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WO2001041919A1 - Systeme d'agitation de turbine a tube d'aspiration destinee au melange de gaz et de liquide dans un reacteur agite - Google Patents

Systeme d'agitation de turbine a tube d'aspiration destinee au melange de gaz et de liquide dans un reacteur agite Download PDF

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Publication number
WO2001041919A1
WO2001041919A1 PCT/US2000/032586 US0032586W WO0141919A1 WO 2001041919 A1 WO2001041919 A1 WO 2001041919A1 US 0032586 W US0032586 W US 0032586W WO 0141919 A1 WO0141919 A1 WO 0141919A1
Authority
WO
WIPO (PCT)
Prior art keywords
draft tube
impeller
shaft
axial
gas
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/US2000/032586
Other languages
English (en)
Inventor
Kishore Kar
Luciano Piras
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.)
Inca International SpA
Original Assignee
Inca International SpA
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 Inca International SpA filed Critical Inca International SpA
Priority to AU19356/01A priority Critical patent/AU1935601A/en
Publication of WO2001041919A1 publication Critical patent/WO2001041919A1/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
    • B01J19/20—Stationary reactors having moving elements inside in the form of helices, e.g. screw reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
    • B01F23/2334—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements provided with stationary guiding means surrounding at least partially the stirrer
    • B01F23/23341—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements provided with stationary guiding means surrounding at least partially the stirrer with tubes surrounding the stirrer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/86—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis co-operating with deflectors or baffles fixed to the receptacle
    • B01F27/861—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis co-operating with deflectors or baffles fixed to the receptacle the baffles being of cylindrical shape, e.g. a mixing chamber surrounding the stirrer, the baffle being displaced axially to form an interior mixing chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/91—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with propellers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
    • B01J19/1875—Stationary reactors having moving elements inside resulting in a loop-type movement internally, i.e. the mixture circulating inside the vessel such that the upwards stream is separated physically from the downwards stream(s)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/15—Stirrers with tubes for guiding the material

Definitions

  • the present invention relates to an improved design for the agitation system in stirred tank reactors for gas-liquid reactions.
  • the present invention relates to a system which incorporates a draft tube, one or more axial impellers and one or more radial impellers.
  • the new agitation design offers improved contact between a liquid phase and a gaseous phase within the reactor.
  • STRs Stirred Tank Reactors
  • gas and liquid phases make intimate contact for mass transfer
  • chemical processes such as fermentation, hydrogenation, phosgenation, neutralization, chlorination, and organic oxidation.
  • the design of the STR has a significant effect on gas bubble dispersion, interfacial area ("a"), bubble surface transience, and the mass transfer coefficient "KL". These factors in turn effect the rate of conversion, selectivity and the yield of the reaction.
  • the design of the STR also has an impact on the power needed to run the impeller system at a given rate.
  • the present invention incorporates a draft tube along with both axial impeller and radial impellers.
  • the axial impeller(s) is (are) located inside the cylinder formed by the draft tube, while the radial impeller(s) is located below the cylinder formed by the draft tube.
  • the fluid flow and the mass transfer characteristics of such a system are superior to the conventional agitation system.
  • Figure 1 is a cross-sectional view of an apparatus which corresponds to the present invention.
  • Figure 2 is a graph of observed Kj_a vs. gas flow rate for three different agitation rates in a system having a draft tube.
  • Figure 3 is a graph of observed Kj ⁇ a vs. gas flow rate for three different agitation rates in a system not having a draft tube.
  • the present invention comprises a shaft 1 ; at least one axial impeller 2 attached to the shaft 1 , for moving fluid in a direction generally parallel to the shaft's axis 1 1 ; at least one radial impeller 3 attached to the shaft 1, for moving fluid in a direction generally perpendicular to the shaft's axis 1 1 ; and a draft tube 4 in the shape of a generally open cylinder.
  • the shaft 1 when the agitation system 5 is placed within a stirred tank reactor 10, the shaft 1 extends through the draft tube 4 and the one or more axial impellers 2 are located within the draft tube cylinder 4 and the one or more radial impellers 3 are located outside of the draft tube cylinder 4.
  • the stirred tank reactor 10 with the agitation system 5 should be arranged in a vertical fashion as presented in Figure 1 , such that the radial impellers 3 are located below the draft tube 4. Also as shown in Figure 1, the entrance to the draft tube 4 is preferably beveled away from the shaft 1 , although this is not mandatory.
  • the axial impellers 2 act to move the reactor contents down through the draft tube 4 in a direction generally parallel to the shaft's axis 1 1.
  • Axial impellers are generally known in the art and any such impellers may be used in the present invention.
  • a double helix impeller such as the one depicted in U.S. 5,108,662, or an airfoil blade impeller such as the one depicted in U.S. Patent 4,231,974 could be used in this invention.
  • Other suitable axial impellers include Pitch Blade Turbine, high efficiency impellers (such as model A-310 from Lightnin Mixing Co, HE-3 from Chemineer, Inc.
  • axial impellers used in general depends on the viscosity of the working media. The more viscous the working media the more axial impellers are warranted. It is contemplated that the invention may comprise from 1 to several axial impellers 2, but it is preferred that there be two.
  • the radial impellers 3 act to move the reactor contents away ,rom the shaft 1, and (as the radial impellers 3 are located below the draft tube 4) outside the draft tube 4.
  • the center line of the radial impeller(s) should be far enough below the end of the draft tube to avoid substantial interference. This is typically in a range of from about 1/8 the distance of the radial impeller's diameter to about 7/8 of the radial impeller's diameter, with about 2/3 being most preferred.
  • Radial impellers are also generally known in the art, and any design may be used in the current invention.
  • radial impellers which are suited for use in the present invention include flat blade impellers, Rushton Impellers, Concave Disk Turbine (Smith turbine) SCABA (SRGT) impellers and model BT-6 from Chemineer, Inc.
  • the optimum number of radial impellers to be used is dependent upon the ratio of the liquid height to the tank diameter. In most cases a single radial impeller will be used in the current invention, but in some reactors, such as tall fermenters, multiple radial impellers may be used.
  • draft tubes and their modifications are also well known in the art, and those teachings are generally applicable to this invention.
  • the draft tube can be slotted to provide for return of liquid to the center of the draft tube if the level of liquid for some reason does not exceed the top of the draft tube.
  • the use of vertical baffles on the inner surface of the draft tube can be advantageously used to redirect tangential flow to axial flow. If baffles are used in the draft tube it is preferred that they have a width of 0.8 to 0.1 of the draft tube inner diameter with a clearance of 0.016 to 0.021 of the draft tube inner diameter.
  • the use of a baffle to partially close of the bottom of the cylinder formed by the draft tube is shown, inter alia, in U.S. Patent 5,536,875 and may also be used in the present invention.
  • the draft tube 4 can optionally contain a conically flared portion 6, at the entrance end of the draft tube. It is believed that this section will aid in straightening the flow of the reactor contents.
  • the angle of the bevel should be between 30 and 60 degrees, with 45 degrees being most preferred.
  • the beveled edge should not be too long, such that it restricts flow around the top of the draft tube. It is preferred if the length of the beveled edge is from zero to about one fourth of the draft tube's inner diameter, with about 1/12 of the length being most preferred.
  • the present invention can be used with stirred tank reactors of any dimensions.
  • the draft tube can be held in the appropriate position using side structural braces which attach to the reactor wall, as is known in the art.
  • baffles can be optionally used, as is generally known in the art. If used, there are preferably four baffles spaced approximately 90 apart from each other.
  • the reactant gas can be brought into the tank by any apparatus known in the art. These include ring spargers and more preferably pipe or nozzle spargers.
  • a transient technique was used to determine the mass transfer coefficient.
  • This dynamic gassing out technique consists of sparging the reactor with pure nitrogen until all oxygen has been stripped from the working media. The sparge gas is then rapidly changed from nitrogen to oxygen. The transient oxygen concentration is then measured. These measurements can then be used to calculate the volumetric mass transfer coefficient (K.La) for the system.
  • Physical techniques such as this are applicable to a well mixed system and to small values of Kj ⁇ a due to the slow response time of dissolved oxygen probes. In general these physical techniques are applicable where Kj ⁇ a ⁇ 1/ ⁇ , where ⁇ is the dissolved oxygen probe response time.
  • An ASME dish bottom PLEXIGLASTM tank having a 0.45 m inner diameter (0.08m3) was used to conduct the gas-liquid mixing experiments.
  • the agitation system included two high- efficiency down-pumping axial impellers (model A-310 from Lightnin Mixers Ltd.), and one radial gas dispersing Rushton disk turbine (Lightnin R-100). The gas was sparged through a ring sparger located below the radial impeller. Deionized water was used as the working media.
  • the agitator speed and torque were measured by a proximity tachometer and load cell, respectively, while the concentration of dissolved oxygen in the water was measured with two oxygen sensors (Electrosense DO probes having a response time of 2 seconds for 95% saturation).
  • the agitation levels (gassed power of 0.26 -2.6 watt/kg) were sufficient to create uniform gas dispersion at a 0.012 - 0.046 m/s (i.e. 1-5 VVM) superficial gas velocity. All of the data was collected using a CAMILETM 2000 data acquisition system.
  • the K.La at different gas flow rates and shaft speeds (power) was first determined for the system without a draft tube.

Landscapes

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

Abstract

La présente invention concerne la conception de système d'agitation dans des réacteurs agités destinés à des réactions gaz-liquide. Plus précisément, cette invention concerne un système comportant un tube d'aspiration, une ou plusieurs turbines axiales et une ou plusieurs turbines radiales. Cette conception d'agitation permet d'obtenir un contact entre une phase liquide et une phase gazeuse à l'intérieur du réacteur.
PCT/US2000/032586 1999-12-10 2000-11-30 Systeme d'agitation de turbine a tube d'aspiration destinee au melange de gaz et de liquide dans un reacteur agite Ceased WO2001041919A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU19356/01A AU1935601A (en) 1999-12-10 2000-11-30 Impeller draft tube agitation system for gas-liquid mixing in a stirred tank reactor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US17005399P 1999-12-10 1999-12-10
US60/170,053 1999-12-10

Publications (1)

Publication Number Publication Date
WO2001041919A1 true WO2001041919A1 (fr) 2001-06-14

Family

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Family Applications (1)

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PCT/US2000/032586 Ceased WO2001041919A1 (fr) 1999-12-10 2000-11-30 Systeme d'agitation de turbine a tube d'aspiration destinee au melange de gaz et de liquide dans un reacteur agite

Country Status (3)

Country Link
AU (1) AU1935601A (fr)
TW (1) TW476661B (fr)
WO (1) WO2001041919A1 (fr)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010139470A1 (fr) 2009-06-05 2010-12-09 F. Hoffmann-La Roche Ag Agitateur combiné
US8197665B2 (en) 2007-06-12 2012-06-12 Solvay (Societe Anonyme) Aqueous composition containing a salt, manufacturing process and use
US8314205B2 (en) 2007-12-17 2012-11-20 Solvay (Societe Anonyme) Glycerol-based product, process for obtaining same and use thereof in the manufacturing of dichloropropanol
US8378130B2 (en) 2007-06-12 2013-02-19 Solvay (Societe Anonyme) Product containing epichlorohydrin, its preparation and its use in various applications
US8471074B2 (en) 2007-03-14 2013-06-25 Solvay (Societe Anonyme) Process for the manufacture of dichloropropanol
US8507643B2 (en) 2008-04-03 2013-08-13 Solvay S.A. Composition comprising glycerol, process for obtaining same and use thereof in the manufacture of dichloropropanol
US8536381B2 (en) 2008-09-12 2013-09-17 Solvay Sa Process for purifying hydrogen chloride
US20140093437A1 (en) * 2011-05-09 2014-04-03 Versalis S.P.A. Ammoximation reactor for cyclohexanone oxime production
US8715568B2 (en) 2007-10-02 2014-05-06 Solvay Sa Use of compositions containing silicon for improving the corrosion resistance of vessels
US8795536B2 (en) 2008-01-31 2014-08-05 Solvay (Societe Anonyme) Process for degrading organic substances in an aqueous composition
US9309209B2 (en) 2010-09-30 2016-04-12 Solvay Sa Derivative of epichlorohydrin of natural origin
EP2950915A4 (fr) * 2013-01-30 2016-10-19 Outotec Finland Oy Réacteur à cuve agitée
US9663427B2 (en) 2003-11-20 2017-05-30 Solvay (Société Anonyme) Process for producing epichlorohydrin
WO2020130539A1 (fr) * 2018-12-21 2020-06-25 한화솔루션 주식회사 Réacteur discontinu
EP4309776A4 (fr) * 2020-12-18 2024-11-06 Hanwha Solutions Corporation Appareil de réaction par lots

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111944663A (zh) * 2020-10-10 2020-11-17 漯河医学高等专科学校 一种用于生产甘草发酵饮料的发酵罐

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WO1997025133A1 (fr) * 1996-01-12 1997-07-17 Kvaerner Pulping Ab Appareil melangeur pour melanger de la liqueur noire avec des cendres de gaz de fumee
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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9663427B2 (en) 2003-11-20 2017-05-30 Solvay (Société Anonyme) Process for producing epichlorohydrin
US8471074B2 (en) 2007-03-14 2013-06-25 Solvay (Societe Anonyme) Process for the manufacture of dichloropropanol
US8197665B2 (en) 2007-06-12 2012-06-12 Solvay (Societe Anonyme) Aqueous composition containing a salt, manufacturing process and use
US8378130B2 (en) 2007-06-12 2013-02-19 Solvay (Societe Anonyme) Product containing epichlorohydrin, its preparation and its use in various applications
US8399692B2 (en) 2007-06-12 2013-03-19 Solvay (Societe Anonyme) Epichlorohydrin, manufacturing process and use
US8715568B2 (en) 2007-10-02 2014-05-06 Solvay Sa Use of compositions containing silicon for improving the corrosion resistance of vessels
US8314205B2 (en) 2007-12-17 2012-11-20 Solvay (Societe Anonyme) Glycerol-based product, process for obtaining same and use thereof in the manufacturing of dichloropropanol
US8795536B2 (en) 2008-01-31 2014-08-05 Solvay (Societe Anonyme) Process for degrading organic substances in an aqueous composition
US8507643B2 (en) 2008-04-03 2013-08-13 Solvay S.A. Composition comprising glycerol, process for obtaining same and use thereof in the manufacture of dichloropropanol
US8536381B2 (en) 2008-09-12 2013-09-17 Solvay Sa Process for purifying hydrogen chloride
WO2010139470A1 (fr) 2009-06-05 2010-12-09 F. Hoffmann-La Roche Ag Agitateur combiné
US11253826B2 (en) 2009-06-05 2022-02-22 Hoffmann-La Roche Inc. Combination stirrer
US10076731B2 (en) 2009-06-05 2018-09-18 Hoffman-La Roche Inc. Combination stirrer
US9309209B2 (en) 2010-09-30 2016-04-12 Solvay Sa Derivative of epichlorohydrin of natural origin
US10525429B2 (en) * 2011-05-09 2020-01-07 Versalis S.P.A. Ammoximation reactor for cyclohexanone oxime production
US20140093437A1 (en) * 2011-05-09 2014-04-03 Versalis S.P.A. Ammoximation reactor for cyclohexanone oxime production
AU2014211305B2 (en) * 2013-01-30 2016-10-20 Metso Outotec Finland Oy Stirred tank reactor
US9815033B2 (en) 2013-01-30 2017-11-14 Outotec (Finland) Oy Stirred tank reactor
EP2950915A4 (fr) * 2013-01-30 2016-10-19 Outotec Finland Oy Réacteur à cuve agitée
WO2020130539A1 (fr) * 2018-12-21 2020-06-25 한화솔루션 주식회사 Réacteur discontinu
JP2022514854A (ja) * 2018-12-21 2022-02-16 ハンワ ソリューションズ コーポレイション 回分式反応器
EP4309776A4 (fr) * 2020-12-18 2024-11-06 Hanwha Solutions Corporation Appareil de réaction par lots

Also Published As

Publication number Publication date
AU1935601A (en) 2001-06-18
TW476661B (en) 2002-02-21

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