulation solid phase volume fraction contour inside the mixing tank.
  • the mixing apparatus 10 comprises a vertically oriented shaft 20 configured to be placed in a reactor 60, a rotary-to-linear motion converter mechanism 30 connected to an upper part 21 of the shaft 20, and a cone-shaped mixing head or mixer 40 connected to another end 22 of the shaft 20 for immersion in a mixture in the reactor 60.
  • the mechanism 30 is driven by a rotary motor 1 10 which acts as the main driving force to create upward and downward movement of the shaft 20 and the cone-shaped mixing head 40 in the reactor 60.
  • the mechanism 30 is provided at a top 61 of the vessel 60 and converts rotational movement of the motor 110 into reciprocating vertical movement of the shaft 20.
  • the mechanism preferably comprises a pumpjack mechanism 30 as shown in Fig. 2.
  • a pumpjack mechanism 30 is preferred as the rotary- to-linear motion converter mechanism as it can provide a larger stroke length than other mechanisms, for example, the slotted link mechanism or the crank and slider mechanism.
  • the motor 1 10 of the pumpjack 30 runs a set of gears to drive a crank 120.
  • a pitman arm 130 connects the crank 120 to one end of a walking beam 140 which is free to move on a Samson post 150.
  • the crank 120 and pitman arm 130 raise and lower one end of the walking beam 140 to make a horse head 160 on the other end of the walking beam 140 move up and down correspondingly.
  • the shaft 20 connects the horse head 160 with the mixing head or mixer 40 at the bottom end 22 of the shaft 20.
  • the shaft 20 follows the movement of the horse head 160 as it lowers and rises to create a vertical stroke of the cone shaped mixer 40.
  • Stroke length is defined as the distance travelled by the mixing head 40 in each upward or downward movement. This translates to the potential of a larger height to diameter ratio of the vessel 60, which is desirable as it results in smaller requirement of space for tank installation.
  • Displacement of the shaft 20 is adjustable by varying the position of a pivot 170 of the walking beam 140.
  • the walking beam 140 is configured such that maximum displacement (i.e. the stroke) of the shaft 20 is achieved when the pivot 170 is shifted to the end of the walking beam 140 that is connected to the pitman arm 130 (shown as dotted lines in Fig. 2).
  • This configuration enables the shaft displacement to be optimized to achieve the desired mixing level for various applications.
  • the bottom end 22 of the shaft 20 is connected with the mixer 40, which has a cone or arrowhead form in the three and two dimensional space, respectively.
  • the mixer 40 is in the form of two cones, an upper cone 41 and a lower cone 42, that are connected at their bases that are identical.
  • the upper cone 41 is preferably a truncated cone such that the bottom end 22 of the shaft 20 is attached to the top 44 of the upper cone 41.
  • the upper and lower cones 41, 42 are in the form of right circular cones.
  • the mixer 40 is placed such that the conical tip 43 of the lower cone 42 is located at the lower part of the mixer 40 while the broader top 41 or the upper cone 41 is preferably rounded.
  • the cone or arrowhead shape reduces the drag force transferred from the liquid in the vessel 60 to the mixer 40 and thus reduces energy consumption. Due to its sharp edge or tip 43, the downward movement of the mixer 40 is effective at breaking up larger agglomerated solid particles in the vessel 60.
  • the cone-shaped mixing head 40 also reduces drag force in the reactor 60 as it has less contact area with the liquid which reduces energy requirement. As the head 40 moves downward, it leaves a cone- shape wake in the liquid that resembles the trail in the sea left when a ship passes by. The total reactor volume which experiences turbulence due to movement of the head 40 is thus maximized. Downward movement of the head 40 spreads the liquid tangentially while the liquid in the lower part 62 of the reactor 60 is pushed backward or upward such that turbulence is generated. Although the cone-shaped mixing head 40 has the potential to create a dead zone in the bottom-most part 63 of the reactor 60, such a dead zone is eliminated when the head 40 is pulled up during an upstroke of the shaft 20.
  • the cone-shaped mixing head 40 As the cone-shaped mixing head 40 is pulled up, it creates upward movement in the surrounding volume 50. As a result, it creates circular motion where the liquid adjacent to the shaft 20 is shifted upward and the surrounding liquid further away is shifted downward.
  • the cone-shaped mixing head 40 thus creates cone-shaped turbulence in its downward movement and full recirculation pattern in its upward movement. With a cone-shaped mixing head 40, the downward and upward movement creates a mixing pattern which ensures no velocity vector elimination and reduces risk of dead zones forming.
  • a computational fluid dynamics simulation to describe and compare the performance of the mixing apparatus 10 was carried out.
  • the simulation aimed to find the optimum dimensions of the cone 40, by investigating the mixing pattern when various shapes and dimensions of cone head 40 were used.
  • the computational fluid dynamic simulation was performed using FLUENT software, using unsteady state SST omega turbulence model.
  • the simulated vessel 60 had a height to diameter ratio of 1.8. It contained a slurry type liquid having a viscosity of 0.1 kg/m.s.
  • the mixer 40 formed a solid region inside the vessel 60, which moved up and down in a straight line. The movement was simulated using moving mesh algorithm. Tetrahedral meshing was utilized for both liquid and solid regions.
  • a 3m 3 anaerobic digestion vessel 60 was considered.
  • the diameter and height of the vessel 60 were 1.26m and 2.28m, respectively.
  • the tank 60 was filled with a slurry-type liquid, where the solid content was 15%.
  • the cone-shaped mixing head 40 was rigid, moving up and down in a straight line.
  • the liquid viscosity was 0.1 kg/m.s. Tetrahedral meshing was utilized for both liquid and solid regions.
  • the recommended mixer 40 diameter was 0.50m.
  • the heights of its upper and lower cones 41 , 42 were 0.07m and 0.25m, respectively.
  • the mixer 40 was moved at the velocity of 0.5m s and the stroke length was 1.5m. Thus, it took approximately 6 seconds for the mixer 40 to perform one complete cycle.
  • Fig. 3 and Fig. 4 show the simulation results on distribution of velocity magnitude and solid volume fraction inside the mixing tank 60, respectively.
  • the simulation was carried out for three cycles, i.e., three downward and upward movements. All tank walls 64 were assumed to be rigid and the reactor surface was set to be an interface.
  • the SST omega turbulence model was used in the simulation.
  • the contour analysis was carried out at the upper and lower turning point of the mixer, i.e. the highest 44 and lowest point 43 of the mixing head 40. Based on Fig. 3, the downward movement creates larger turbulence area compared to its upward movement, which may be caused by downward gravitational force. Further analysis on turbulence kinetic energy showed that the surface and the area surrounding the wall 64 have least turbulence compared to other areas in the mixing vessel 60, even though the velocity magnitude contour does not indicate any dead zone formed in the area.
  • the computational fluid dynamic simulation also indicates even distribution of solid particle throughout the mixing vessel 60 and the presence of laminar flow in the liquid surface.
  • the optimization in the dimension of the cone-shaped mixing head 40 revealed that it requires a smaller cone 41 at the upper part 41 as well.
  • the tiny upper cone 41 slightly decreases homogeneity during downward movement. Nevertheless, it significantly improves the homogeneity during its upward movement, such that it is a worthwhile trade-off.
  • the recommended height of the upper cone 41 is approximately 25% of the height of the lower cone 42. Further studies showed that increasing the height of the upper cone 41 further does not have any effect on increased homogeneity.
  • Increasing mixing condition inside the reactor 60 eliminates dead zone, the inactive area of the reactor. In addition, it improves homogeneity inside the reactor 60. Improvement in mixing condition and homogeneity may result in conversion increase. Given that linear motion mixing utilizes upward and downward motions, it has more potential to provide a more uniform condition compared to other mechanical mixers, in particular in the axial direction. Therefore, it can be expected to promote conversion increase by means of increasing homogeneity inside the reactor 60.
  • a potential implementation of the proposed mixing apparatus is in biochemical reactors for mixing of anaerobic digestion processes with their specific characteristics, such as the presence of solid particle and the requirement to release the biogas as the result of the anaerobic reactions, where the organism is used as the catalysts.
  • the microorganisms form the solid phase inside the reactor.
  • the presence of biomasses in the form of solid particles incurs additional challenges in mixing as these particles have to be distributed evenly to enable optimal exposure to the substrates and thus improving yield.
  • the mixing apparatus 10 is able to prevent formation of suspended biomass which decreases substrate conversion.
  • chemical reaction which includes solid phase catalysts may benefit from the mixing apparatus 10 as it ensures effective contact between catalyst and substrate inside catalytic reactors.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)

Abstract

L'invention concerne un appareil de mélange destiné à être utilisé dans un réacteur conçu pour contenir un mélange, l'appareil de mélange comprenant : une tige orientée verticalement, conçue pour être placée dans le réacteur ; un mélangeur en forme de cône conçu pour être relié à une extrémité inférieure de la tige dans le réacteur ; et un mécanisme de convertisseur de mouvement rotatif/linéaire conçu pour être relié à une partie supérieure de la tige et pour créer un mouvement vertical alternatif de la tige et du mélangeur en forme de cône dans le mélange.
PCT/SG2014/000560 2013-11-27 2014-11-27 Appareil de mélange Ceased WO2015080667A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN201480065210.7A CN106061594B (zh) 2013-11-27 2014-11-27 一种混合装置
MYPI2016000995A MY185698A (en) 2013-11-27 2014-11-27 A mixing apparatus

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US201361909536P 2013-11-27 2013-11-27
US61/909,536 2013-11-27

Publications (1)

Publication Number Publication Date
WO2015080667A1 true WO2015080667A1 (fr) 2015-06-04

Family

ID=53199470

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SG2014/000560 Ceased WO2015080667A1 (fr) 2013-11-27 2014-11-27 Appareil de mélange

Country Status (3)

Country Link
CN (1) CN106061594B (fr)
MY (1) MY185698A (fr)
WO (1) WO2015080667A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108993276A (zh) * 2018-08-08 2018-12-14 湖南长乐粮油贸易有限公司 一种防堵料糙米调质仓
CN114288901A (zh) * 2021-11-29 2022-04-08 安徽省碧绿春生物科技有限公司 一种饲料搅拌加工设备

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109737712A (zh) * 2019-01-22 2019-05-10 张宇 一种用于农业的谷物烘干设备
CN110152538B (zh) * 2019-05-16 2021-10-08 山东大学 地质力学模型实验智能化涡轮式自动拌和装置及方法

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB624207A (en) * 1947-06-12 1949-05-31 Anglo Iranian Oil Co Ltd Improvements relating to mixing apparatus
US2615692A (en) * 1948-02-05 1952-10-28 Muller Hans Device for mixing, stirring, emulsifying, etc.
GB1441280A (en) * 1973-07-03 1976-06-30 Ostberg J E Method and apparatus for stirring metallurgical melts
DD205824A1 (de) * 1982-07-01 1984-01-11 Adw Ddr Vorrichtung zur vibrationskultivierung
US4563247A (en) * 1984-05-10 1986-01-07 Phillips Petroleum Company Retort with anti-bridging mechanical agitator
JP2001170513A (ja) * 1999-12-20 2001-06-26 Aloka Co Ltd 攪拌具及び磁気ビーズ回収攪拌具
US6257755B1 (en) * 1998-12-10 2001-07-10 Taja Sevelle Compact butter maker
WO2002083280A1 (fr) * 2001-04-17 2002-10-24 Enersave Fluid Mixers Inc. Dispositif de commande de la taille de gouttelettes liquides

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1012468B (zh) * 1989-12-27 1991-05-01 北京化工学院 一种双轴复动式行星搅拌装置

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB624207A (en) * 1947-06-12 1949-05-31 Anglo Iranian Oil Co Ltd Improvements relating to mixing apparatus
US2615692A (en) * 1948-02-05 1952-10-28 Muller Hans Device for mixing, stirring, emulsifying, etc.
GB1441280A (en) * 1973-07-03 1976-06-30 Ostberg J E Method and apparatus for stirring metallurgical melts
DD205824A1 (de) * 1982-07-01 1984-01-11 Adw Ddr Vorrichtung zur vibrationskultivierung
US4563247A (en) * 1984-05-10 1986-01-07 Phillips Petroleum Company Retort with anti-bridging mechanical agitator
US6257755B1 (en) * 1998-12-10 2001-07-10 Taja Sevelle Compact butter maker
JP2001170513A (ja) * 1999-12-20 2001-06-26 Aloka Co Ltd 攪拌具及び磁気ビーズ回収攪拌具
WO2002083280A1 (fr) * 2001-04-17 2002-10-24 Enersave Fluid Mixers Inc. Dispositif de commande de la taille de gouttelettes liquides

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108993276A (zh) * 2018-08-08 2018-12-14 湖南长乐粮油贸易有限公司 一种防堵料糙米调质仓
CN114288901A (zh) * 2021-11-29 2022-04-08 安徽省碧绿春生物科技有限公司 一种饲料搅拌加工设备

Also Published As

Publication number Publication date
MY185698A (en) 2021-05-30
CN106061594B (zh) 2019-06-25
CN106061594A (zh) 2016-10-26

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