EP0669852B1 - Verfahren und anordnung zur lösung einer gasmenge in einer strömenden flüssigkeitsmenge - Google Patents

Verfahren und anordnung zur lösung einer gasmenge in einer strömenden flüssigkeitsmenge Download PDF

Info

Publication number
EP0669852B1
EP0669852B1 EP93920760A EP93920760A EP0669852B1 EP 0669852 B1 EP0669852 B1 EP 0669852B1 EP 93920760 A EP93920760 A EP 93920760A EP 93920760 A EP93920760 A EP 93920760A EP 0669852 B1 EP0669852 B1 EP 0669852B1
Authority
EP
European Patent Office
Prior art keywords
gas
liquid
pipe
stream
flow
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.)
Expired - Lifetime
Application number
EP93920760A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0669852A1 (de
Inventor
Holger Grossmann
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.)
Otto Tuchenhagen GmbH and Co KG
Original Assignee
Otto Tuchenhagen GmbH and Co KG
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 Otto Tuchenhagen GmbH and Co KG filed Critical Otto Tuchenhagen GmbH and Co KG
Publication of EP0669852A1 publication Critical patent/EP0669852A1/de
Application granted granted Critical
Publication of EP0669852B1 publication Critical patent/EP0669852B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • B01F25/50—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
    • B01F25/53—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle in which the mixture is discharged from and reintroduced into a receptacle through a recirculation tube, into which an additional component is introduced
    • 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
    • B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
    • 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
    • B01F23/23762—Carbon dioxide
    • B01F23/237621—Carbon dioxide in beverages
    • 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
    • Y10S261/07—Carbonators
    • 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
    • Y10S261/27—Gas circulated in circuit

Definitions

  • the invention relates to a method for dissolving an amount of gas in a flowing amount of liquid according to the preamble of claim 1 and an arrangement for performing the method.
  • a method of the type identified in the introduction and an arrangement for carrying out the method are known from WO-A-8802276.
  • the separating device used in the known arrangement has a partition which is permeable to the bubble-free liquid and which retains the gas bubbles in the circulating liquid.
  • the procedural and fluid-mechanical requirements for the gas / liquid mass transfer are well known.
  • the gas must be supplied to the liquid, dispersed in it and distributed homogeneously over the cross-section through which the liquid flows.
  • the so-called equilibrium curve the solution equilibrium between gas and liquid, provides the maximum amount of gas that is soluble in the liquid at a given line pressure and temperature.
  • the amount of gas resulting from the solution equilibrium if it is offered to the liquid in exactly this amount, theoretically, they can only be dissolved in the liquid over an infinitely long period of time. Therefore, in practice, the solution equilibrium is generally not achieved and the choice of the changeable operating parameters ensures that there is a sufficient concentration gradient between the equilibrium concentration (also saturation concentration) and the desired and ultimately occurring actual concentration.
  • the mixture of gas and liquid supplied via the two-substance nozzle flows downward together with the two-phase mixture which is drawn in from the annular space.
  • Part of the liquid is drawn off at the lower end of the reactor.
  • the other part of the liquid flows upwards together with the gas in the annulus.
  • part of the gas degasses, while the other part together with the liquid again participates in the circulation in the reactor.
  • Loop reactors are to be understood to mean apparatuses in which at least one defined circulation of a fluid or fluidized system, which comprises the total flow, takes place. In this case, a continuous flow can be superimposed on the circulating flow, as a result of which the flow pattern of a “loop” is created. There are loop reactors with internal and external circulation.
  • a loop reactor is not particularly easy to clean or clean, particularly when used in the food and beverage industry, where it is extremely important that all areas of the reactor are cleaned biologically CIP-compliant arrangement (CIP: abbreviation for "cleaning in place”, which means “cleanable on the spot in the flow”), and on the other hand it may have to be classified as a pressure vessel that has to meet certain safety requirements, which means that it can be subject to approval or monitoring, which makes it technically complex and expensive from the outset.
  • CIP abbreviation for "cleaning in place”
  • DE 39 20 472 A1 discloses a method for the defined loading of a liquid with a gas, in which the loading process at a specific point in the flow path of the liquid is essentially ended by coalescence of the undissolved gas bubbles. Undissolved, coalesced gas bubbles are either redispersed and mixed again in the course of the flow path of the liquid to be loaded in the latter, or they are separated from the liquid.
  • the known device for carrying out the aforementioned method provides a separating device at the end of the loading section, in which a separation of undissolved gas bubbles from the liquid is achieved by centrifugal forces in the rotating liquid.
  • This separating device is a container in which the rotating liquid forms a paraboloid of revolution, over the free surface of which the undissolved gas bubbles are separated (column 4, lines 37 to 51). Because of these conditions, the separated material flow is a pure gas flow, and no further statements are made regarding its further use.
  • the object of the present invention is to increase the amount of gas which is actually soluble in a liquid under given conditions compared to known methods.
  • the arrangement for carrying out the method in the structure should be simple, flow-cleanable (CIP-capable), and its adaptation to certain practical requirements and its regulation should be as simple as possible.
  • the separation of the total flow by subjecting it to flow guidance on curved paths into a bubble-free liquid flow and a gas / liquid flow designed as a two-phase flow ensures, on the one hand, that no uncontrollable after-gassing takes place in the liquid continued from the separation point.
  • the separation is the prerequisite for the return of a partial flow.
  • the recirculated gas / liquid stream is superimposed as a recycle stream on the supplied non-gassed or fumigated liquid stream, which forms the continuous flow.
  • the recycling offers the possibility of redispersing the undissolved gas bubbles contained in the circulating stream and distributing them homogeneously in the overall stream.
  • the concentration gradient is increased at the point where the throughflow and circulation flow are brought together, and the superimposition of both flows also results in increased turbulence there.
  • the gas in the returning gas / liquid stream is at least partially redispersed in its carrier liquid before being combined with the supplied non-gassed or fumigated liquid stream (continuous flow). This measure contributes to a further improvement of the mass transfer.
  • another embodiment of the proposed method according to the invention provides that the combined gas / liquid mixture is subjected to flow guidance on curved paths and the rotational energy required for this is obtained from the energy of the flowing gas / liquid mixture is disputed, which results in a relatively simple apparatus implementation of this process step.
  • the centerpiece of the arrangement according to the invention is a separating device in which a separation of undissolved gas bubbles from the liquid is achieved by centrifugal forces in the rotating liquid, the mixing device or the solution section opening into an inlet of the separating device and, on the one hand, to an outlet of the separating device Continued pipeline section of the pipeline for the bubble-free liquid flow and, on the other hand, the return line for the remaining gas / liquid flow is connected to a head region of the separating device.
  • the gas in the gas / liquid stream to be recycled in the sense of the procedural measures already proposed above, can be at least partially and effectively effective in its carrier liquid before being combined with the supplied non-degassed or fumigated liquid stream redispersed and homogeneously distributed over the return line cross section, which serves to further improve the mass transfer.
  • the proposed arrangement can be regulated in a very simple manner by the second conveying device in the return line, so that it can be adapted very easily to changed operating conditions.
  • the separating device as a centrifugal separator, specifically in a first embodiment as a hydrocyclone, as is provided by another embodiment of the proposed arrangement, it is particularly easy to separate the total flow into a bubble-free flow and a circulation flow designed as a two-phase flow (gas / liquid flow) , but still extremely effective.
  • the return line is connected to the dip tube of the hydrocyclone.
  • the separating device When the separating device is designed as a hydrocyclone, under certain operating conditions, so-called "trombone formation" can occur, as a result of which the gas concentrating in the vortex core is partially entrained in the outlet arranged coaxially in the separating device. Special design precautions are then required in the sequence so that the gas can be retained in the separating device, at least up to a certain degree of loading of the liquid with gas, and can be discharged solely via the dip tube used to discharge the two-phase flow (gas / liquid flow).
  • the separation performance improves compared to the design of the separating device as a hydrocyclone if, as is provided by a further advantageous arrangement according to the invention, it is designed as a container into which the inlet is tangential Drain, in continuation of the direction of flow, open tangentially, and a dip tube engages a bit in the interior of the container via the discharge-side end face of a dip tube in the direction of the axis and concentrically to the lateral surface of the container, the dip tube on the other hand is connected to the return line.
  • the outlet like the inlet, is also arranged in the jacket region of the container, as a result of which the degassed liquid rotating in this region can preferably be removed.
  • the liquid rotating in the center, in the area of the container axis, and highly loaded with gas now only has the option of leaving the separating device in the form of the two-phase flow (gas / liquid flow) via the dip tube. It is essential that the immersion tube is arranged in the outlet-side area of the separating device so that the dwell time necessary for separating the gas bubbles from the jacket area into the axial area of the container is available for the gas / liquid mixture flowing through the container.
  • the second delivery device is designed as a self-priming centrifugal pump, preferably as a side channel pump is.
  • Self-priming centrifugal pumps are relatively simple in construction; they can convey both a two-phase mixture and pure gas, they are self-cleaning, they have no abrasion and therefore require little maintenance.
  • the arrangement ( Figure 1) consists of a pipe 1, which consists of the pipe sections 1a and 1b.
  • the pipe section 1a opens into a static mixing device 5, which is optionally followed by a solution section 5a.
  • the entire mixing and solution device can also consist of only one solution section 5a.
  • the static mixing device 5 can be constructed from a single static mixer or a mixing element or from a plurality of static mixers connected in series; it is referred to below as "static mixer 5".
  • the static mixer 5 or the solution section 5a are connected to an inlet 6a of a separating device 6, in which, according to the invention, the gas / liquid mixture is separated into a gas / liquid and a bubble-free liquid flow.
  • the pipeline 1 is continued behind the separating device 6 in the pipeline section 1b via an outlet 6b arranged in the foot region thereof.
  • a return line 7 is at the head region of the separating device 6 connected, which engages in the interior of the separating device 6 via an immersion tube 6c and which, on the other hand, opens into the pipeline section 1a at a second introduction point 9.
  • a gas line 3 serving the gas supply G which is led via a metering device 10, leads via an introduction point 4 into the return line 7 behind a second conveying device 8 arranged therein.
  • the introduction point 4 as provided by further configurations of the arrangement according to the invention, can also be arranged in front of or behind or at the second introduction point 9 (dash-dotted representation of the part of the gas line 3 opening at the introduction point 4). .
  • a separating device 6 designed as a cylindrical container has an inlet 6a arranged tangentially and an outlet 6b opening out tangentially from the container in continuation of the flow direction. This becomes clear in the top view of the separating device 6 (FIG. 2a).
  • wrap angle seen in a container cross-sectional plane
  • the only decisive factor is that the rotational flow in the container can flow smoothly and thus inevitably into the outlet 6b in the direction of flow. It is also irrelevant to the mode of operation of the separating device 6 whether it is arranged vertically, horizontally or in any inclined position in space with respect to its container axis.
  • An ungased amount of liquid L1 (liquid phase) is supplied via the pipe section 1a (see FIGS. 1, 2 and 2a), which is conveyed through the arrangement by means of the first conveying device 2, which can be a centrifugal pump, the amount of liquid L1 being the so-called continuous flow forms.
  • a gas quantity G (gas phase) is supplied via the gas line 3.
  • the gas flow G can be set by means of the metering device 10, which is generally designed as a throttle and control valve.
  • the gas / liquid flow G * / L2 formed as a two-phase flow is combined with the gas flow G, the entire gas fraction G + G * in the further course through the return line 7 being at least partially already in it Carrier liquid L2 can be redispersed.
  • the static mixer 5 and the solution section 5a are acted upon by the flow which is established in the return line 7.
  • the gas / liquid flow G * / L2 formed as a two-phase flow.
  • the latter forms the so-called circulation flow, which is superimposed on the flow current L1 within the pipeline 1 between the second introduction point 9 and the separation device 6.
  • a bubble-free liquid flow L1 * (liquid phase) is discharged via the outlet 6b of the separating device 6, which is connected to the pipe section 1b.
  • the second delivery device 8 Since the second delivery device 8 has to deliver both bubble-free liquid L2 and pure gas G * in addition to the two-phase flow G * / L2 under certain operating conditions, it is expediently designed as a self-priming centrifugal pump, preferably as a side channel pump. It goes without saying that the second conveying device 8 can also be substituted by another pump, such as, for example, a rotating displacement pump, in particular an impeller pump or jet pump, provided that it has the required conveying properties.
  • a rotating displacement pump such as, for example, a rotating displacement pump, in particular an impeller pump or jet pump, provided that it has the required conveying properties.
  • FIGS. 1 to 2a for carrying out the proposed method are particularly suitable for the so-called carbonization of beer.
  • Carbonation of beer refers to the enrichment of beer with CO2 gas, whereby brewery technology today demands a complete solution of a given amount of CO2 in a certain amount of beer.
  • Design criteria for such a carbonation plant are therefore firstly to ensure a certain CO2 concentration in the beer and secondly its complete and therefore bubble-free solution.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Degasification And Air Bubble Elimination (AREA)
EP93920760A 1992-11-19 1993-09-18 Verfahren und anordnung zur lösung einer gasmenge in einer strömenden flüssigkeitsmenge Expired - Lifetime EP0669852B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE4238971A DE4238971C2 (de) 1992-11-19 1992-11-19 Verfahren und Anordnung zur Lösung einer Gasmenge in einer strömenden Flüssigkeitsmenge
DE4238971 1992-11-19
PCT/EP1993/002527 WO1994011097A1 (de) 1992-11-19 1993-09-18 Verfahren und anordnung zur lösung einer gasmenge in einer strömenden flüssigkeitsmenge

Publications (2)

Publication Number Publication Date
EP0669852A1 EP0669852A1 (de) 1995-09-06
EP0669852B1 true EP0669852B1 (de) 1996-06-12

Family

ID=6473225

Family Applications (1)

Application Number Title Priority Date Filing Date
EP93920760A Expired - Lifetime EP0669852B1 (de) 1992-11-19 1993-09-18 Verfahren und anordnung zur lösung einer gasmenge in einer strömenden flüssigkeitsmenge

Country Status (9)

Country Link
US (1) US5762687A (pt)
EP (1) EP0669852B1 (pt)
JP (1) JP2681711B2 (pt)
BR (1) BR9307485A (pt)
CA (1) CA2149775A1 (pt)
DE (2) DE4238971C2 (pt)
DK (1) DK0669852T3 (pt)
ES (1) ES2091034T3 (pt)
WO (1) WO1994011097A1 (pt)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19716447C1 (de) * 1997-04-21 1998-05-07 Tuchenhagen Gmbh Verfahren zum Anfahren einer Flüssigkeits-Dosieranlage mit In-line-Eigenschaften, insbesondere bei der Herstellung von Softdrinks aus Wasser, Sirup und Kohlendioxid
DE19801695C1 (de) * 1997-04-21 1999-05-27 Tuchenhagen Gmbh Verfahren zum Anfahren einer Flüssigkeits-Dosieranlage mit In-Line-Eigenschaften, insbesondere bei der Herstellung von Softdrinks aus Wasser, Sirup und Kohlendioxid
AU9263498A (en) 1997-08-22 1999-03-16 Tuchenhagen Gmbh Method and device for filling non-carbonated beverages into thin-walled containers stabilised by internal pressure
RU2142074C1 (ru) * 1998-04-17 1999-11-27 Попов Сергей Анатольевич Насосно-эжекторная компрессорная установка (варианты)
US6730214B2 (en) * 2001-10-26 2004-05-04 Angelo L. Mazzei System and apparatus for accelerating mass transfer of a gas into a liquid
DE102004007727A1 (de) * 2004-02-16 2005-09-01 Margret Spiegel Herkömmliche Karbonatorsysteme oder Imprägniersysteme zusätzlich mindestens ein Hohlkörper-Inlineimprägnierer befüllt mit Schüttgut um schon karbonisierte oder imprägnierte Flüssigkeiten nachzukarbonisieren oder imprägnieren
CA2646162A1 (en) * 2006-03-29 2007-10-11 Carbotek Holding Gmbh Impregnator
JP5122912B2 (ja) 2007-10-25 2013-01-16 サントリーホールディングス株式会社 炭酸飲料の製造方法
JP5627877B2 (ja) 2009-11-18 2014-11-19 サントリーホールディングス株式会社 炭酸飲料の製造方法
DE102010025690A1 (de) * 2010-06-30 2012-01-05 Khs Gmbh Verfahren und Anlage zur Herstellung von Fluidgemischen, z.B. Getränken
DE102012219159B4 (de) 2012-10-19 2024-03-07 Krones Ag Vorrichtung zum Karbonisieren eines flüssigen Mediums und Verfahren zum Karbonisieren eines flüssigen Mediums
CN107008168B (zh) * 2017-05-19 2023-10-31 北京东方同华科技股份有限公司 一种单循环二级溶气系统及其溶气方法
CN112334221A (zh) * 2018-07-05 2021-02-05 日本斯频德制造株式会社 浆料制造装置及浆料的制造方法
JP7260429B2 (ja) * 2019-07-19 2023-04-18 株式会社荏原製作所 ガス溶解液製造装置

Family Cites Families (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US547816A (en) * 1895-10-15 Soda-water apparatus
US655727A (en) * 1899-02-10 1900-08-14 New Era Carbonator Company Carbonating apparatus.
DE398640C (de) * 1922-09-19 1924-07-15 Pfisterer Karl Einrichtung zur Behandlung von Stoffen verschiedener physikalischer Eigenschaften miteinander
FR909115A (fr) * 1944-09-27 1946-04-30 Ets Kuhlmann Dispositif pour la mise en contact intime d'un ou plusieurs gaz avec un liquide
US3256802A (en) * 1962-03-14 1966-06-21 Shasta Beverage Division Of Co Continuous carbonation system
GB1051907A (pt) * 1963-05-07
US3572550A (en) * 1968-10-14 1971-03-30 Eaton Yale & Towne Method of and apparatus for carbonating, having intersecting streams of gas and liquid
DE1915135B2 (de) * 1969-03-25 1971-10-28 Anlass schalter fuer einen einphasen asynchronmotor
FR2098483A5 (pt) * 1970-01-27 1972-03-10 Cem Comp Electro Mec
US3900420A (en) * 1970-05-18 1975-08-19 Felix Sebba Microgas emulsions and method of forming same
FR2123649A6 (en) * 1971-01-26 1972-09-15 Cem Comp Electro Mec Liquid-gas contactor - giving high surface /volume ratio between the phases
GB1368023A (en) * 1971-02-24 1974-09-25 Zanussi A Spa Industrie Device for the production of carbonated beverages
US3780198A (en) * 1971-06-07 1973-12-18 Crown Cork & Seal Co System for carbonating beverages
US3877358A (en) * 1972-06-19 1975-04-15 Shasta Beverages Carbonated beverage system
JPS5126685A (pt) * 1974-08-29 1976-03-05 Mitsubishi Electric Corp
GB1589306A (en) * 1978-05-24 1981-05-13 Grace W R Ltd Method and apparatus for mixing polyurethane foam
ZA793185B (en) * 1978-08-30 1981-02-25 Dorr Oliver Inc Apparatus and process for dissolution of gases in liquid
US4483826A (en) * 1980-08-12 1984-11-20 Phillips Petroleum Company Combination reaction vessel and aspirator-mixer
US4584002A (en) * 1981-06-22 1986-04-22 Halliburton Company Recirculating foam generator
FR2530484B1 (fr) * 1982-07-26 1989-09-08 Sgn Soc Gen Tech Nouvelle Procede et dispositif pour la dissolution de gaz dans un liquide
FR2597003B1 (fr) * 1986-04-15 1990-09-07 Air Liquide Procede et dispositif de traitement d'un liquide alimentaire avec un gaz
FR2604371B1 (fr) * 1986-09-30 1990-07-06 Toulouse Inst Nal Sciences App Procede et dispositif d'echange entre un gaz et un liquide
DE3920472A1 (de) * 1989-06-22 1991-01-10 Tuchenhagen Otto Gmbh Verfahren und vorrichtung zur definierten beladung einer fluessigkeit mit einem gas

Also Published As

Publication number Publication date
JP2681711B2 (ja) 1997-11-26
DE59302951D1 (de) 1996-07-18
CA2149775A1 (en) 1994-05-26
WO1994011097A1 (de) 1994-05-26
BR9307485A (pt) 1999-08-24
DE4238971C2 (de) 1996-08-29
EP0669852A1 (de) 1995-09-06
ES2091034T3 (es) 1996-10-16
US5762687A (en) 1998-06-09
JPH07509181A (ja) 1995-10-12
DK0669852T3 (da) 1996-10-28
DE4238971A1 (de) 1994-05-26

Similar Documents

Publication Publication Date Title
EP0669852B1 (de) Verfahren und anordnung zur lösung einer gasmenge in einer strömenden flüssigkeitsmenge
EP0819101B1 (de) Anlage und verfahren zur oxidation eines wässrigen mediums
DE2722826A1 (de) Vorrichtung zum einblasen von gas in eine fluessigkeit
DE3047101A1 (de) Verfahren zum verbessern der gasverteilung in mammut-schlaufenreaktoren
DE4240572A1 (de) Beizanlage und Verfahren zum Betreiben der Beizanlage
EP0044498B1 (de) Vorrichtung zum Begasen von Flüssigkeiten oder Suspensionen
DE2708653C3 (de) Anlage zur Behandlung von pumpfähigem Abfallstoff
CH630046A5 (en) Method for the continuous entry of air or other oxygen-containing gases into an activated-sludge-containing wastewater or fermentation broths
DE2516371A1 (de) Verfahren und vorrichtung zur loesung von gasfoermigem sauerstoff in einer fluessigkeit
WO1995032795A1 (de) Vorrichtung zum mischen zweier fluide
DE4337091A1 (de) Verfahren zum Betreiben eines Wasserbelüftungssystems sowie Vorrichtung, insbesondere zur Durchführung des Verfahrens
DE19842332A1 (de) Verfahren und Vorrichtung zur biologischen Reinigung von Abwasser
DE2552228A1 (de) Verfahren und vorrichtung zur mikroflotation mittels druckfluessigkeit
DE2359656B2 (de) Vorrichtung zum Klaren von feste Stoffe enthaltendem Abwasser o.dgl. Flüssigkeiten
DE2647913A1 (de) Verfahren und vorrichtung zur gasuebertragung mit verduennungssteuerung
DE19625108C2 (de) Verfahren und Vorrichtung zur Entgasung von Flüssigkeiten, insbesondere zur Entfernung von Sauerstoff aus Wasser
DE3331993A1 (de) Verfahren und vorrichtung zur entgasung von gas-liquid-systemen ohne schaumbildung
DE2603798B1 (de) Vorrichtung zur begasung von fluessigkeiten und/oder fluessig-feststoffgemischen
DE8524206U1 (de) Vorrichtung zur Gasinjektion in Flüssigkeiten
DE1557197A1 (de) Verfahren und Vorrichtung zum Umruehren und Homogenisieren der Inhalte von grossen Behaeltern
DE2310027A1 (de) Verfahren und vorrichtung zum dispergieren von gas in einer fluessigkeit
DE8608486U1 (de) Vorrichtung zur Anreicherung von Wasser mit Sauerstoff
DE3516691A1 (de) Vorrichtung zum homogenisieren und temperieren von fluessigkeiten
DE2553824A1 (de) Fallrohr-vorrichtung
DE2542656A1 (de) Verfahren zum eindispergieren von gasen in eine zusammenhaengende fluessigkeitsphase

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19950427

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE DK ES FR GB IT NL SE

17Q First examination report despatched

Effective date: 19951108

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: OTTO TUCHENHAGEN GMBH & CO. KG

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DE DK ES FR GB IT NL SE

ITF It: translation for a ep patent filed

Owner name: BARZANO' E ZANARDO MILANO S.P.A.

REF Corresponds to:

Ref document number: 59302951

Country of ref document: DE

Date of ref document: 19960718

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19960802

ET Fr: translation filed
REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2091034

Country of ref document: ES

Kind code of ref document: T3

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2091034

Country of ref document: ES

Kind code of ref document: T3

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19990705

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19990721

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DK

Payment date: 19990916

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 19990928

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000918

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000919

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 20000929

EUG Se: european patent has lapsed

Ref document number: 93920760.1

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010531

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20010930

Year of fee payment: 9

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20030401

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20030901

Year of fee payment: 11

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20011011

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040918

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20040918

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20050918

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20060913

Year of fee payment: 14

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20080401