WO2007129023A1 - Mixing apparatus - Google Patents

Mixing apparatus Download PDF

Info

Publication number
WO2007129023A1
WO2007129023A1 PCT/GB2007/001524 GB2007001524W WO2007129023A1 WO 2007129023 A1 WO2007129023 A1 WO 2007129023A1 GB 2007001524 W GB2007001524 W GB 2007001524W WO 2007129023 A1 WO2007129023 A1 WO 2007129023A1
Authority
WO
WIPO (PCT)
Prior art keywords
impeller
mixing apparatus
cis
impellers
bis
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/GB2007/001524
Other languages
French (fr)
Inventor
Darren Gobby
John Colin Middleton
Neil Tindale
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.)
Mitsubishi Chemical UK Ltd
Original Assignee
Lucite International UK 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
Priority to CN2007800167915A priority Critical patent/CN101443100B/en
Priority to BRPI0711430-3A priority patent/BRPI0711430A2/en
Priority to ES07732561T priority patent/ES2375233T3/en
Priority to EA200870518A priority patent/EA015826B1/en
Priority to AT07732561T priority patent/ATE534456T1/en
Priority to AU2007246957A priority patent/AU2007246957B2/en
Priority to US12/300,072 priority patent/US20090208390A1/en
Priority to CA2650969A priority patent/CA2650969C/en
Priority to EP07732561A priority patent/EP2018218B1/en
Application filed by Lucite International UK Ltd filed Critical Lucite International UK Ltd
Priority to KR1020087027240A priority patent/KR101431600B1/en
Priority to JP2009508450A priority patent/JP5490528B2/en
Priority to MX2008014170A priority patent/MX2008014170A/en
Priority to PL07732561T priority patent/PL2018218T3/en
Publication of WO2007129023A1 publication Critical patent/WO2007129023A1/en
Anticipated expiration legal-status Critical
Priority to NO20084866A priority patent/NO20084866L/en
Priority to US13/763,393 priority patent/US9138694B2/en
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms 
    • B01F27/906—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms  with fixed axis
    • 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
    • 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
    • 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
    • B01F23/2336—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer
    • B01F23/23362—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer the gas being introduced under the stirrer
    • 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
    • B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
    • B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
    • B01F23/23763—Chlorine or chlorine containing gases
    • 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
    • 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
    • B01F27/113—Propeller-shaped stirrers for producing an axial flow, e.g. shaped like a ship or aircraft propeller
    • 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
    • B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
    • B01F27/191—Stirrers with two or more mixing elements mounted in sequence on the same axis with similar elements
    • 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
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • B01J10/002—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor carried out in foam, aerosol or bubbles
    • 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
    • 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
    • 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
    • B01J19/1806—Stationary reactors having moving elements inside resulting in a turbulent flow of the reactants, such as in centrifugal-type reactors, or having a high Reynolds-number
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
    • C07C51/14—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on a carbon-to-carbon unsaturated bond in organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2215/00—Auxiliary or complementary information in relation with mixing
    • B01F2215/04—Technical information in relation with mixing
    • B01F2215/0413—Numerical information
    • B01F2215/0436—Operational information
    • B01F2215/0481—Numerical speed values
    • 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
    • B01F23/2335—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the direction of introduction of the gas relative to the stirrer
    • B01F23/23351—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the direction of introduction of the gas relative to the stirrer the gas moving along the axis of rotation
    • 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
    • B01F23/2335—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the direction of introduction of the gas relative to the stirrer
    • B01F23/23353—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the direction of introduction of the gas relative to the stirrer the gas being sucked towards the rotating stirrer
    • 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
    • B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
    • B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
    • B01F23/23764—Hydrogen
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00761—Details of the reactor
    • B01J2219/00763—Baffles
    • B01J2219/00779—Baffles attached to the stirring means

Definitions

  • the invention relates to a mixing apparatus.
  • the invention relates to an apparatus for dispersing gas in liquid.
  • Impeller driven mixing systems generally incorporate one impeller mounted on a rotating shaft. Such systems may be said to have an axial longitudinal flow parallel to the axis of the rotating shaft and/or a radial flow parallel to the radially extending blades mounted on the shaft.
  • the impeller may thus be a radial flow impeller which projects fluid in a radial direction towards a wall of a chamber in which the impeller is housed, for example, a Chemineer BT- 6TM turbine, or alternatively, the impeller may be an axial flow impeller which comprises radially extending blades that are pitched at an angle so as to direct the fluid flow in an axial direction.
  • Examples of axial flow impellers include marine impellers and hydrofoil impellers.
  • Mixed flow systems are known, where the impeller causes flow in both axial and radial directions.
  • An example of a mixed flow impeller is the 45° pitched blade turbine.
  • Such mixing systems can be used in liquid-liquid, liquid-solid, or liquid-gas reactions.
  • a dual impeller system for dispersing a gas in a liquid, in a vessel is known.
  • Kuboi entitled “The Power Drawn by Dual Impeller Systems Under Gassed and Ungassed Conditions” Fourth European Conference on Mixing, April 27-29 1982
  • the combination of two axially spaced 45° pitched blade turbines is disclosed whereby a first impeller is mounted below a second impeller on a common shaft.
  • the impeller blades are orientated such that the first impeller projects liquid upwards and outwards and the second impeller projects liquid downwards and outwards.
  • the first impeller causes the incoming flow of gas bubbles to split so that some of the flow is driven radially outwards towards the walls of the vessel, and some is driven axially upwards towards the second impeller.
  • the effectiveness of the two impeller system under gassing conditions depends upon the speed of rotation of the impellers. At lower speeds it is possible that the bubbles that have been projected upwards by the first impeller are not affected by the second impeller.
  • the second impeller is unable to overcome buoyancy forces and therefore the second impeller plays no part in the dispersion of gas in the liquid. Only when the rotational speed of the second impeller is increased are the buoyancy forces overcome.
  • a controlled turbulent kinetic energy dissipation field results in a narrow bubble size distribution over a range of impeller specific powers.
  • a mixing apparatus for mixing at least two fluids, the mixing apparatus comprising a shaft rotatable about its longitudinal axis, a first and a second radially extending impeller mounted on the shaft and respectively axially spaced apart, characterised in that the first impeller comprises a plurality of curved blades operable to move said fluids in an axial direction towards the second impeller, and the second impeller comprises a plurality of curved blades operable to move said fluids in an axial direction towards the first impeller.
  • the blades on each impeller are inward pumping into the space between the impellers.
  • the lower impeller is, therefore, upward pumping and the upper impeller is downward pumping.
  • the blades of each impeller are hydrofoil blades.
  • a suitable hydrofoil blade is the Chemineer MaxfloTM W.
  • the Lightnin A315TM, A320TM or A340TM may be used.
  • a region of high turbulence is observed in a central mixing zone between said impellers.
  • the high turbulence is maintained in this zone, and so there is little variation in the turbulence energy dissipation. Consequently, there is minimal variation in bubble size which results in a narrow size distribution of the bubbles in the central mixing zone.
  • a narrow bubble size distribution enables the process or chemical reaction to be more easily controlled.
  • This region provides a zone where the at least two fluids are brought together to be mixed. A chemical reaction can therefore be facilitated in the central mixing zone.
  • the fluids may be liquid-solid, liquid-liquid, or liquid-gas.
  • the at least two fluids comprise a liquid and a gas.
  • the first impeller and the second impeller each comprise two or more curved blades, more preferably, three or more curved blades. Most preferably, are impellers with four curved blades.
  • the provision of an impeller with a large number of curved blades increases the shear forces acting to break up large bubbles .
  • the small bubbles produced have a smaller average bubble diameter than those produced with a first impeller and/or a second impeller with fewer curved blades and therefore, the available surface area for a reaction to occur is increased.
  • the diameter of the first impeller is the same as the diameter of the second impeller.
  • the diameter of the or each impeller is substantially half the diameter of the vessel in which said impeller is mounted.
  • the smaller the diameter of the impeller the greater the shear force created for a given power and therefore, a large number of small bubbles are produced which leads to an increase in available surface area for a reaction to occur.
  • the axial distance between the first impeller and the second impeller is at least one impeller diameter apart.
  • the turbulence created by the opposing impellers is an equilibrium in the central mixing zone which allows for prediction of bubble size and therefore control of the reaction occurring.
  • the total power drawn by the combination of impellers is low.
  • the impellers operate at a low power number, preferably substantially between 1 to 5, more preferably, substantially between 1 to 3, most preferably substantially 1.75.
  • the system consumes less energy than conventional systems which operate at power numbers of typically 3.2.
  • the power may be measured using conventional equipment, for example, strain gauges.
  • hydrofoil blades reduces tip vortices and converts more of the shaft energy into flow rather than turbulent kinetic energy, aiding complete dispersion.
  • the specific power used when the first impeller and the second impeller rotate is substantially between 50W/m 3 to 900W/m 3 , more preferably, substantially between 100W/m 3 to 800W/m 3 .
  • the preferred specific power is substantially between 50W/m 3 to 900W/m 3 .
  • the preferred specific power is substantially between 400W/m 3 to 3200W/m 3 . At such specific powers, a narrow bubble size distribution is maintained and the reaction is controlled.
  • the arithmetic mean size (di 0 ) is substantially between 250 ⁇ m to 550 ⁇ m and the surface volume mean diameter (d 32 ) is substantially between 400 ⁇ m to 750 ⁇ m.
  • the d xo is substantially between 250 ⁇ m to 350 ⁇ m, most preferably substantially 296 ⁇ m, and preferably, the d 32 is substantially between 400 ⁇ m to 500 ⁇ m, most preferably substantially 450 ⁇ m.
  • the di 0 when operating at substantially 991rpm, is substantially between 300 ⁇ m to 400 ⁇ m, most preferably substantially 330 ⁇ m, and preferably, the d 32 is substantially between 460 ⁇ m to ⁇ 60 ⁇ m, most preferably substantially 510 ⁇ m.
  • the di 0 when operating at substantially 1200rpm, is substantially between 350 ⁇ m to 450 ⁇ m, most preferably substantially 394 ⁇ m, and preferably, the d 32 is substantially between 450 ⁇ m to 550 ⁇ m, most preferably substantially 500 ⁇ m.
  • the d 10 is substantially between 250 ⁇ m to 1500 ⁇ m.
  • the d i0 is substantially between 550 ⁇ m to 650 ⁇ m, most preferably substantially 633 ⁇ m
  • the d 32 is preferably substantially between 800 ⁇ m to lOOO ⁇ m, most preferably substantially 978 ⁇ m.
  • the d 10 is preferably substantially between 800 ⁇ m to 900 ⁇ m, most preferably substantially 841 ⁇ m
  • the d 32 is preferably substantially between lOOO ⁇ m to 1500 ⁇ m, most preferably substantially 1345 ⁇ m.
  • the di 0 is preferably substantially between 500 ⁇ m to 600 ⁇ m, most preferably substantially 597 ⁇ m, and the d 32 is preferably substantially between 700 ⁇ m to 800 ⁇ m, most preferably substantially 721 ⁇ m.
  • the d 10 is preferably substantially between 300 ⁇ m to 400 ⁇ m, most preferably substantially 378 ⁇ m, and the d 32 is preferably substantially between 400 ⁇ m to 500 ⁇ m, most preferably substantially 445 ⁇ m.
  • the sparged gas rate is substantially between 0.05 to 1.0 m 3 /s, preferably substantially between 0.1 to 0.5m 3 /s, most preferably substantially 0.13m 3 /s at an impeller speed of preferably between 50rpm to 1200rpm, most preferably substantially 50rpm to 200rpm.
  • a key parameter used in the design of gas-liquid mixing systems is the critical dispersion speed. This is the minimum impeller speed required to ensure uniform dispersion of the gas bubbles.
  • the critical dispersion speed for achieving dispersion in a dual opposed flow hydrofoil system in a vessel having a diameter of preferably substantially between 1 to 10m, more preferably, substantially between 2 to 5m, is preferably substantially between 1 to lOOrpm, preferably substantially between 5 to 50rpm, more preferably substantially between 10 to 20rpm, most preferably substantially 14rpm.
  • a chemical reaction system comprising a liquid phase and a mixing apparatus according to the first aspect of the invention for mixing a fluid into the liquid phase.
  • the fluid is a solid or most preferably, the fluid is a gas.
  • the liquid phase comprises at least one liquid phase reactant for reacting with a gas introduced into the liquid phase, as well as at least one liquid phase reaction product.
  • the liquid phase includes a gas introduced therein.
  • the said gas comprises one or more reactants capable of reacting with the said one or more reactants.
  • the liquid phase comprises a catalyst system.
  • the reaction system is a carbonylation reaction system such as one described in co-pending United Kingdom patent application GB 0516556.8 or as referred to in European patents and patent applications EP-A-0055875, EP-A- 04489472, EP-A-0106379 , EP-A-0235864 , EP-A-0274795 , EP-A- 0499329, EP-A-0386833, EP-A-0441447 , EP-A-0489472 , EP-A- 0282142, EP-A- 0227160 , EP-A-0495547 , EP-A-0495548 , EP-A- 1651587, EP-A-1565425, EP-A-1554039 , EP-A-1534427 , EP-A- 1527038, EP-A-1204476, WO2005118519 and WO2005079981.
  • the reaction system is a carbonylation process comprising carbonylating an ethylenically unsaturated compound with carbon monoxide in the presence of a source of hydroxy1 groups, preferably, methanol, and a catalyst system comprising (a) a bidentate phosphine, arsine or stibine ligand, and (b) a catalytic metal selected from a group 8, 9 or 10 metal or a compound thereof, preferably palladium.
  • a source of hydroxy1 groups preferably, methanol
  • a catalyst system comprising (a) a bidentate phosphine, arsine or stibine ligand, and (b) a catalytic metal selected from a group 8, 9 or 10 metal or a compound thereof, preferably palladium.
  • the phosphine ligand is selected from 1, 2-bis- (di-tert-butylphosphinomethyl) benzene, 1,2- bis- (di-tert-pentylphosphinomethyl) benzene, 1 , 2-bis- (di- tert-butylphosphinomethyl) naphthalene, 1, 2 bis (diadamantylphosphinomethyl) benzene, 1,2 bis(di-3,5- dimethyladamantylphosphinomethyl) benzene, 1,2 bis(di-5- tert-butyladamantylphosphinomethyl) benzene, 1,2 bis (1- adamantyl tert-butyl -phosphinomethyl) benzene, 1- (diadamantylphosphinomethyl) -2- (di-tert- butylphosphinomethyl) benzene, 1- (di-tert-tert-
  • adamantylmethyl ) ) benzene; cis-1, 2-bis (di-t- butylphosphinomethyl) -4 , 5- dimethyl cyclohexane; cis-1, 2- bis (di-t-butylphosphinomethyl) -5- methylcyclopentane; cis-1 , 2 -bis (2 -phosphinomethyl-1,3,5, 7-tetramethyl-6,9,10- trioxa-adamantyl) -4 , 5-dimethylcyclohexane; cis-1, 2-bis (2- phosphinomethyl-1, 3,5, 7-tetramethyl-6, 9, 10-trioxa- adamantyl) 5-methylcyclopentane; cis-1, 2-bis (di- adamantylphosphinomethyl) -4 , 5 dimethylcyclohexane; cis- 1, 2-bis (di -adamantylphosphinomethyl)
  • Figure 1 is a schematic sectional side view of a prior art mixing apparatus
  • Figure 2 is a schematic sectional side view of a mixing apparatus according to the invention.
  • Figure 3 is a schematic sectional side view of a mixing apparatus according to the invention in use.
  • Figure 4 is a further schematic sectional side view. of a mixing apparatus according to the invention in use.
  • FIG. 1 shows a prior art mixing apparatus 10 in use in a vessel 12 containing a liquid 14.
  • the vessel 12 has an inlet 16 through which a gas 18 is sparged into the liquid 14.
  • the mixing apparatus 10 comprises a vertical elongate shaft 20 rotatable about a longitudinal axis 21 on which are fixedly mounted a first impeller 22 and a second impeller 24 in spaced apart relation.
  • the first impeller 22 is mounted above the second impeller 24.
  • Both the first and the second impellers 22,24 are 45° pitched blade turbines .
  • said impellers In use, said impellers must rotate at the same speed.
  • the first impeller 22 causes incoming gas bubbles 26 to flow in a both an axial and radial direction.
  • the axial component of the flow creates momentum, which along with buoyancy, prevents the second impeller 24 from operating effectively.
  • the momentum and buoyancy is only overcome by increasing the speed of the impellers 22, 24. This increase in speed causes full dispersion of the gas 18 in the liquid 14 as shown in Figure 1 by the lines A. Nonuniform dispersion of the liquid 14 in the gas 18 is undesirable because the mixing process cannot be controlled.
  • FIG. 2 shows a mixing apparatus 100 according to the present invention.
  • the mixing apparatus 100 comprises a vertical elongate shaft 120 rotatable about a longitudinal axis 121 on which are fixedly mounted a first impeller 122 and a second impeller 124 in a spaced apart arrangement. Both the first and the second impeller 122, 124 comprise a number of hydrofoil blades 125.
  • Each impeller 122,124 comprises four radially extending blades 125 fixedly mounted on the shaft 120 for co-operating rotation about the longitudinal axis of the shaft, in use.
  • Each blade 125 on each impeller 122,124 is a hydrofoil blade arranged so as to impel the surrounding fluid axially in the direction of the other impeller.
  • the first or lower impeller 122 is thus an up-pumping impeller and the second or upper impeller 124 is a down-pumping impeller.
  • the first or lower impeller 122 is thus an up-pumping impeller and the second or upper impeller 124 is a down-pumping impeller.
  • the second or upper impeller 124 is a down-pumping impeller.
  • any number of blades may be used on each of the said impellers, for example, 3, 4 or even 6 blades.
  • Particularly suitable commercially available impellers are those known as MaxfloTM W, A315, A320 or A340 impellers.
  • the first impeller 122 is mounted on the shaft 120 so that the concave face of the blades 125 face in an upward direction.
  • the second impeller 124 is spaced along the shaft 120 and is mounted so that the concave face of the blades 125 face in a downwards direction.
  • the distance between the first impeller 122 and the second impeller 124 is approximately the diameter of either of the said impellers 122, 124.
  • FIG 3 shows the mixing apparatus 100 in a cylindrical vessel 112.
  • a gas inlet 116 is located in the bottom-wall 132 of the vessel 112 adjacent to the base 132.
  • the vessel 112 can be of any suitable alternative configuration, for example, it may be a hopper.
  • the mixing apparatus 100 is centrally suspended in the vessel 112.
  • mixing apparatus 100 Although only one mixing apparatus 100 is shown in Figure 3, it will be appreciated that any number of mixing apparatus 100 could be used in the chamber 112. For example, two, three, or four mixing apparatus 100 may be mounted in the chamber 112.
  • first or second impellers 122,124 may be mounted on the shaft 120 and in keeping with the object of the invention.
  • the arrangement 200 shown in Figure 4 wherein a series of first impellers 222 and a series of second impellers 224 are mounted on the shaft 220.
  • Any number of impellers 222,224 may be provided on the shaft 220.
  • An alternative configuration would comprise pairs of impellers mounted on the shaft. Each pair would comprise a first impeller and a second impeller. There may be a number of pairs of impellers on any given shaft, for example, two, three, or four pairs.
  • the fluid for example, gas
  • the fluid may be introduced into the chamber through the base or the side wall thereof, being directed under and towards the first impeller.
  • the first or the second impeller may be driven by a separate drive means so that the rotational speed of, for example, the first impeller, may be different to the rotational speed of the said other impeller.
  • the diameter of the first and second impellers may not necessarily be the same in any one of the embodiments shown. Further, the optimum distance between two impellers is dependent upon the geometry of the vessel and the diameter of said impellers.
  • the vessel 112,212 is filled with fluid 114,214.
  • a gas 118,218 is then directed into the vessel 112,212 via gas inlet 116,216.
  • the shaft 120,220 is rotated by a suitable drive means (not shown) , so as to cause the first impeller 122,222 and the second impeller 124,224 to rotate about the longitudinal axis 121,221 of the shaft 120,220 in a liquid 114.
  • the gas 118,218 enters the vessel 112,212 as large bubbles 150,215. Rotation of the first impeller 122,222 causes the large bubbles 150,215 to move in an axial direction towards the blades 125,225.
  • the second impeller 124,224 causes axial flow in a downwards direction towards the first impeller 122,222. Due to the opposing axial flow paths created by said impellers, a central zone 160,260, or high turbulent energy dissipation zone, is established.
  • the central zone 160,260 comprises an area of comparatively uniform high turbulent energy dissipation with high interfacial area to allow reaction between reactants in the liquid 114,214 and in reactants in the gas 118,218. Further, because the turbulent energy dissipation in the central zone 160,260 is maintained without much variation, a narrow size distribution of small bubbles is produced. Such a narrow size distribution enables the reactor performance to be predicted and controlled.
  • the mixing apparatus 100,200 is particularly suited to carbonylation processes.
  • Table 1 gives an example of resultant bubble size for a dual opposed Maxflo impeller system operating at various speeds, and at 4.2mm/sec.
  • the bubble size was determined using a typical image capture camera.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Dispersion Chemistry (AREA)
  • Aviation & Aerospace Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Confectionery (AREA)
  • Accessories For Mixers (AREA)

Abstract

A mixing apparatus (100) for mixing at least two fluids, the mixing apparatus (100) comprising a shaft (120) rotatable about its longitudinal axis (121), a first (122) and a second (124) radially extending impeller mounted on the shaft (120) and respectively axially spaced apart, characterised in that the first impeller (122) comprises a plurality of curved blades (125) operable to move said fluids in an axial direction towards the second impeller (124), and the second impeller (124) comprises a plurality of curved blades (125) operable to move said fluids in an axial direction towards the first impeller (122).

Description

MIXING APPARATUS
The invention relates to a mixing apparatus. In particular, but not exclusively, the invention relates to an apparatus for dispersing gas in liquid.
Many industrial processes incorporate an impeller driven mixing system, for example, processes for fermentation, hydrogenation, chlorination, oxidation, and carbonylation.
Impeller driven mixing systems generally incorporate one impeller mounted on a rotating shaft. Such systems may be said to have an axial longitudinal flow parallel to the axis of the rotating shaft and/or a radial flow parallel to the radially extending blades mounted on the shaft. The impeller may thus be a radial flow impeller which projects fluid in a radial direction towards a wall of a chamber in which the impeller is housed, for example, a Chemineer BT- 6™ turbine, or alternatively, the impeller may be an axial flow impeller which comprises radially extending blades that are pitched at an angle so as to direct the fluid flow in an axial direction. Examples of axial flow impellers include marine impellers and hydrofoil impellers. Mixed flow systems are known, where the impeller causes flow in both axial and radial directions. An example of a mixed flow impeller is the 45° pitched blade turbine. Such mixing systems can be used in liquid-liquid, liquid-solid, or liquid-gas reactions.
A dual impeller system for dispersing a gas in a liquid, in a vessel, is known. Specifically, in a paper by Kuboi , entitled "The Power Drawn by Dual Impeller Systems Under Gassed and Ungassed Conditions" Fourth European Conference on Mixing, April 27-29 1982, the combination of two axially spaced 45° pitched blade turbines is disclosed whereby a first impeller is mounted below a second impeller on a common shaft. The impeller blades are orientated such that the first impeller projects liquid upwards and outwards and the second impeller projects liquid downwards and outwards. Under gassed conditions, as gas is introduced into the vessel, the first impeller causes the incoming flow of gas bubbles to split so that some of the flow is driven radially outwards towards the walls of the vessel, and some is driven axially upwards towards the second impeller.
The effectiveness of the two impeller system under gassing conditions depends upon the speed of rotation of the impellers. At lower speeds it is possible that the bubbles that have been projected upwards by the first impeller are not affected by the second impeller. The second impeller is unable to overcome buoyancy forces and therefore the second impeller plays no part in the dispersion of gas in the liquid. Only when the rotational speed of the second impeller is increased are the buoyancy forces overcome.
Disadvantageously, non-uniform dispersion of the gas in the liquid results. This is shown in Figure 1 of the application. In order to achieve uniform dispersion, further disadvantageously, the rotational speed of the second impeller has to be sharply increased.
It is highly desirable to be able to achieve complete uniform dispersion in an industrial process. In industrial processes where gas/liquid mass transfer is an essential feature, this aids controllability and enhances reactor performance. In such processes, when the gas is well dispersed, a region of reasonably uniform turbulent
kinetic eddy dissipation can exist in the liquid between and around the impellers which controls coalescence and breakup of the bubbles. If the gas dispersion is highly non-uniform, undesirable coalescence can result in a sharp increase in bubble size and therefore, the surface area for interface mass transfer to occur is reduced. Advantageously, a controlled turbulent kinetic energy dissipation field results in a narrow bubble size distribution over a range of impeller specific powers.
It is an object of the present invention to provide a mixing apparatus which enables controllable mixing of fluids or solids whilst simultaneously providing an effective mixing environment.
According to a first aspect of the present invention there is provided a mixing apparatus for mixing at least two fluids, the mixing apparatus comprising a shaft rotatable about its longitudinal axis, a first and a second radially extending impeller mounted on the shaft and respectively axially spaced apart, characterised in that the first impeller comprises a plurality of curved blades operable to move said fluids in an axial direction towards the second impeller, and the second impeller comprises a plurality of curved blades operable to move said fluids in an axial direction towards the first impeller.
Preferably, the blades on each impeller are inward pumping into the space between the impellers. In the case of a substantially vertical shaft, the lower impeller is, therefore, upward pumping and the upper impeller is downward pumping. Preferably, the blades of each impeller are hydrofoil blades. A suitable hydrofoil blade is the Chemineer Maxflo™ W. Alternatively, the Lightnin A315™, A320™ or A340™ may be used.
Advantageously, due to the opposing axial flows created by the first impeller and the second impeller, a region of high turbulence is observed in a central mixing zone between said impellers. The high turbulence is maintained in this zone, and so there is little variation in the turbulence energy dissipation. Consequently, there is minimal variation in bubble size which results in a narrow size distribution of the bubbles in the central mixing zone. Advantageously, a narrow bubble size distribution enables the process or chemical reaction to be more easily controlled. This region provides a zone where the at least two fluids are brought together to be mixed. A chemical reaction can therefore be facilitated in the central mixing zone. The fluids may be liquid-solid, liquid-liquid, or liquid-gas. Preferably, the at least two fluids comprise a liquid and a gas.
It is advantageous to provide a gas/liquid mixing environment where the bubble size is largely independent of the impeller specific power. In such a system the liquid mixing time may be varied independently of the bubble size.
Preferably, the first impeller and the second impeller each comprise two or more curved blades, more preferably, three or more curved blades. Most preferably, are impellers with four curved blades. The provision of an impeller with a large number of curved blades increases the shear forces acting to break up large bubbles . The small bubbles produced have a smaller average bubble diameter than those produced with a first impeller and/or a second impeller with fewer curved blades and therefore, the available surface area for a reaction to occur is increased.
Preferably, the diameter of the first impeller is the same as the diameter of the second impeller. Preferably, the diameter of the or each impeller is substantially half the diameter of the vessel in which said impeller is mounted.
Advantageously, the smaller the diameter of the impeller, the greater the shear force created for a given power and therefore, a large number of small bubbles are produced which leads to an increase in available surface area for a reaction to occur.
Preferably, the axial distance between the first impeller and the second impeller is at least one impeller diameter apart. In this configuration, the turbulence created by the opposing impellers is an equilibrium in the central mixing zone which allows for prediction of bubble size and therefore control of the reaction occurring.
It is preferable that the total power drawn by the combination of impellers is low. Preferably, the impellers operate at a low power number, preferably substantially between 1 to 5, more preferably, substantially between 1 to 3, most preferably substantially 1.75. In so doing, the system consumes less energy than conventional systems which operate at power numbers of typically 3.2. The power may be measured using conventional equipment, for example, strain gauges.
Preferably, when operating at a low power number complete uniform dispersed phase distribution is achieved. This is highly desirable and is because of the energy efficiency of the blades, preferably hydrofoil blades.
Without being restricted by theory, one possible explanation for the efficiency of the invention is that the use of hydrofoil blades reduces tip vortices and converts more of the shaft energy into flow rather than turbulent kinetic energy, aiding complete dispersion.
Preferably, the specific power used when the first impeller and the second impeller rotate is substantially between 50W/m3 to 900W/m3, more preferably, substantially between 100W/m3 to 800W/m3.
Preferably, when dual opposed Maxflo type impellers are used in the system, the preferred specific power is substantially between 50W/m3 to 900W/m3. Preferably, when BT- 6 type impellers are used, the preferred specific power is substantially between 400W/m3 to 3200W/m3. At such specific powers, a narrow bubble size distribution is maintained and the reaction is controlled.
Preferably, when dual opposed Maxflo impellers are used, the arithmetic mean size (di0) is substantially between 250μm to 550μm and the surface volume mean diameter (d32) is substantially between 400μm to 750μm. Preferably, when operating at substantially 750rpm, the dxo is substantially between 250μm to 350μm, most preferably substantially 296μm, and preferably, the d32 is substantially between 400μm to 500μm, most preferably substantially 450μm. Preferably, when operating at substantially 991rpm, the di0 is substantially between 300μm to 400μm, most preferably substantially 330μm, and preferably, the d32 is substantially between 460μm to Ξ60μm, most preferably substantially 510μm. ■ Preferably, when operating at substantially 1200rpm, the di0 is substantially between 350μm to 450μm, most preferably substantially 394μm, and preferably, the d32 is substantially between 450μm to 550μm, most preferably substantially 500μm.
Preferably, when BT- 6 type impellers are used, the d10 is substantially between 250μm to 1500μm. Particularly, when operating at substantially 251rpm, preferably the di0 is substantially between 550μm to 650μm, most preferably substantially 633μm, and the d32 is preferably substantially between 800μm to lOOOμm, most preferably substantially 978μm. Preferably, when operating at substantially 380rpm, the d10 is preferably substantially between 800μm to 900μm, most preferably substantially 841μm, and the d32 is preferably substantially between lOOOμm to 1500μm, most preferably substantially 1345μm. At substantially 500rpm, the di0 is preferably substantially between 500μm to 600μm, most preferably substantially 597μm, and the d32 is preferably substantially between 700μm to 800μm, most preferably substantially 721μm. Preferably, when operating at substantially 765rpm, the d10 is preferably substantially between 300μm to 400μm, most preferably substantially 378μm, and the d32 is preferably substantially between 400μm to 500μm, most preferably substantially 445μm. In a reactor where gas is sparged into an agitated liquid medium, preferably, the sparged gas rate is substantially between 0.05 to 1.0 m3/s, preferably substantially between 0.1 to 0.5m3/s, most preferably substantially 0.13m3/s at an impeller speed of preferably between 50rpm to 1200rpm, most preferably substantially 50rpm to 200rpm.
A key parameter used in the design of gas-liquid mixing systems is the critical dispersion speed. This is the minimum impeller speed required to ensure uniform dispersion of the gas bubbles. The critical dispersion speed for achieving dispersion in a dual opposed flow hydrofoil system in a vessel having a diameter of preferably substantially between 1 to 10m, more preferably, substantially between 2 to 5m, is preferably substantially between 1 to lOOrpm, preferably substantially between 5 to 50rpm, more preferably substantially between 10 to 20rpm, most preferably substantially 14rpm.
Accordingly, in a further aspect of the present invention there is provided a chemical reaction system comprising a liquid phase and a mixing apparatus according to the first aspect of the invention for mixing a fluid into the liquid phase. Preferably, the fluid is a solid or most preferably, the fluid is a gas.
Preferably, the liquid phase comprises at least one liquid phase reactant for reacting with a gas introduced into the liquid phase, as well as at least one liquid phase reaction product. Preferably, the liquid phase includes a gas introduced therein. Preferably, the said gas comprises one or more reactants capable of reacting with the said one or more reactants. Preferably, the liquid phase comprises a catalyst system. Preferably, the reaction system is a carbonylation reaction system such as one described in co-pending United Kingdom patent application GB 0516556.8 or as referred to in European patents and patent applications EP-A-0055875, EP-A- 04489472, EP-A-0106379 , EP-A-0235864 , EP-A-0274795 , EP-A- 0499329, EP-A-0386833, EP-A-0441447 , EP-A-0489472 , EP-A- 0282142, EP-A- 0227160 , EP-A-0495547 , EP-A-0495548 , EP-A- 1651587, EP-A-1565425, EP-A-1554039 , EP-A-1534427 , EP-A- 1527038, EP-A-1204476, WO2005118519 and WO2005079981.
Preferably, the reaction system is a carbonylation process comprising carbonylating an ethylenically unsaturated compound with carbon monoxide in the presence of a source of hydroxy1 groups, preferably, methanol, and a catalyst system comprising (a) a bidentate phosphine, arsine or stibine ligand, and (b) a catalytic metal selected from a group 8, 9 or 10 metal or a compound thereof, preferably palladium. Preferably, the phosphine ligand is selected from 1, 2-bis- (di-tert-butylphosphinomethyl) benzene, 1,2- bis- (di-tert-pentylphosphinomethyl) benzene, 1 , 2-bis- (di- tert-butylphosphinomethyl) naphthalene, 1, 2 bis (diadamantylphosphinomethyl) benzene, 1,2 bis(di-3,5- dimethyladamantylphosphinomethyl) benzene, 1,2 bis(di-5- tert-butyladamantylphosphinomethyl) benzene, 1,2 bis (1- adamantyl tert-butyl -phosphinomethyl) benzene, 1- (diadamantylphosphinomethyl) -2- (di-tert- butylphosphinomethyl) benzene, 1- (di-tert- butylphosphinomethyl) -2-
(dicongressylphosphinomethyl) benzene, I- (di-tert- butylphosphinomethyl) -2- (phospha-adamantyl-P- methyl) benzene, 1- (diadamantylphosphinomethyl) -2- (phospha- adamantyl-P-methyl) benzene, 1- (tert- butyladamantylphosphinomethyl) -2- (diadamantylphosphinomethyl) benzene and 1- [(P- (2, 2,6,6, - tetra-methylphosphinan-4-one)phosphinomethyl) ] -2- (phospha- adamantyl-P-methyl) benzene, wherein "phospha-adamantyl" is selected from 2-phospha-l , 3 , 5, 7-tetramethyl-6, 9, 10- trioxadamantyl , 2-phospha-l , 3 , 5-trimethyl-6, 9,10 trioxadamantyl , 2-phospha-l, 3,5,7-tetra (trifluoromethyl) - 6, 9, 10 -trioxadamantyl or 2-phospha-l , 3 , 5- tri (trifluoromethyl) -6,9, 10 -trioxadamantyl ; 1, 2-bis-
(dimethylaminomethyl) ferrocene, 1,2-bis-
(ditertbutylphosphinomethyl) ferrocene, l-hydroxymethyl-2- dimethylaminomethylferrocene, 1 , 2-bis- (ditertbutylphosphinomethyl) ferrocene, 1-hydroxymethyl-
2, 3 -bis- (dimethylaminomethyl) ferrocene, 1,2, 3-tris-
(ditertbutylphosphinomethyl) ferrocene, 1,2-bis-
(dicyclohexylphosphinomethyl) ferrocene, 1,2-bis- (di-iso- butylphosphinomethyl) ferrocene, 1, 2-bis- (dicyclopentylphosphinomethyl) ferrocene, 1,2-bis-
(diethylphosphinomethyl) ferrocene, 1 , 2 -bis (di- isopropylphosphinomethyl) ferrocene, 1 , 2-bis-
(dimethylphosphinomethyl) ferrocene, 1,2-bis- (di- (1,3,5,7- tetramethyl-6, 9, 10-trioxa-2-phospha- adamantylmethyl) ) ferrocene, 1,2-bis-
(dimethylaminomethyl) ferrocene-bismethyl iodide, 1,2- bis (dihydroxymethylphosphinomethyl) ferrocene, 1,2- bis (diphosphinomethyl) ferrocene, 1, 2-bis-α,o;- (P- (2,2,6,6, - tetramethylphosphinan-4 -one) ) dimethylferrocene, and 1,2- bis- (di-1, 3, 5, 7-tetramethyl-6 , 9, 10-trioxa-2-phospha-
adamantylmethyl ) ) benzene; cis-1, 2-bis (di-t- butylphosphinomethyl) -4 , 5- dimethyl cyclohexane; cis-1, 2- bis (di-t-butylphosphinomethyl) -5- methylcyclopentane; cis-1 , 2 -bis (2 -phosphinomethyl-1,3,5, 7-tetramethyl-6,9,10- trioxa-adamantyl) -4 , 5-dimethylcyclohexane; cis-1, 2-bis (2- phosphinomethyl-1, 3,5, 7-tetramethyl-6, 9, 10-trioxa- adamantyl) 5-methylcyclopentane; cis-1, 2-bis (di- adamantylphosphinomethyl) -4 , 5 dimethylcyclohexane; cis- 1, 2-bis (di -adamantylphosphinomethyl) -5-methyl cyclopentane; cis-1- (P, P adamantyl, t-butyl phosphinomethyl) -2- (di-t-butylphosphinomethyl) -4,5- dimethylcyclohexane; cis-1- (P, P adamantyl, t-butyl phosphinomethyl) -2- (di-t-butylphosphinomethyl) -5- methylcyclopentane; cis-1- (2-phosphinomethyl-l, 3 , 5 , 7- tetramethyl-6, 9, 10-trioxa-adamantyl) - 2 - (di-t- butylphosphinomethyl) 4, 5- dimethylcyclohexane; cis-1- (2- phosphinomethyl- 1, 3,5, 7-tetramethyl-6 , 9, 10-trioxa- adamantyl) - 2 - (di-t-butylphosphinomethyl) -5-methyl cyclopentane; cis-1- (2-phosphinomethyl-l ,3,5,7- tetramethyl-6 , 9 , 10-trioxa-adamantyl) -2- (diadamantylphosphinomethyl) -5-methyl cyclohexane; cis-1- (2-phosphinomethyl-l, 3,5, 7-tetramethyl-6, 9, 10-trioxa- adamantyl) -2- (diadamantylphosphinomethyl) -5-methyl cyclopentane ; cis-1- (2-phosphinomethyl-l , 3,5,7- tetramethyl-6, 9 , 10-trioxa-adamantyl) -2- (diadamantylphosphinomethyl) cyclobutane; cis-1- (di-t- butylphosphinomethyl) -2- (diadamantylphosphinomethyl) - 4,5-dimethyl cyclohexane; cis-1- (di-t- butylphosphinomethyl) -2- (diadamantylphosphinomethyl) -5- methyl cyclopentane; cis-1 , 2-bis (2-phospha-l , 3 , 5- trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -4,5- dimethyl cyclohexane; cis-1, 2-bis (2-phospha-l, 3 , 5- trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -5- methyl cyclopentane; cis-1- (2-phospha-l , 3 , 5-trimethyl- 6,9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2- (di-t- butylphosphinomethyl) -4 , 5 -dimethyl cyclohexane; cis-1- (2-phospha-l, 3, 5-trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2- (di-t-butylphosphinomethyl) -5- methyl cyclopentane; cis-1- (2-phospha-l , 3 , 5-trimethyl- 6,9,10-trioxatricyclo-{3.3.1.1 [3.7] }decyl) -2-
(diadamantylphosphinomethyl) -4 , 5 -dimethyl cyclohexane; cis-1- (2-phospha-l , 3 , 5-trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2- (diadamantylphosphinomethyl) -5- methyl cyclopentane; cis-1, 2-bis-perfluoro (2-phospha- 1,3,5, 7-tetramethyl-6, 9, 10-trioxatricyclo{3.3.1.1 [3.7] }- decyl) -4 , 5 -dimethyl cyclohexane; cis-1 , 2-bis-perfluoro (2- phospha-1, 3,5, 7-tetramethyl-6, 9, 10- trioxatricyclo{3.3.1.1 [3.7] } decyl) -5-methyl cyclopentane; cis-1, 2 -bis- (2-phospha-l , 3 , 5, 7-tetra (trifluoro-methyl) - 6, 9,10-trioxatricyclo{3.3.1.1 [3.7] } decyl) -4 , 5-dimethyl cyclohexane; cis-l,2-bis- (2-phospha-l , 3 , 5, 7- tetra (trifluoro-methyl) -6,9, 10- trioxatricyclo{3.3.1.1 [3.7] }decyl) -5 -methyl cyclopentane; cis-l,2-bis (di-t-butylphosphinomethyl) cyclohexane; cis- 1, 2 -bis (di-t-butylphosphinomethyl) cyclopentane; cis-1, 2- bis (di-t-butylphosphinomethyl) cyclobutane; cis-1, 2- bis (2-phosphinomethyl-l, 3,5, 7-tetramethyl-6 , 9, 10-trioxa- adamantyl) cyclohexane; cis-1, 2-bis (2-phosphinomethyl- 1,3,5, 7-tetramethyl-6 , 9 , 10-trioxa-adamantyl) cyclopentane; cis-1, 2-bis (2-phosphinomethyl-l, 3 , 5, 7-tetramethyl-6, 9, 10- trioxa-adamantyl) cyclobutane; cis-1, 2-bis (diadamantylphosphinomethyl) cyclohexane; cis-1, 2-bis (diadamantylphosphinomethyl) cyclopentane; cis-1, 2-bis (diadamantylphosphinomethyl) cyclobutane; cis-1- (P, P- adamantyl, t-butyl -phosphinomethyl) -2- (di-t- butylphosphinomethyl) cyclohexane; cis-1- (P, P-adamantyl, t-butyl-phosphinomethyl) -2- (di-t- butylphosphinomethyl) cyclopentane; cis-1- (P, P-adamantyl, t-butyl-phosphinomethyl) -2- (di-t- butylphosphinomethyl) cyclobutane; cis-1- (2- phosphinomethyl-1, 3,5, 7-tetramethyl-6, 9, 10-trioxa- adamantyl) - 2 - (di-t-butylphosphinomethyl) cyclohexane; cis-1- (2-phosphinomethyl-l,3,5,7-tetramethyl-6, 9, 10- trioxa-adamantyl) - 2 - (di-t- butylphosphinomethyl) cyclopentane; cis-1- (2- phosphinomethyl-1, 3,5, 7-tetramethyl-6 , 9, 10-trioxa- adatnantyl) - 2 - (di-t-butylphosphinomethyl) cyclobutane; cis-1- (2 -phosphinomethyl-1,3, 5, 7-tetramethyl-6 , 9, 10- trioxa-adamantyl) -2-
(diadamantylphosphinomethyl) cyclohexane; cis-1- (2- phosphinomethyl-1, 3,5, 7-tetramethyl-6 , 9, 10-trioxa- adamantyl) -2- (diadamantylphosphinomethyl) cyclopentane; cis-1- (2-phosphinomethyl-l, 3,5, 7-tetramethyl-6, 9,10- trioxa-adamantyl) -2-
(diadamantylphosphinomethyl) cyclobutane; cis-1- (di-t- butylphosphinomethyl) -2- (diadamantylphosphinomethyl) cyclohexane; cis-1- (di-t- butylphosphinomethyl) -2-
(diadamantylphosphinomethyl) cyclopentane; cis-1- (di-t- butylphosphinomethyl) -2-
(diadamantylphosphinomethyl) cyclobutane; cis-1, 2-bis (2- phospha-1, 3 , 5-trimethyl-6 , 9, 10-trioxatricyclo- {3.3.1.1 [3.7] Jdecyl) cyclohexane; cis-1 , 2-bis (2-phospha- 1,3, 5-trimethyl-6, 9, 10-trioxatricyclo-
{3.3.1.1 [3.7] }decyl) cyclopentane; cis-1, 2-bis (2-phospha- 1,3, 5-trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) cyclobutane; cis-1- (2-phospha- 1,3, 5-trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2- (di-t- butylphosphinomethyl) cyclohexane; cis-1- (2-phospha- 1,3, 5-trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2- (di-t- butylphosphinomethyl) cyclopentane; cis-1- (2-phospha-l, 3 , 5- trimethyl-6,9,10-trioxatricyclo-{3.3.1.1 [3.7] }decyl) -2- (di-t-butylphosphinoτnethyl) cyclobutane; cis-1- (2-phospha- 1,3, 5-trimethyl-6, 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2-
(diadamantylphosphinomethyl) cyclohexane; cis-1- (2-phospha- 1,3, 5-trimethyl-6, 9 , 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2- (diadamantylphosphinomethyl) cyclopentane; cis-1- (2- phospha-1, 3 , 5-trimethyl-6 , 9, 10-trioxatricyclo- {3.3.1.1 [3.7] }decyl) -2-
(diadamantylphosphinomethyl) cyclobutane; cis-l,2-bis- perfluoro (2-phospha-l, 3,5, 7-tetramethyl-6, 9, 10- trioxatricyclo{3.3.1.1 [3.7] }-decyl) cyclohexane; cis-1, 2- bis-perfluoro (2-phospha-l, 3,5, 7-tetramethyl-6 ,9,10- trioxatricyclo{3.3.1.1 [3.7] }decyl) cyclopentane; cis-1, 2- bis-perfluoro (2-phospha-l, 3,5, 7-tetramethyl-6, 9, 10- trioxatricyclo{3.3.1.1 [3.7] }decyl) cyclobutane; cis-1, 2- bis- (2-phospha-l, 3 , 5, 7-tetra (trifluoro-methyl) -6, 9, 10- trioxatricyclo{3.3.1.1 [3.7] }decyl) cyclohexane; cis- 1, 2-bis- (2-phospha-l, 3,5, 7-tetra (trifluoro-methyl) - 6,9, 10-trioxatricyclo{3.3.1.1 [3.7] }decyl) cyclopentane; and cis-1, 2-bis- (2-phospha-l, 3 , 5 , 7-tetra (trifluoro-methyl) - 6,9, 10-trioxatricyclo{3.3.1.1 [3.7] }decyl) cyclobutane; (2- exo, 3-exo) -bicyclo [2.2.1] heptane-2 , 3-bis (di-tert- butylphosphinomethyl) and (2-endo, 3-endo)- bicyclo [2.2.1] heptane-2 , 3-bis (di-tert- butylphosphinomethyl) . The bubble size produced by the invention may be small and therefore a large surface area is provided for interface mass transfer to take place. Furthermore, because the bubble size distribution is narrow with small deviation, the carbonylation reaction can be controlled.
All of the features described herein may be combined with any of the above aspects, in any combination unless such combinations are mutually exclusive.
An embodiment of the invention will now be described, by way of example only, with reference to the accompanying drawings, wherein:
Figure 1 is a schematic sectional side view of a prior art mixing apparatus ;
Figure 2 is a schematic sectional side view of a mixing apparatus according to the invention;
Figure 3 is a schematic sectional side view of a mixing apparatus according to the invention in use; and
Figure 4 is a further schematic sectional side view. of a mixing apparatus according to the invention in use.
Figure 1 shows a prior art mixing apparatus 10 in use in a vessel 12 containing a liquid 14. The vessel 12 has an inlet 16 through which a gas 18 is sparged into the liquid 14. The mixing apparatus 10 comprises a vertical elongate shaft 20 rotatable about a longitudinal axis 21 on which are fixedly mounted a first impeller 22 and a second impeller 24 in spaced apart relation. The first impeller 22 is mounted above the second impeller 24. Both the first and the second impellers 22,24 are 45° pitched blade turbines .
In use, said impellers must rotate at the same speed. The first impeller 22 causes incoming gas bubbles 26 to flow in a both an axial and radial direction. The axial component of the flow creates momentum, which along with buoyancy, prevents the second impeller 24 from operating effectively. The momentum and buoyancy is only overcome by increasing the speed of the impellers 22, 24. This increase in speed causes full dispersion of the gas 18 in the liquid 14 as shown in Figure 1 by the lines A. Nonuniform dispersion of the liquid 14 in the gas 18 is undesirable because the mixing process cannot be controlled.
Figure 2 shows a mixing apparatus 100 according to the present invention. The mixing apparatus 100 comprises a vertical elongate shaft 120 rotatable about a longitudinal axis 121 on which are fixedly mounted a first impeller 122 and a second impeller 124 in a spaced apart arrangement. Both the first and the second impeller 122, 124 comprise a number of hydrofoil blades 125. Each impeller 122,124 comprises four radially extending blades 125 fixedly mounted on the shaft 120 for co-operating rotation about the longitudinal axis of the shaft, in use. Each blade 125 on each impeller 122,124 is a hydrofoil blade arranged so as to impel the surrounding fluid axially in the direction of the other impeller. The first or lower impeller 122 is thus an up-pumping impeller and the second or upper impeller 124 is a down-pumping impeller. Although only two blades 125 can be seen in the figure, it will be understood by a skilled person, that any number of blades may be used on each of the said impellers, for example, 3, 4 or even 6 blades. Particularly suitable commercially available impellers are those known as Maxflo™ W, A315, A320 or A340 impellers.
The first impeller 122 is mounted on the shaft 120 so that the concave face of the blades 125 face in an upward direction. The second impeller 124 is spaced along the shaft 120 and is mounted so that the concave face of the blades 125 face in a downwards direction. The distance between the first impeller 122 and the second impeller 124 is approximately the diameter of either of the said impellers 122, 124.
Figure 3 shows the mixing apparatus 100 in a cylindrical vessel 112. A gas inlet 116 is located in the bottom-wall 132 of the vessel 112 adjacent to the base 132. It will be appreciated that the vessel 112 can be of any suitable alternative configuration, for example, it may be a hopper. The mixing apparatus 100 is centrally suspended in the vessel 112.
Although only one mixing apparatus 100 is shown in Figure 3, it will be appreciated that any number of mixing apparatus 100 could be used in the chamber 112. For example, two, three, or four mixing apparatus 100 may be mounted in the chamber 112.
It will also be understood that any number of first or second impellers 122,124 may be mounted on the shaft 120 and in keeping with the object of the invention. For example, the arrangement 200 shown in Figure 4, wherein a series of first impellers 222 and a series of second impellers 224 are mounted on the shaft 220. Any number of impellers 222,224 may be provided on the shaft 220.
An alternative configuration would comprise pairs of impellers mounted on the shaft. Each pair would comprise a first impeller and a second impeller. There may be a number of pairs of impellers on any given shaft, for example, two, three, or four pairs. In such an arrangement, the fluid, for example, gas, may be introduced into the chamber through the base or the side wall thereof, being directed under and towards the first impeller.
The first or the second impeller may be driven by a separate drive means so that the rotational speed of, for example, the first impeller, may be different to the rotational speed of the said other impeller.
The diameter of the first and second impellers may not necessarily be the same in any one of the embodiments shown. Further, the optimum distance between two impellers is dependent upon the geometry of the vessel and the diameter of said impellers.
In use, as in the illustrated carbonylation reaction, the vessel 112,212 is filled with fluid 114,214. A gas 118,218 is then directed into the vessel 112,212 via gas inlet 116,216. The shaft 120,220 is rotated by a suitable drive means (not shown) , so as to cause the first impeller 122,222 and the second impeller 124,224 to rotate about the longitudinal axis 121,221 of the shaft 120,220 in a liquid 114. The gas 118,218 enters the vessel 112,212 as large bubbles 150,215. Rotation of the first impeller 122,222 causes the large bubbles 150,215 to move in an axial direction towards the blades 125,225. The large bubbles 150,250 impact on the blades 125,225 and are broken up into a number of small bubbles 152,252 in the region of high turbulent energy dissipation. Small bubbles follow the liquid flow path which is initially axial then radial .
The second impeller 124,224 causes axial flow in a downwards direction towards the first impeller 122,222. Due to the opposing axial flow paths created by said impellers, a central zone 160,260, or high turbulent energy dissipation zone, is established. The central zone 160,260 comprises an area of comparatively uniform high turbulent energy dissipation with high interfacial area to allow reaction between reactants in the liquid 114,214 and in reactants in the gas 118,218. Further, because the turbulent energy dissipation in the central zone 160,260 is maintained without much variation, a narrow size distribution of small bubbles is produced. Such a narrow size distribution enables the reactor performance to be predicted and controlled.
The mixing apparatus 100,200 is particularly suited to carbonylation processes.
Table 1 gives an example of resultant bubble size for a dual opposed Maxflo impeller system operating at various speeds, and at 4.2mm/sec. The bubble size was determined using a typical image capture camera.
Figure imgf000021_0001
Table 1
It is a distinct advantage to be able to control the reaction occurring between two fluids, particularly a liquid and a gas. It is also especially favorable to be able to promote effective and efficient mixing and interphase mass transfer between at least two fluids.
When applied to industrial processes, such advantages are of high commercial value.
The reader's attention is directed to all papers and documents which are filed concurrently with or previous to this specification in connection with this application and which are open to public inspection with this specification, and the contents of all such papers and documents are incorporated herein by reference.
All of the features disclosed in this specification (including any accompanying claims, abstract and drawings) , and/or all of the steps of any method or process so disclosed, may be combined in any combination, except combinations where at least some of such features and/or steps are mutually exclusive.
Each feature disclosed in this specification (including any accompanying claims, abstract and drawings) , may be replaced by alternative features serving the same, equivalent or similar purpose, unless expressly stated otherwise. Thus, unless expressly stated otherwise, each feature disclosed is one example only of a generic series of equivalent or similar features.
The invention is not restricted to the details of the foregoing embodiment (s) . The invention extends to any- novel one, or any novel combination, of the features disclosed in this specification (including any accompanying claims, abstract and drawings) , or to any novel one, or any novel combination, of the steps of any method or process so disclosed.

Claims

1. A mixing apparatus for mixing at least two fluids, the mixing apparatus comprising a shaft rotatable about its longitudinal axis, a first and a second radially extending impeller mounted on the shaft and respectively axially spaced apart, characterised in that the first impeller comprises a plurality of curved blades operable to move said fluids in an axial direction towards the second impeller, and the second impeller comprises a plurality of curved blades operable to move said fluids in an axial direction towards the first impeller.
2. A mixing apparatus as claimed in claim 1, characterised in that the blades on each impeller are inward pumping into the space between the impellers.
3. A mixing apparatus as claimed in claim 1 or 2, characterised in that the at least two fluids comprise a liquid and a gas.
4. A mixing apparatus as claimed in any one of the preceding claims, characterised in that the first impeller and the second impeller each comprise two or more curved blades .
5. A mixing apparatus as claimed in any one of the preceding claims, characterised in that the diameter of the first impeller is the same as the diameter of the second impeller.
6. A mixing apparatus as claimed in any one of the preceding claims, characterised in that the axial distance between the first impeller and the second impeller is at least one impeller diameter apart.
7. A mixing apparatus as claimed in any one of the preceding claims, characterised in that said impellers operate at a power number substantially 1.75.
8. A mixing apparatus as claimed in any one of the preceding claims, characterised in that the specific power used when the first impeller and the second impeller rotate is substantially between lOOW/m3 to 800W/m3.
9. A mixing apparatus as claimed in any one of the preceding claims, characterised in that when dual opposed Maxflo impellers are used, the arithmetic mean size (dio)' is substantially between 250μm to 550μm and the surface volume mean diameter (d32) is substantially between 400μm to 750μm.
10. A mixing apparatus as claimed in any one of the preceding claims, characterised in that when BT-6 type impellers are used, the di0 is substantially between 250μm to 1500μm.
11. A mixing apparatus as claimed in claim 10, characterised in that when operating at substantially 765rpm, the dio is substantially 378μm, and the d32 is substantially 445μm.
12. A mixing apparatus as claimed in any one of the preceding claims, characterised in that the sparged gas rate is substantially between 0.05 to 1.0 m3/s.
13. A mixing apparatus as claimed in claim 12, characterised in that the sparged gas rate is substantially 0.13m3/s at an impeller speed of substantially 50rpm to 200rpm.
14. A mixing apparatus as claimed in any one of the preceding claims, characterised in that a critical dispersion speed in a vessel having a diameter of substantially between 2 to 5m, is substantially between 10 to 20rpm.
15. A chemical reaction system comprising a liquid phase and a mixing apparatus according to the first aspect of the invention for mixing a fluid into the liquid phase.
16. A chemical reaction system as claimed in claim 15, characterised in that the liquid phase comprises at least one liquid phase reactant for reacting with a gas introduced into the liquid phase, as well as at least one liquid phase reaction product.
17. A chemical reaction system as claimed in claims 15 or 16, characterised in that the liquid phase comprises a catalyst system.
18. A chemical reaction system as claimed in any one of claims 15 to 17, characterised in that the reaction system is a carbonylation process comprising carbonylating an ethylenically unsaturated compound with carbon monoxide in the presence of a source of hydroxyl groups, and a catalyst system comprising (a) a bidentate phosphine, arsine or stibine ligand, and (b) a catalytic metal selected from a group 8, 9 or 10 metal or a compound thereof .
19. A mixing apparatus substantially as hereinbefore described with reference to any one of the accompanying drawings .
PCT/GB2007/001524 2006-05-10 2007-04-25 Mixing apparatus Ceased WO2007129023A1 (en)

Priority Applications (15)

Application Number Priority Date Filing Date Title
EP07732561A EP2018218B1 (en) 2006-05-10 2007-04-25 Mixing apparatus for mixing at least two fluids, and its use
ES07732561T ES2375233T3 (en) 2006-05-10 2007-04-25 MIXING DEVICE FOR MIXING AT LEAST TWO FLUIDS, AND ITS USE.
KR1020087027240A KR101431600B1 (en) 2006-05-10 2007-04-25 Mixing device
AT07732561T ATE534456T1 (en) 2006-05-10 2007-04-25 MIXING DEVICE FOR MIXING AT LEAST TWO FLUIDS, AND USE THEREOF
AU2007246957A AU2007246957B2 (en) 2006-05-10 2007-04-25 Mixing apparatus
US12/300,072 US20090208390A1 (en) 2006-05-10 2007-04-25 Mixing apparatus
CA2650969A CA2650969C (en) 2006-05-10 2007-04-25 Mixing apparatus
CN2007800167915A CN101443100B (en) 2006-05-10 2007-04-25 Mixing apparatus
EA200870518A EA015826B1 (en) 2006-05-10 2007-04-25 Mixing apparatus
BRPI0711430-3A BRPI0711430A2 (en) 2006-05-10 2007-04-25 mixing apparatus for mixing at least two fluids, and, chemical reaction system
JP2009508450A JP5490528B2 (en) 2006-05-10 2007-04-25 Mixing equipment
MX2008014170A MX2008014170A (en) 2006-05-10 2007-04-25 Mixing apparatus.
PL07732561T PL2018218T3 (en) 2006-05-10 2007-04-25 Mixing apparatus for mixing at least two fluids, and its use
NO20084866A NO20084866L (en) 2006-05-10 2008-11-19 mixing device
US13/763,393 US9138694B2 (en) 2006-05-10 2013-02-08 Mixing apparatus

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB0609219A GB2437930A (en) 2006-05-10 2006-05-10 Mixing apparatus
GB0609219.1 2006-05-10

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US13/763,393 Continuation US9138694B2 (en) 2006-05-10 2013-02-08 Mixing apparatus

Publications (1)

Publication Number Publication Date
WO2007129023A1 true WO2007129023A1 (en) 2007-11-15

Family

ID=36637204

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB2007/001524 Ceased WO2007129023A1 (en) 2006-05-10 2007-04-25 Mixing apparatus

Country Status (20)

Country Link
US (2) US20090208390A1 (en)
EP (1) EP2018218B1 (en)
JP (2) JP5490528B2 (en)
KR (1) KR101431600B1 (en)
CN (1) CN101443100B (en)
AT (1) ATE534456T1 (en)
AU (1) AU2007246957B2 (en)
BR (1) BRPI0711430A2 (en)
CA (1) CA2650969C (en)
EA (1) EA015826B1 (en)
ES (1) ES2375233T3 (en)
GB (1) GB2437930A (en)
MX (1) MX2008014170A (en)
MY (1) MY149061A (en)
NO (1) NO20084866L (en)
PL (1) PL2018218T3 (en)
SG (1) SG174060A1 (en)
TW (1) TWI429481B (en)
WO (1) WO2007129023A1 (en)
ZA (1) ZA200809066B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9670446B2 (en) 2009-02-09 2017-06-06 Lonza Biologics Plc Bioreactor for the cultivation of mammalian cells

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103651237B (en) * 2012-09-05 2016-12-21 曾进辉 A kind of return stirring mechanism and micro-bubble generator
JP6159577B2 (en) * 2013-05-24 2017-07-05 佐竹化学機械工業株式会社 Gas-liquid stirring blade
EP3165279B1 (en) * 2014-07-01 2020-08-05 Satake Chemical Equipment Mfg Ltd. Reciprocating stirrer device with microbubble-generating unit
KR102256402B1 (en) * 2018-10-15 2021-05-25 한화솔루션 주식회사 Batch reactor
SG11202112086TA (en) * 2019-05-03 2021-11-29 Philadelphia Mixing Solutions Ltd Reaction mixer
CN112479815A (en) * 2019-09-12 2021-03-12 南京延长反应技术研究院有限公司 A kind of reaction system and process for preparing butanol and octanol based on micro-interface enhanced carbonylation of propylene
JP7555059B2 (en) * 2020-06-02 2024-09-24 株式会社フォーティー科研 Bubble generating device and bubble generating method
WO2024252434A1 (en) * 2023-06-06 2024-12-12 Aquasoil S.R.L. Process and system for degrading a chemical compound in a liquid stream
CN116983871B (en) * 2023-09-20 2023-12-01 常州登达适医疗科技有限公司 Gas-liquid mixing and stirring device and stirring method thereof
CN117160276A (en) * 2023-10-18 2023-12-05 河络新图生物科技(上海)有限公司 Rotor for biological reaction

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH332926A (en) * 1955-09-22 1958-09-30 Kreuzer Emil Agitator
US4004786A (en) * 1975-05-16 1977-01-25 Barnard & Leas Manufacturing Co. Inc. Stirring device
US4401645A (en) * 1979-02-28 1983-08-30 Joy Manufacturing Company Lime slaking method
DE4421478A1 (en) * 1994-06-20 1995-12-21 Netzsch Erich Holding Propeller mill to mix, break up, and mill material mixts.
DE20306404U1 (en) * 2003-04-24 2003-06-26 Mavag Verfahrenstechnik Ag Neu Single-shaft twin propeller mixer comprises rotating shaft with two or more mixer blades on float bearing, minimizing mechanical loads on float bearing
US20040042942A1 (en) 2002-09-03 2004-03-04 Siccardi Edward S. Continually stirred reactor system

Family Cites Families (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3330818A (en) * 1963-02-18 1967-07-11 Monsanto Co Elimination of fouling in ziegler polymerizations
US3252689A (en) * 1964-06-10 1966-05-24 Diamond Alkali Co Method and apparatus for mixing and distributing liquids
US4013273A (en) * 1973-12-19 1977-03-22 The International Nickel Company, Inc. Method of, and mixer for intimate blending of fine, dry, particulate solid materials with moist wet or slurried particulate solid materials
DE3175174D1 (en) 1981-01-06 1986-09-25 Shell Int Research Process for the carbonylation of olefins
US4468130A (en) * 1981-11-04 1984-08-28 General Signal Corp. Mixing apparatus
CA1231346A (en) 1982-09-30 1988-01-12 Eit Drent Process for the carbonylation of olefinically unsaturated compounds with a palladium catalyst
US4594228A (en) * 1984-05-21 1986-06-10 The Standard Oil Company Mixing apparatus
JPS6245330A (en) * 1985-08-23 1987-02-27 Tokushu Kika Kogyo Kk Shearing type stirrer
GB8531624D0 (en) 1985-12-23 1986-02-05 Shell Int Research Carbonylation of ethylenically unsaturated compounds
GB8605034D0 (en) 1986-02-28 1986-04-09 Shell Int Research Carbonylation of compounds
KR880007426A (en) 1986-12-24 1988-08-27 오노 알버어스 Carbonylation Method of Olefinic Unsaturated Compound Using Palladium Catalyst
GB8705699D0 (en) 1987-03-11 1987-04-15 Shell Int Research Carbonylation of olefinically unsaturated compounds
US5145255A (en) * 1987-05-19 1992-09-08 Mitsubishi Jukogoyo Kabushiki Kaisha Stirring apparatus and stirring tower type apparatus for polmerization reactions
US5158921A (en) 1989-03-03 1992-10-27 Shell Oil Company Carbonylation catalyst and process
US4934828A (en) * 1989-06-07 1990-06-19 Ciba-Geigy Corporation Apparatus for mixing viscous materials
CA2034971A1 (en) 1990-02-05 1991-08-06 Eit Drent Carbonylation catalyst system
CA2055628A1 (en) 1990-12-03 1992-06-04 Eit Drent Carbonylation process and catalyst composition
ES2088082T3 (en) 1991-01-15 1996-08-01 Shell Int Research OLEPHINE CARBONILATION.
DE69204691T2 (en) 1991-01-15 1996-04-11 Shell Int Research Process for carbonylation of olefin.
KR100230139B1 (en) 1991-02-15 1999-11-15 오노 알버어스 Carbonylation catalyst system
JPH078776A (en) 1993-04-30 1995-01-13 Kansai Kagaku Kikai Seisaku Kk Stirring blade
JPH0810597A (en) 1994-06-29 1996-01-16 Fuji Electric Co Ltd Device for mixing and transferring gas and liquid
JP3584582B2 (en) 1995-11-28 2004-11-04 富士ゼロックス株式会社 Powder mixing apparatus and toner manufacturing method
JP3210877B2 (en) 1997-02-28 2001-09-25 中国塗料株式会社 Stirrer and tank with stirrer
US5972661A (en) * 1998-09-28 1999-10-26 Penn State Research Foundation Mixing systems
GB9918229D0 (en) 1999-08-04 1999-10-06 Ici Plc Improvements relating to metal-compound catalysed processes
MY127093A (en) * 2000-05-17 2006-11-30 Lucite Int Uk Ltd Bidentate ligands useful in catalyst systems
US6796707B2 (en) * 2002-02-26 2004-09-28 Spx Corporation Dual direction mixing impeller and method
JP4112908B2 (en) * 2002-06-07 2008-07-02 株式会社日立プラントテクノロジー Continuous stirring device and continuous polycondensation method of polycondensation resin
GB0228018D0 (en) 2002-11-30 2003-01-08 Lucite Int Uk Ltd Carbonylation of ester
GB0218613D0 (en) * 2002-08-10 2002-09-18 Lucite Int Uk Ltd Process for the carbonylation of ethylenically unsaturated compounds
TWI301481B (en) * 2002-08-10 2008-10-01 Lucite Int Uk Ltd A catalyst system
AU2003269119B2 (en) * 2002-09-12 2009-06-18 Lucite International Uk Limited A catalyst system comprising a metallocene ligand
WO2005003070A1 (en) 2003-07-03 2005-01-13 Lucite International Uk Limited Process for the hydroformylation of ethylenically unsaturated compounds
GB0403592D0 (en) * 2004-02-18 2004-03-24 Lucite Int Uk Ltd A catalyst system
GB0411951D0 (en) * 2004-05-28 2004-06-30 Lucite Int Uk Ltd Carbonylation of ester
US7168849B2 (en) * 2005-02-04 2007-01-30 Spx Corporation Agitation apparatus and method for dry solids addition to fluid

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH332926A (en) * 1955-09-22 1958-09-30 Kreuzer Emil Agitator
US4004786A (en) * 1975-05-16 1977-01-25 Barnard & Leas Manufacturing Co. Inc. Stirring device
US4401645A (en) * 1979-02-28 1983-08-30 Joy Manufacturing Company Lime slaking method
DE4421478A1 (en) * 1994-06-20 1995-12-21 Netzsch Erich Holding Propeller mill to mix, break up, and mill material mixts.
US20040042942A1 (en) 2002-09-03 2004-03-04 Siccardi Edward S. Continually stirred reactor system
DE20306404U1 (en) * 2003-04-24 2003-06-26 Mavag Verfahrenstechnik Ag Neu Single-shaft twin propeller mixer comprises rotating shaft with two or more mixer blades on float bearing, minimizing mechanical loads on float bearing

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9670446B2 (en) 2009-02-09 2017-06-06 Lonza Biologics Plc Bioreactor for the cultivation of mammalian cells
US9783771B2 (en) 2009-02-09 2017-10-10 Lonza Biologics Plc Three bioreactor system for the cultivation of mammalian cells
US10179898B2 (en) 2009-02-09 2019-01-15 Lonza Biologics Plc Bioreactor for the cultivation of mammalian cells
EP2393912B1 (en) * 2009-02-09 2020-04-29 Lonza Biologics plc. Bioreactor for the cultivation of mammalian cells
US10883076B2 (en) 2009-02-09 2021-01-05 Lonza Biologies PLC Bioreactor for the cultivation of mammalian cells

Also Published As

Publication number Publication date
EA015826B1 (en) 2011-12-30
JP5490528B2 (en) 2014-05-14
BRPI0711430A2 (en) 2011-11-16
EA200870518A1 (en) 2009-04-28
MY149061A (en) 2013-07-15
JP2009536095A (en) 2009-10-08
US20130150618A1 (en) 2013-06-13
AU2007246957B2 (en) 2012-03-08
ES2375233T3 (en) 2012-02-28
KR20090016552A (en) 2009-02-16
CN101443100B (en) 2012-09-05
US20090208390A1 (en) 2009-08-20
TWI429481B (en) 2014-03-11
ATE534456T1 (en) 2011-12-15
ZA200809066B (en) 2009-08-26
CN101443100A (en) 2009-05-27
EP2018218B1 (en) 2011-11-23
SG174060A1 (en) 2011-09-29
GB2437930A (en) 2007-11-14
KR101431600B1 (en) 2014-08-19
CA2650969A1 (en) 2007-11-15
PL2018218T3 (en) 2012-04-30
NO20084866L (en) 2008-11-19
GB0609219D0 (en) 2006-06-21
CA2650969C (en) 2014-10-28
MX2008014170A (en) 2008-11-18
JP2013121590A (en) 2013-06-20
EP2018218A1 (en) 2009-01-28
TW200810828A (en) 2008-03-01
AU2007246957A1 (en) 2007-11-15
US9138694B2 (en) 2015-09-22

Similar Documents

Publication Publication Date Title
US9138694B2 (en) Mixing apparatus
RU207190U1 (en) DEVICE FOR ADVANCED MICRO-SURFACE HYDRATION REACTION
Patwardhan et al. Design of gas-inducing reactors
CN111686665A (en) Micro-interface enhanced reaction system
Poncin et al. Hydrodynamics and volumetric gas–liquid mass transfer coefficient of a stirred vessel equipped with a gas-inducing impeller
Suarez et al. Stirred tank membrane emulsification using flat metallic membranes: A dimensional analysis
US8192695B2 (en) Reactor apparatus having reduced back mixing
Luo et al. Flow behavior and size characteristics of microbubble swarm in a HiGee-aided fixed bed reactor with different packed structures
Lueske et al. Power Draw and Gas‐Liquid Mass Transfer Characteristics of a Stirred‐Tank Reactor with Draft Tube Configuration
Wang et al. Deep deoxidation of water in a miniaturized annular rotating device: Experimental investigation and machine learning modeling
JP7341389B2 (en) Reactor and chemical treatment method using the reactor
JP3238406U (en) Micro-interface enhanced reaction system
US10603643B2 (en) Process and device for dispersing gas in a liquid
JP7105445B2 (en) Reactor
Leng et al. Industrial mixing technology
GB2541283A (en) Apparatus
JP7299591B2 (en) Method of operating the reactor
Kausley et al. Process intensification opportunities in multiphase stirred tank reactors
Yatomi et al. Mass transfer characteristics by surface aeration of large paddle impeller: application to a polymerization reactor with liquid level change
GB2221166A (en) Generation of fine bubbles
Majumder Yeah, welcome to massive open online course on Chemical Process Intensification. Here we start the model 8 regarding interfacial area based process intensification.

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 07732561

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2007246957

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: DZP2008000634

Country of ref document: DZ

WWE Wipo information: entry into national phase

Ref document number: 2009508450

Country of ref document: JP

Ref document number: 2007732561

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2650969

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: MX/a/2008/014170

Country of ref document: MX

WWE Wipo information: entry into national phase

Ref document number: 1020087027240

Country of ref document: KR

WWE Wipo information: entry into national phase

Ref document number: 200780016791.5

Country of ref document: CN

Ref document number: 6087/CHENP/2008

Country of ref document: IN

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2007246957

Country of ref document: AU

Date of ref document: 20070425

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 200870518

Country of ref document: EA

WWE Wipo information: entry into national phase

Ref document number: 12300072

Country of ref document: US

ENP Entry into the national phase

Ref document number: PI0711430

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20081107