US3833719A - Method and apparatus for mixing gas and liquid - Google Patents

Method and apparatus for mixing gas and liquid Download PDF

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Publication number
US3833719A
US3833719A US00226808A US22680872A US3833719A US 3833719 A US3833719 A US 3833719A US 00226808 A US00226808 A US 00226808A US 22680872 A US22680872 A US 22680872A US 3833719 A US3833719 A US 3833719A
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US
United States
Prior art keywords
liquid
gas
mixing
mixing zone
zone
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Expired - Lifetime
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US00226808A
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English (en)
Inventor
H Kuerten
R Sinn
O Nagel
R Platz
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BASF SE
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/311—Injector mixers in conduits or tubes through which the main component flows for mixing more than two components; Devices specially adapted for generating foam
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S261/00—Gas and liquid contact apparatus
    • Y10S261/72—Packing elements

Definitions

  • the invention relates to a method of mixing a gas with liquids in a tubular reactor by feeding the gas and the liquids to a mixing zone.
  • the invention also relates to an apparatus for carrying out this method. Rapid mixing is effected by feeding a stream of liquid to the mixing zone through one or more nozzles whose axes extend in the same direction as the axis of the mixing zone, the injected liquid having a velocity of from to 100 m./s., whilst a second stream of liquid of much lower velocity is introduced into the reactor inlet zone surrounding said nozzles.
  • the gas is fed to the mixing zone through one or more gas inlets located near the orifices of the liquid nozzles.
  • the mean cross-sectional area of the mixing zone bears a specific ratio to the cross-sectional area of the orifices of the liquid nozzles and the length of the mixing zone, bears a specific ratio to the hydraulic diameter thereof.
  • the method and apparatus are particularly suitable for carrying out reactions in which short residence times are desirable and the reaction products must not recontact the starting materials.
  • the present invention relates to a method and apparatus for mixing gas and liquid in a tubular reactor.
  • Such so-called ejector reactors are known, for example, as Venturi absorbers in the chemical industry. It is frequently necessary to connect the relatively small ejector reactors to a larger reaction chamber for continuation of the reaction, which reaction chamber may be in the form of a bubble column for example. In a large number of reactions between a gas and a liquid, however, the degree of gas/liquid mixing achieved in ejector reactors is inadequate for the provision of satisfactory yields and conversions.
  • spiral motion is imparted to the liquid flowing through the liquid nozzles before it emerges therefrom and/or spiral motion is imparted to the liquid/ gas mixture in the mixing zone.
  • Our new method is .generally suitable for mixing gases and liquids in processes either for effecting exchange of matter or for inducing a reaction between a gas and a liquid. It is particularly suitable for carrying out chemical reactions between gases and liquids where rapid and thorough mixing is required. It will be appreciated that the gas and liquid need not be pure substances but may also be any desired mixtures of substances. In the method of the invention it is also possible to mix a gas with two different liquids, one of which is injected through a nozzle while the other is fed to the reactor inlet zone surrounding the nozzle. The method of the invention is used to advantage in carrying out reactions between gas and liquid where the reaction product should not recontact the starting materials.
  • the present method may be used for the absorption of chlorine in water or the reaction of propylene with aqueous chlorine solution to form propylene chlorohydride.
  • the reaction conditions generally used for such processes for example catalyst, temperature and pressure, are not affected.
  • the greater mixing rate and improved thoroughness of mixing achieved in our method increase the reaction rate and thus improve the degree of conversion. It may therefore be advantageous to determine new optimum process parameters such as average residence time, temperature, pressure and amount of catalyst used, since the optimum values hitherto found in an industrial process may now no longer apply due to the higher reaction rate obtained in our method.
  • the method is advantageously used in the oxidation of organic and inorganic compounds with oxygen or oxygen-containing gases such as air, for example the oxidation of sodium sulfite in aqueous solution with air to form sodium sulfate.
  • the method of the invention is also advantageous for carrying our processes for effecting the transfer of material, for example the absorption of chlorine in water or the absorption of phosgene in organic solvents such as methylene chloride.
  • a preferably relatively small stream of liquid is injected through a nozzle at a velocity of from 5 to m./s. and preferably from 10 to 30 m./s. Whilst a second, preferably relatively large stream of liquid, is fed to the reactor inlet zone surrounding the nozzles at a considerably lower velocity than that of the injected liquid.
  • the ratio of injected liquid to the liquid fed to the said inlet zone is from 1:1 to 1:50 and preferably from 1:1 to 1:10.
  • the velocity of the liquid fed to said inlet zone is from 0.1 to 20 m./s. and preferably from 0.5 to 5 m./s.
  • the feed of liquid to the reactor inlet zone surrounding the nozzles may be elfected through one or more feed lines and the actual number of such feed lines is not critical.
  • the average cross-sectional area of the mixing zone should be from 5 to 500 times and preferably from to 100 times as large as the cross-sectional area of the liquid nozzle orifice or the sum of the cross-sectional areas of the liquid nozzle orifices, and the length of the mixing zone should be from 2 to 30 times as great as its hydraulic diameter.
  • the length and the hydraulic diameter of the inlet zone may be varied within wide limits.
  • the mixing zone generally has a constant cross-sectional or a crosssection which increases in the direction of flow, and. it may vary in design. In general, a cylindrical tube or alternatively a mixing tube having a short cylindrical neck followed by a conically diverging tube is used.
  • the inlet zone may also vary in design, although it generally takes the form of a cylindrical tube.
  • hydraulic diameter of a zone we mean the diameter of a cylindrical tube which has the same length as the zone in question and shows the same pressure loss when fluid is passed therethrough at the same rate.
  • a single liquid nozzle or a plurality of liquid nozzles may be used. Where a plurality of liquid nozzles is used, these may be arranged in a circle or in one or more close groups.
  • the gas is also fed through one or more, for example from 2 to 10, gas nozzles, the number of gas nozzles and the number of liquid nozzles being the same or different.
  • the gas is generally introduced in the proximity of the orifices of the liquid nozzles.
  • the nozzle orifices may be in the form of, say, round holes, slots or even annular gaps.
  • the gas generally emerges from the nozzle(s) in the same direction as the jet(s) of liquid and the gas velocity is convenient- 1y not higher than that of the jet(s) of liquid.
  • the velocity of the injected gas is from 5 to 50 m./s.
  • the gas and injected liquid are introduced through a two-component nozzle, the liquid being fed through the central orifice of the nozzle whilst the gas flows through the annular gap coaxially surrounding the said central orifice.
  • spiral motion is imparted to the injected liquid before it leaves the nozzle and/or spiral motion is imparted to the liquid/gas mixture in the mixing zone.
  • Spiral motion may be imparted to the injected liquid for example by placing a twist guide in the form of a single-pitch or multiplepitch screw in the path of the liquid upstream of the nozzle outlet or by arranging for the liquid to flow into the feed line of the nozzle tangentially.
  • Spiral motion may be imparted to the liquid/gas mixture in the mixing zone for example by imparting a twist to the slow outer stream also, for example by providing a rifled inlet to said mixing zone. It is particularly advantageous to create a back pressure at the end of the mixing zone.
  • This may be achieved, for example, by connecting a sufliciently high bubble column to the outlet of the mixing zone.
  • an energy-consuming system in the form of battle plates or centrifugal separators may be placed downstream of the mixing zone.
  • Another method of creating a back-pressure is to insert a pressure-holding valve downstream of the mixing zone.
  • the mixing zones are arranged vertically, the gas and liquids being caused to flow upwardly therethrough.
  • the gas and liquid may be caused to flow downwardly through vertical mixing zones or the mixing zones may be disposed horizontally or in an inclined position, as desired.
  • the invention is further described with reference to nozzle outlet by 3, the liquid and gas nozzle inlets by 4 and '5 respectively, whilst the reference numeral. .6 -designates the liquid inlet to the inlet zone 7.
  • the transition from inlet zone to mixing zone is conveniently gradual in order to prevent the liquid flowing from the inlet zone to the mixing zone from detaching itself from the walls of these zones.
  • FIG. 2 illustrates a combination of the jet reactor with baffle plate 8 disposed downstream; of the mixing zone and the use of a twist guide in the path of the injected liquid.
  • FIG. 3 illustrates a combination of the jet reactor with a conventional bubble column 10 having a gas outlet 11 and liquid outlet 12.
  • the pet reactor serves as the gassing device for the bubble column.
  • EXAMPLE 1 The reaction was carried out using a tubular reactor having a diameter of 20 mm. (see FIG. 1). The length of the mixing zone was 150 mm. and the diameter of the liquid nozzle was 5 mm. The liquid nozzle was coaxially surrounded by an annular gas nozzle.
  • the liquid passed through the liquid nozzle at a velocity of 20 m./s. consisted of 1.4 m. /hr. of an aqueous sodium sulfite solution containing 600 moles/m. of sodium sulfite and 0.27 mole/m. of cobalt sulfate as catalyst.
  • the reaction temperature was 20 C. and the pH was adjusted to 9.2 m. /hr. of air (STP) were passed through the annular nozzle.
  • STP 9.2 m. /hr. of air
  • a futher 2.0 m. /hr. of aqueous sodium sulfite solution of the above concentration were passed to the inlet zone through a separate inlet.
  • the slow stream of liquid had a velocity of 2.2 m./s.
  • the conversion based on atmospheric oxygen, was 52%.
  • EXAMPLE 2 EXAMPLE 3 The reaction was carried out as described in the first paragraph of Example 1, a bafiie plate having been placed at a distance of 20 mm. from the outlet of the mixing zone. The conversion of sulfite to sulfate was 80%.
  • EXAMPLE 4 The reaction was carried out using a tubular reactor having a diameter of 20 mm. The length of the mixing zone was 200 mm. and the diameter of the liquid nozzle was 3 mm. The liquid nozzle was coaxially surrounded by an annular gas nozzle.
  • a method of mixing a gas with liquids in a tubular reactor by feeding the gas and liquids to a mixing zone, wherein a stream of liquid is fed to a mixing zone through one or more liquid nozzles whose axes extend in the same direction as the axis of the mixing zone, the injected liquid having a velocity of from 5 to 100 m./s., while a second stream of liquid is introduced at a velocity in the range of 0.1 to 20 m./s.
  • the gas being fed to the mixing zone through one or more gas inlets located near the orifices of the liquid nozzles and the mean cross-sectional area of the mixing zone being from 5 to 500 times as large as the cross-sectional areas of the orifices of said liquid nozzles, the ratio of said injected liquid to said liquid of said second stream being in the range of 1:1 to 1:50, and the length of the mixing zone is from 2 to 30 times as great as its hydraulic diameter.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
US00226808A 1971-02-19 1972-02-16 Method and apparatus for mixing gas and liquid Expired - Lifetime US3833719A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE19712107960 DE2107960A1 (de) 1971-02-19 1971-02-19 Verfahren und Vorrichtung zum Vermischen eines Gases und einer Flüssigkeit

Publications (1)

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US3833719A true US3833719A (en) 1974-09-03

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US00226808A Expired - Lifetime US3833719A (en) 1971-02-19 1972-02-16 Method and apparatus for mixing gas and liquid

Country Status (8)

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US (1) US3833719A (de)
BE (1) BE779540A (de)
CH (1) CH535593A (de)
DE (1) DE2107960A1 (de)
FR (1) FR2125506B1 (de)
GB (1) GB1370538A (de)
IT (1) IT948586B (de)
NL (1) NL7201511A (de)

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4019983A (en) * 1974-10-10 1977-04-26 Houdaille Industries, Inc. Disinfection system and method
US4152409A (en) * 1977-02-04 1979-05-01 Dowa Mining Co., Ltd. Method for carrying out air oxidation and for adding fine bubbles to a liquid
FR2409234A1 (fr) * 1977-11-22 1979-06-15 Clevepak Corp Parasiticide pour lutter contre les micro-organismes nocifs
US4220612A (en) * 1979-04-23 1980-09-02 Envirotech Corporation Flotation cell feed duct
US4252780A (en) * 1978-05-11 1981-02-24 Wacker-Chemitronic Gesellschaft Fur Elektronik Grundstoffe Mbh Process for working up hydrolyzable and/or water-soluble compounds
US4313827A (en) * 1980-09-04 1982-02-02 Fischer & Porter Co. Enhanced disinfection system
US4370304A (en) * 1978-06-01 1983-01-25 Unie Van Kunstmestfabrieken, B.V. Two-phase spraying device and reaction chamber for the preparation of a product containing ammonium orthophosphate
US4389312A (en) * 1981-10-05 1983-06-21 Harold Beard Variable venturi sewerage aerator
US4515655A (en) * 1983-08-15 1985-05-07 Westvaco Corporation Method of bleaching paper pulp by blending chlorine with a flow volume of paper pulp slurry
US4645603A (en) * 1977-11-09 1987-02-24 Frankl Gerald P Liquid aeration device and method
EP0338147A1 (de) * 1986-02-12 1989-10-25 QUANTUM TECHNOLOGIES, Inc. Kontinuierliche Reaktion von Gasen mit Flüssigkeiten
RU2140616C1 (ru) * 1998-10-22 1999-10-27 Товарищество с ограниченной ответственностью Многопрофильное предприятие "Кварк" Тепломассообменник смесительного типа
US5985231A (en) * 1996-12-05 1999-11-16 Ammonia Casale S.A. Catalytic carbon monoxide conversion with acceleration or gaseous feed
US6682057B2 (en) * 2001-05-01 2004-01-27 Estr, Inc. Aerator and wastewater treatment system
US20080048348A1 (en) * 2006-07-11 2008-02-28 Shung-Chi Kung Circulation water vortex bubble generation device for aquaculture pond
US20100065972A1 (en) * 2008-09-12 2010-03-18 Msp Corporation Method and apparatus for liquid precursor atomization
US20140064017A1 (en) * 2006-09-21 2014-03-06 Basf Aktiengesellschaft Process for mixing a liquid or mixture of a liquid and a fine solid present in an essentially self-containing vessel
US20160039400A1 (en) * 2014-08-08 2016-02-11 Ford Global Technologies, Llc Multi-passageway aspirator

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2410570C2 (de) * 1974-03-06 1982-04-29 Basf Ag, 6700 Ludwigshafen Vorrichtung zum Ansaugen und Verdichten von Gasen und deren Vermischung mit Flüssigkeit
FR2339430A1 (fr) * 1976-02-02 1977-08-26 Cem Comp Electro Mec Procede pour obtenir un melange homogene de deux ou plusieurs liquides, miscibles ou non miscibles
GB8607699D0 (en) * 1986-03-27 1986-04-30 Shell Int Research Mixing fluids
GR862922B (en) * 1986-12-18 1987-01-12 Himikes Viomihanies Voreiou El Tubular reactor
JPH0240225A (ja) * 1988-06-23 1990-02-09 Exxon Res & Eng Co 液中に微細気泡を発生させる方法及び装置
GB2233245A (en) * 1989-06-27 1991-01-09 Lian Seng Lee Injecting gas into liquid
DE29808307U1 (de) 1998-05-11 1998-08-20 Möbius, Andreas, Prof. Dr.rer.nat., 41472 Neuss Vorrichtung zum gerichteten Einblasen von Luft, anderen Gasen oder Dämpfen unter gleichzeitiger Flüssigkeitsumwälzung
DE102008017620B4 (de) * 2008-04-04 2010-04-08 Snowbox Schnee- Und Eistechnik Gmbh Vorrichtung zur Erzeugung von Schnee, insbesondere Schneedüse, bzw. Schnee-Erzeugungs-Vorrichtung

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4019983A (en) * 1974-10-10 1977-04-26 Houdaille Industries, Inc. Disinfection system and method
US4152409A (en) * 1977-02-04 1979-05-01 Dowa Mining Co., Ltd. Method for carrying out air oxidation and for adding fine bubbles to a liquid
US4645603A (en) * 1977-11-09 1987-02-24 Frankl Gerald P Liquid aeration device and method
FR2409234A1 (fr) * 1977-11-22 1979-06-15 Clevepak Corp Parasiticide pour lutter contre les micro-organismes nocifs
US4252780A (en) * 1978-05-11 1981-02-24 Wacker-Chemitronic Gesellschaft Fur Elektronik Grundstoffe Mbh Process for working up hydrolyzable and/or water-soluble compounds
US4370304A (en) * 1978-06-01 1983-01-25 Unie Van Kunstmestfabrieken, B.V. Two-phase spraying device and reaction chamber for the preparation of a product containing ammonium orthophosphate
US4220612A (en) * 1979-04-23 1980-09-02 Envirotech Corporation Flotation cell feed duct
US4313827A (en) * 1980-09-04 1982-02-02 Fischer & Porter Co. Enhanced disinfection system
US4389312A (en) * 1981-10-05 1983-06-21 Harold Beard Variable venturi sewerage aerator
US4515655A (en) * 1983-08-15 1985-05-07 Westvaco Corporation Method of bleaching paper pulp by blending chlorine with a flow volume of paper pulp slurry
EP0338147A1 (de) * 1986-02-12 1989-10-25 QUANTUM TECHNOLOGIES, Inc. Kontinuierliche Reaktion von Gasen mit Flüssigkeiten
US5985231A (en) * 1996-12-05 1999-11-16 Ammonia Casale S.A. Catalytic carbon monoxide conversion with acceleration or gaseous feed
AU733699B2 (en) * 1996-12-05 2001-05-24 Ammonia Casale S.A. High efficiency catalytic carbon monoxide conversion process
RU2140616C1 (ru) * 1998-10-22 1999-10-27 Товарищество с ограниченной ответственностью Многопрофильное предприятие "Кварк" Тепломассообменник смесительного типа
US6682057B2 (en) * 2001-05-01 2004-01-27 Estr, Inc. Aerator and wastewater treatment system
US20040140576A1 (en) * 2001-05-01 2004-07-22 La Crosse Gaylen R. Treatment of water with contaminants
US20080048348A1 (en) * 2006-07-11 2008-02-28 Shung-Chi Kung Circulation water vortex bubble generation device for aquaculture pond
US20140064017A1 (en) * 2006-09-21 2014-03-06 Basf Aktiengesellschaft Process for mixing a liquid or mixture of a liquid and a fine solid present in an essentially self-containing vessel
US20100065972A1 (en) * 2008-09-12 2010-03-18 Msp Corporation Method and apparatus for liquid precursor atomization
US8132793B2 (en) * 2008-09-12 2012-03-13 Msp Corporation Method and apparatus for liquid precursor atomization
US8393599B2 (en) 2008-09-12 2013-03-12 Msp Corporation Apparatus for liquid precursor atomization
US8529985B2 (en) 2008-09-12 2013-09-10 Msp Corporation Method for liquid precursor atomization
US20160039400A1 (en) * 2014-08-08 2016-02-11 Ford Global Technologies, Llc Multi-passageway aspirator

Also Published As

Publication number Publication date
DE2107960A1 (de) 1972-08-24
GB1370538A (en) 1974-10-16
FR2125506A1 (de) 1972-09-29
BE779540A (fr) 1972-08-18
IT948586B (it) 1973-06-11
FR2125506B1 (de) 1975-02-14
NL7201511A (de) 1972-08-22
CH535593A (de) 1973-04-15

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