EP2608875A1 - Device and method for gas dispersion - Google Patents

Device and method for gas dispersion

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Publication number
EP2608875A1
EP2608875A1 EP11723393.2A EP11723393A EP2608875A1 EP 2608875 A1 EP2608875 A1 EP 2608875A1 EP 11723393 A EP11723393 A EP 11723393A EP 2608875 A1 EP2608875 A1 EP 2608875A1
Authority
EP
European Patent Office
Prior art keywords
zone
zones
gas
liquid
mixing elements
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.)
Granted
Application number
EP11723393.2A
Other languages
German (de)
French (fr)
Other versions
EP2608875B1 (en
Inventor
Jens Hepperle
Jörg KIRCHHOFF
Klemens KOHLGRÜBER
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.)
Bayer Intellectual Property GmbH
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Bayer Intellectual Property GmbH
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Publication date
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Publication of EP2608875A1 publication Critical patent/EP2608875A1/en
Application granted granted Critical
Publication of EP2608875B1 publication Critical patent/EP2608875B1/en
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Classifications

    • 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
    • B01F23/232—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
    • B01F23/2323—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 by circulating the flow in guiding constructions or conduits
    • 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
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3131—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit with additional mixing means other than injector mixers, e.g. screens, baffles or rotating elements
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/431—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor
    • B01F25/4314—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor with helical baffles
    • B01F25/43141—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor with helical baffles composed of consecutive sections of helical formed elements
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/431—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor
    • B01F25/4316—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor the baffles being flat pieces of material, e.g. intermeshing, fixed to the wall or fixed on a central rod
    • B01F25/43161—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor the baffles being flat pieces of material, e.g. intermeshing, fixed to the wall or fixed on a central rod composed of consecutive sections of flat pieces of material
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/433—Mixing tubes wherein the shape of the tube influences the mixing, e.g. mixing tubes with varying cross-section or provided with inwardly extending profiles
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/433—Mixing tubes wherein the shape of the tube influences the mixing, e.g. mixing tubes with varying cross-section or provided with inwardly extending profiles
    • B01F25/4334—Mixers with a converging cross-section
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/82—Combinations of dissimilar mixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/82—Combinations of dissimilar mixers
    • B01F33/821—Combinations of dissimilar mixers with consecutive receptacles

Definitions

  • the invention relates to an apparatus and a method for dispersing gas in a liquid.
  • the dispersion of gases in liquid media is widely used in the chemical industry, for example in hydrogenations, chlorinations or oxidations.
  • the oxygen input is essential.
  • a dispersion of gas takes place in a liquid medium.
  • gases are dispersed in highly viscous liquids, e.g. Make creams, foam or chocolate with air-filled porous structure (e.g., described in WO02 / 13618A2).
  • gas dispersion The goal of a gas dispersion is the introduction of gas into a fluid, preferably in the form of small bubbles as possible, to produce the largest possible interface between gaseous and liquid phase.
  • Gas dispersion often takes place in two steps:
  • the division of the bubbles can be done for example by means of a dynamic or static mixer. While in dynamic mixers, the homogenization of a mixture is achieved by moving organs such as stirrers, is static
  • the feed fluid eg a pump
  • static mixers For an overview of various types of static mixers, see, for example, Static Mixers and Their Applications, "MH Pahl and E. Muschelknautz, Chem. Ing. 52 (1980) No. 4, pp. 285-291
  • static mixers are SMX mixers (see patent US4062524) or SMXL mixers (see, for example, US 5520460.) They consist of two or more mutually perpendicular lattices of parallel metal strips which are interconnected at their intersection points and in one An individual mixing element is unsuitable as a mixer since mixing takes place only along a preferential direction transverse to the main flow direction Therefore, usually several mixing elements, each to each other around 90 °, arranged one behind the other The use of static mixers for dispersing vo n Gas in a liquid is known.
  • WO2005 / 103115A1 describes the use of a static mixer in a process for the preparation of polyalkarate by the transesterification process.
  • a foaming agent is added to the polymer melt. By subsequent reduction in pressure, the foaming agent escapes with foaming of the melt.
  • the foam causes a large increase in surface area, which is advantageous for degassing, i. the removal of volatiles is.
  • an inert gas such as e.g. Nitrogen used by means of a static mixer, e.g. an SMX mixer, is introduced into the melt and dispersed.
  • a first subject of the present invention is therefore an apparatus for dispersing gas into a liquid having a number n of successive zones Zi, Z 2 , ..., Z n with static mixing elements, each zone Z; a length L t and an effective diameter D t , characterized in that the individual zones are designed so that the normalized to the respective ratio Lj / Dj mechanical energy input E t , which acts on the gas-liquid mixture, in the flow direction increases from zone to zone, where n is an integer greater than or equal to 3 and i is an index that traverses the integer from 1 to the number n of zones.
  • Another object of the present invention is a method for dispersing gas into a liquid in which gas and liquid are conveyed together by a mixing device and thereby a number n of successive Zones Zi, Z 2 , ..., Z n flow through with static mixing elements, each zone Z; has a length L t and an effective diameter D t , characterized in that the normalized to the respective ratio Lj / Dj mechanical energy input E t , which acts on the gas-liquid mixture increases in the flow direction from zone to zone, wherein n an integer greater than or equal to 3, and i is an index that traverses the integer from 1 to the number n of zones.
  • Liquid is generally understood here to mean a medium which can be conveyed through the device according to the invention. This may, for example, also be a melt or a dispersion (eg emulsion or suspension).
  • the term fluid is used.
  • the fluid is preferably of higher viscosity, ie it has a viscosity between 2 mPas and 10,000,000 mPas, more preferably between 1,000 mPas and 1,000,000 mPas (measured in a cone-plate viscometer according to DIN 53019 at a shear rate of 1 s "1).
  • a gas or gas mixture in the fluid is entered mechanical energy into the mixture. This energy input is realized by static mixing elements.
  • a mixer is composed of a series of In order to increase the mixing effect, the number of mixing elements in a mixer can be increased. Usually, the mixing elements are introduced into a tube to form a static mixer.It should be noted that the present invention is not limited to mixers consisting of a mixing element Arrangement of modular mixing elements are constructed, but also on mixers in a compact Ba uform application finds.
  • the device according to the invention is characterized in that it has a number n of contiguous zones, where n is an integer greater than or equal to 3. There are static mixing elements in each zone. Each zone Z; has a length L t and a cross-sectional area A t .
  • i is an index that traverses the integer from 1 to the number n of zones.
  • the length L t of a zone Z corresponds to the length of the mixing elements arranged one behind the other in this zone; the cross-sectional area A t corresponds to the cross-sectional area of that in the zone Z; present mixing elements. From the cross-sectional area A t to an effective diameter D can t according to equation 1 errechn n:
  • the effective diameter D corresponds in a circular cross section to the diameter of the circle.
  • the effective diameter D t is the diameter of a circle having an area corresponding to the cross-sectional area.
  • the ratio Lj / Dj is one for the respective zone Z; characteristic index.
  • a mixing element has internal structures and channels between these structures. If a fluid is conveyed through a mixing element, the structures and channels cause the fluid to be divided, distributed, sheared and, if necessary, fluidized into partial flows, thus mixing the partial flows with one another.
  • the mean diameter of a channel is subsequently abbreviated by the letter di.
  • a mean channel diameter di is understood to mean the channel diameter arithmetically averaged over all channels, the effective channel diameter corresponding to the effective diameter of a zone Z; can be calculated according to equation 1.
  • the ratio djlDj between the mean channel diameter di and the effective diameter D t of the mixing elements in a zone Z; is also a characteristic index for the respective zone Z;
  • the parameter a t denotes the open cross-sectional area, more precisely the projection surface of the free cross-section.
  • the open cross-sectional area a results from the sum of the projection areas of the individual free cross-sectional areas of the open channels, through which the fluid can flow (equation 3).
  • the parameter m is a counting parameter
  • N is the number of individual free cross-sectional areas.
  • the static mixers used in the prior art for gas dispersion have mixing internals that are consistent throughout the length of the mixer.
  • the length L corresponds to the length of the mixer and whose effective diameter D corresponds to the effective diameter of the mixer.
  • the length L can be increased.
  • the mechanical energy input E abs is proportional to the pressure loss according to equation (4), where V is the volume flow of the fluid.
  • the device according to the invention is characterized by a number n of zones. Each zone Z; is characterized by a specific mechanical energy input E t , which is registered in a fluid flowing through the respective zone.
  • the specific mechanical energy input E t is the mechanical energy input E abs normalized to the characteristic Lj / Dj.
  • the number n of zones in a device according to the invention is not limited. It can run to infinity if the zones become infinitesimally small and there is a continuously increasing specific energy input along the length of the device, as might be the case, for example, with a conically narrowing tube. It is conceivable that further zones exist before or after the zones Zi to Z "which have freely selectable specific energy inputs.
  • a particularly preferred embodiment of the device according to the invention is characterized in that there is a first zone Z 0 , which provides a higher specific energy input than the downstream in the flow direction zone Zi (Eo> Ei).
  • a first zone Z 0 which provides a higher specific energy input than the downstream in the flow direction zone Zi (Eo> Ei).
  • the device according to the invention has a number n of mixing zones, which are arranged one behind the other, wherein the mean channel diameter d t in the mixing zones in the flow direction is smaller. Smaller channels produce a higher pressure loss per length, which is equivalent to increasing specific energy input.
  • This embodiment preferably comprises a cylindrical tube into which mixing elements are introduced.
  • the effective diameter D t of the mixing elements is preferably constant over the entire tube length, while the mean channel diameter d t in successive zones in the flow direction is smaller.
  • mixing elements of the same type are used, e.g. SMX mixers with different ratios d / D.
  • the device according to the invention has an arrangement of mixing elements which have an increasingly smaller effective diameter D t in the flow direction at a constant ratio di / Dj.
  • this embodiment comprises a cylindrical tube into which mixing elements are introduced, which have an increasingly smaller effective diameter D t in the flow direction.
  • the mixing elements whose outer diameter is smaller than the inner diameter of the tube are preferably enclosed with a jacket tube, the outer diameter of which approximately corresponds to the inner diameter of the tube in order to be able to fit into the tube.
  • transition jacket tubes are preferably present, which have a conically tapering in the direction of the mixing element with a small diameter inner diameter.
  • the device according to the invention has Z in each zone; via an arrangement of mixing elements of different types which, with the same ratio Lj / Dj in the flow direction in each zone Z; cause an increasing pressure loss.
  • the mixing elements are introduced into a cylindrical tube. They preferably have the same effective diameter Dj.
  • the device according to the invention is suitable for the dispersion of gas in a liquid, for example for introducing a towing gas into a polymer melt or for foaming liquid media.
  • the gas may be added with tubes or thin capillaries, preferably in the flow direction before the static mixer cascade. Furthermore, the gas may also be added through a porous body.
  • a porous body may comprise, for example, the following geometries: a frit and / or a porous, sintered body and / or a single or multi-layer sieve.
  • the porous body may, for example, be in the form of a cylinder, in the form of a cuboid, a sphere or a cube or in conical form, e.g. as a cone, be formed. These devices ensure a fine predispersion of the gas and possibly also for a distribution of the gas over the cross section.
  • the capillary or the porous body has a mean effective internal hole diameter of preferably 0.1 to 500 ⁇ m, preferably 1 to 200 ⁇ m, particularly preferably 10 to 90 ⁇ m.
  • Porous bodies which may be used are, for example, porous sintered bodies of metal, such as frit bodies used in chromatography, for example the sintered bodies of Mott Corporation (Farmington, USA).
  • wound wire mesh can be used, for example, the wound wire mesh from Fuji Filter Manufacturing Co., Ltd. (Tokyo, Japan), trade name: Fujiloy ®.
  • sieves or multi-layered fabrics can be used, such as the metal wire mesh composite panels of F a. H ⁇ v er & Boecker Wire Weaving (Oelde, Germany), trade name: Häver Porostar.
  • the effective diameter D t of the holes inserted in the porous sintered bodies or wires or wound wire meshes is preferably 1-500 ⁇ m, particularly preferably 2-200 ⁇ m, very particularly preferably 10-90 ⁇ m.
  • Fig. 1 shows examples of three different static mixers according to the invention (No. 1, No. 2 and No. 3): Fig. 1 (a) from above, Fig. 1 (b) from the side (sectional drawing) and Fig. 1 (c) in the arrangement after installation in a pipe or housing.
  • the data for wi and bi indicate the length resp. Width of the projected cross section of the free flow channels.
  • Di denotes the clear diameter and DM the outer diameter of the static mixing elements.
  • Li denotes the entire length of a geometrically uniform mixer section and Ii the length of a single mixing element.
  • No. 1 shows a Kenics mixer.
  • No.2 shows a commercially available SMX static mixer without or with an outer ring.
  • No. 3 shows a mixer with web structure and outer ring (DE 29923895U1 and EP1 189686B1).
  • Fig. 2 shows three different examples (A, B and C) of variants of static mixer according to the invention, with individual zones (characterized by the lengths Li, L 2 , L 3 ), characterized in that the respective ratio Lj / Dj of the individual Zones normalized mechanical energy input E t to a fluid containing the respective zone Z; flows through, increases in the flow direction.
  • the flow direction is indicated by the thick arrow.
  • FIG. 2A shows a sequence of static mixers with a geometrically similar structure and an arrangement of mixing elements which have an increasingly smaller effective diameter D t in the direction of flow at a constant ratio d.
  • Fig. 2 B shows an embodiment with a cylindrical tube into which mixing elements are introduced, in which the effective diameter D t is constant over the entire tube length, while the mean channel diameter d; becomes smaller in successive zones in the flow direction.
  • SMX mixers used mixing elements of the same type, eg SMX mixers with different ratios d / D.
  • Fig. 2C shows an arrangement of mixing elements of different types which, with the same ratio Lj / Dj in the flow direction in each zone Z; cause an increasing pressure loss.
  • a Kenics mixer shown in the first zone of length LI.
  • L2 is an SMX mixer in the second zone of length L2 .
  • the third zone of length L3 is also an SMX mixer with smaller effective diameter D t compared to the mixer in the second zone.
  • Fig. 3A shows a device according to the invention with three zones and a premixer and a gas metering via a capillary. Before the premixer is the area where the fluid is metered (L) and a device for metering gases (G) via a capillary (Ca).
  • FIG. 3B shows a gas metering by means of a porous sintered body (the mixer behind it is not shown here).
  • the premixer In front of the premixer is the area where the fluid is metered (L) and a device for gas metering (G) via a porous sintered body (PS), which is located within the flow cross section.
  • L metered
  • G gas metering
  • PS porous sintered body

Abstract

The invention relates to a device for dispersing gas into a liquid. The device has a number n of successive zones Z1, Z2,...,Zn having static mixing elements, wherein each zone Z i has a length L i and an effective diameter D i . The mechanical energy input Et, which is standardised to the particular ratio L i /D i and acts on the gas/liquid mixture, increases from zone to zone in the flow direction. In this connection n is a whole number greater than or equal to 3 and i is an index which runs through the whole numbers from 1 to the number n of zones. The invention further relates to a method for dispersing gas into a liquid using the device according to the invention.

Description

Vorrichtung und Verfahren zur Gasdispergierung  Apparatus and method for gas dispersion
Die Erfindung betrifft eine Vorrichtung und ein Verfahren zur Dispergierung von Gas in eine Flüssigkeit. The invention relates to an apparatus and a method for dispersing gas in a liquid.
Die Dispergierung von Gasen in flüssigen Medien findet in der chemischen Industrie beispielsweise bei Hydrierungen, Chlorierungen oder Oxidationen eine breite Anwendung. Bei Fermentationen und der aeroben Abwasserreinigung ist der Sauerstoffeintrag von wesentlicher Bedeutung. Auch bei der Schaumerzeugung findet eine Dispergierung von Gas in einem flüssigen Medium statt. In der Lebensmitteltechnik werden Gase in hochviskosen Flüssigkeiten dispergiert, um z.B. Cremes, Schaumgummi oder Schokolade mit luftgefüllter poröser Struktur herzustellen (z.B. beschrieben in WO02/13618A2). The dispersion of gases in liquid media is widely used in the chemical industry, for example in hydrogenations, chlorinations or oxidations. In fermentations and aerobic wastewater treatment, the oxygen input is essential. Also in the foam generation, a dispersion of gas takes place in a liquid medium. In food technology, gases are dispersed in highly viscous liquids, e.g. Make creams, foam or chocolate with air-filled porous structure (e.g., described in WO02 / 13618A2).
Das Ziel einer Gasdispergierung ist der Eintrag von Gas in ein Fluid, vorzugsweise in Form von möglichst kleinen Bläschen, um eine möglichst große Grenzfläche zwischen gasförmiger und flüssiger Phase herzustellen. Je größer die Phasengrenzfläche ist, desto höher ist nach dem ersten Fick'schen Gesetz der Stofftransport zwischen Gas und Flüssigkeit. Die Gasdispergierung erfolgt dabei häufig in zwei Schritten: The goal of a gas dispersion is the introduction of gas into a fluid, preferably in the form of small bubbles as possible, to produce the largest possible interface between gaseous and liquid phase. The larger the phase interface, the higher the mass transfer between gas and liquid according to the first Fick's law. Gas dispersion often takes place in two steps:
1. Einbringen des Gases in die Flüssigkeit in Form von Blasen  1. introduction of the gas into the liquid in the form of bubbles
2. Zerteilen der Blasen  2. Parting the bubbles
Die Art des Einbringens, im Allgemeinen über Düsen, Fritten oder Lochplatten, bestimmt die Größenverteilung der Primärblasen. In dem Artikel„Gasdispergierung in Flüssigkeiten durch Düsen bei hohen Durchsätzen''' aus Chemie-Ingenieur-Technik, 28. Jahrgang 1956, Nr 6, Seiten 389 - 395 wird beispielsweise beschrieben, welchen Einfluss Parameter wie Düsenweite, Gasdurchsatz, Viskosität und Grenzflächenspannung auf die Größenverteilung von Gasblasen, die beim Hineinschießen eines Gasstrahls in eine Flüssigkeit aus einer Düse entstehen, haben. The type of introduction, generally via nozzles, frits or perforated plates, determines the size distribution of the primary bubbles. In the article "gas dispersion in liquids through nozzles at high flow rates' '' from Chemie-Ingenieur-Technik, 28th year 1956, No. 6, pages 389-395 is described, for example, what influence parameters such as nozzle size, gas flow, viscosity and interfacial tension on the size distribution of gas bubbles, which arise when injecting a gas jet into a liquid from a nozzle, have.
Das Zerteilen der Blasen kann beispielsweise mittels eines dynamischen oder statischen Mischers erfolgen. Während bei dynamischen Mischern die Homogenisierung einer Mischung durch bewegte Organe wie z.B. Rührer erreicht wird, wird bei statischen Mischern die Strömungsenergie des Fluids ausgenutzt: eine Fördereinheit (z.B. eine Pumpe) drückt die Flüssigkeit durch ein mit statischen Mischereinbauten versehenes Rohr, wobei die der Hauptströmungsachse folgende Flüssigkeit in Teilströme aufgeteilt wird, die je nach Art der Einbauten gedehnt, geschert, miteinander verwirbelt und vermischt werden. Der Vorteil bei der Verwendung von statischen Mischern liegt u. a. darin, dass keine beweglichen Teile vorhanden sind. The division of the bubbles can be done for example by means of a dynamic or static mixer. While in dynamic mixers, the homogenization of a mixture is achieved by moving organs such as stirrers, is static The feed fluid (eg a pump) pushes the liquid through a tube provided with static mixer inserts, wherein the liquid following the main flow axis is divided into partial flows which, depending on the type of internals, are stretched, sheared, intermixed and mixed become. The advantage of using static mixers is that there are no moving parts.
Einen Überblick über verschiedene Typen von statischen Mischern gibt zum Beispiel der Artikel Statische Mischer und ihre Anwendungen", M. H. Pähl und E. Muschelknautz, Chem.-Ing.-Techn. 52 (1980) Nr. 4, S. 285-291. Als Beispiele für statische Mischer seien SMX-Mischer (vgl. Patentschrift US4062524) oder SMXL-Mischer (vgl. z.B. Patentschrift US5520460) genannt. Sie bestehen aus zwei oder mehr zueinander senkrecht stehenden Gittern von parallelen Blechstreifen, die an ihren Kreuzungspunkten miteinander verbunden und in einem Winkel gegen die Hauptströmungsrichtung des Mischgutes angestellt sind, um die Flüssigkeit in Teilströme zu teilen und zu mischen. Ein einzelnes Mischelement ist als Mischer ungeeignet, da eine Durchmischung nur entlang einer Vorzugsrichtung quer zur Hauptströmungsrichtung erfolgt. Deshalb werden üblicherweise mehrere Mischelemente, die jeweils zueinander um 90° verdreht sind, hintereinander angeordnet. Die Verwendung statischer Mischer zur Dispergierung von Gas in einer Flüssigkeit ist bekannt. In WO2005/1031 15A1 wird zum Beispiel die Verwendung eines statischen Mis chers in einem V erfahren zur Herstellung von P o lycarb onat nach dem Umesterungsverfahren beschrieben. Um Monomere und andere flüchtige Bestandteile aus dem Polycarbonat zu entfernen, wird der Polymerschmelze ein Schäumungsmittel zugesetzt. Durch anschließende Druckerniedrigung entweicht das Schäumungsmittel unter Aufschäumen der Schmelze. Der Schaum bewirkt eine starke Oberflächenvergrößerung, die vorteilhaft für die Entgasung, d.h. die Entfernung flüchtiger Bestandteile ist. Als Schäumungsmittel wird bevorzugt ein inertes Gas wie z.B. Stickstoff eingesetzt, das mittels eines statischen Mischers, z.B. eines SMX-Mischers, in die Schmelze eingebracht und dispergiert wird. For an overview of various types of static mixers, see, for example, Static Mixers and Their Applications, "MH Pahl and E. Muschelknautz, Chem. Ing. 52 (1980) No. 4, pp. 285-291 Examples of static mixers are SMX mixers (see patent US4062524) or SMXL mixers (see, for example, US 5520460.) They consist of two or more mutually perpendicular lattices of parallel metal strips which are interconnected at their intersection points and in one An individual mixing element is unsuitable as a mixer since mixing takes place only along a preferential direction transverse to the main flow direction Therefore, usually several mixing elements, each to each other around 90 °, arranged one behind the other The use of static mixers for dispersing vo n Gas in a liquid is known. WO2005 / 103115A1, for example, describes the use of a static mixer in a process for the preparation of polyalkarate by the transesterification process. To remove monomers and other volatiles from the polycarbonate, a foaming agent is added to the polymer melt. By subsequent reduction in pressure, the foaming agent escapes with foaming of the melt. The foam causes a large increase in surface area, which is advantageous for degassing, i. the removal of volatiles is. As the foaming agent, an inert gas such as e.g. Nitrogen used by means of a static mixer, e.g. an SMX mixer, is introduced into the melt and dispersed.
In US2005/0094482A1 und US5480589 sind statische Mischer zur Dispergierung von Gasen zur Herstellung geschlossenzelliger Schäume beschrieben. Ein stufenförmiger Aufbau zur Erhöhung der Effektivität der Gasdispergierung ist nicht beschrieben. Bei der Dispergierung von Gas in eine Flüssigkeit sind im Allgemeinen größere Mischerlängen nötig als bei der Dispergierung von Flüssigkeiten. Ausgehend vom Stand der Technik stellt sich die Aufgabe, eine Vorrichtung und ein Verfahren zur Dispergierung von Gas in eine Flüssigkeit bereitzustellen, um eine effektivere Gasdispergierung als nach dem Stand der Technik beschrieben zu ermöglichen. Im Vergleich zum Stand der Technik soll bei gleicher Mischer länge eine kleinere mittlere Blasengröße am Mischeraustritt erzielt werden. Alternativ soll bei gleichem Druckverlust über den gesamten Mischer eine kleinere mittlere Blasengröße am Mischeraustritt erzielt werden. In US2005 / 0094482A1 and US5480589 static mixers for the dispersion of gases for the production of closed-cell foams are described. A step-shaped structure for increasing the effectiveness of the gas dispersion is not described. When dispersing gas into a liquid, generally longer mixer lengths are required than with the dispersion of liquids. Starting from the prior art, the object is to provide an apparatus and a method for dispersing gas in a liquid, to enable a more effective gas dispersion than described in the prior art. Compared to the prior art, a smaller average bubble size is to be achieved at the mixer outlet with the same mixer length. Alternatively, a smaller average bubble size should be achieved at the mixer outlet with the same pressure loss over the entire mixer.
Überraschend wurde gefunden, dass ein statischer Mischer, bei dem in Fließrichtung ein steigender spezifischer Energieeintrag vorliegt, über eine besonders effektive Dispergierwirkung verfügt. Es lassen sich mit Hilfe eines solchen Mischers bei vergleichbarem Gesamtdruckverlust kleinere Gasblasen erzeugen als mit einem statischen Mischer, bei dem der Energieeintrag über die Länge des Mischers konstant ist. Es lassen sich mit Hilfe eines solchen Mischers ebenfalls bei gleicher Gesamtmischer länge kleinere Gasblasen erzeugen als mit einem statischen Mischer, bei dem der Energieeintrag über die Länge des Mischers konstant ist. Surprisingly, it has been found that a static mixer in which there is an increasing specific energy input in the direction of flow has a particularly effective dispersing effect. With the aid of such a mixer, with comparable total pressure loss, smaller gas bubbles can be produced than with a static mixer in which the energy input over the length of the mixer is constant. With the aid of such a mixer, it is also possible to produce smaller gas bubbles at the same total mixer length than with a static mixer in which the energy input over the length of the mixer is constant.
Ein erster Gegenstand der vorliegenden Erfindung ist daher eine Vorrichtung zur Dispergierung von Gas in eine Flüssigkeit mit einer Anzahl n an aufeinander folgenden Zonen Zi, Z2, ... , Zn mit statischen Mischelementen, wobei jede Zone Z; eine Länge Lt und einen effektiven Durchmesser Dt aufweist, dadurch gekennzeichnet, dass die einzelnen Zonen so ausgeführt sind, dass der auf das jeweilige Verhältnis Lj/Dj normierte mechanische Energieeintrag Et, der auf das Gas-Flüssigkeits-Gemisch wirkt, in Fließrichtung von Zone zu Zone zunimmt, wobei n eine ganze Zahl größer oder gleich 3 ist und i ein Index ist, der die ganzen Zahl von 1 bis zur Anzahl n der Zonen durchläuft. Ein weiterer Gegenstand der vorliegenden Erfindung ist ein Verfahren zur Dispergierung von Gas in eine Flüssigkeit, bei dem Gas und Flüssigkeit gemeinsam durch eine Mischvorrichtung gefördert werden und dabei eine Anzahl n an aufeinander folgenden Zonen Zi, Z2, ... ,Zn mit statischen Mischelementen durchströmen, wobei jede Zone Z; eine Länge Lt und einen effektiven Durchmesser Dt aufweist, dadurch gekennzeichnet, dass der auf das jeweilige Verhältnis Lj/Dj normierte mechanische Energieeintrag Et, der auf das Gas- Flüssigkeits-Gemisch wirkt, in Fließrichtung von Zone zu Zone zunimmt, wobei n eine ganze Zahl größer oder gleich 3 ist und i ein Index ist, der die ganzen Zahl von 1 bis zur Anzahl n der Zonen durchläuft. A first subject of the present invention is therefore an apparatus for dispersing gas into a liquid having a number n of successive zones Zi, Z 2 , ..., Z n with static mixing elements, each zone Z; a length L t and an effective diameter D t , characterized in that the individual zones are designed so that the normalized to the respective ratio Lj / Dj mechanical energy input E t , which acts on the gas-liquid mixture, in the flow direction increases from zone to zone, where n is an integer greater than or equal to 3 and i is an index that traverses the integer from 1 to the number n of zones. Another object of the present invention is a method for dispersing gas into a liquid in which gas and liquid are conveyed together by a mixing device and thereby a number n of successive Zones Zi, Z 2 , ..., Z n flow through with static mixing elements, each zone Z; has a length L t and an effective diameter D t , characterized in that the normalized to the respective ratio Lj / Dj mechanical energy input E t , which acts on the gas-liquid mixture increases in the flow direction from zone to zone, wherein n an integer greater than or equal to 3, and i is an index that traverses the integer from 1 to the number n of zones.
Unter Flüssigkeit wird hier allgemein ein Medium verstanden, das durch die erfindungsgemäße Vorrichtung gefördert werden kann. Dabei kann es sich beispielsweise auch um eine Schmelze oder eine Dispersion (z.B. Emulsion oder Suspension) handeln. Im Folgenden wird auch der Begriff Fluid verwendet. Das Fluid ist dabei vorzugsweise höherviskos, d.h. es weist eine Viskosität zwischen 2 mPas und 10.000.000 mPas, besonders bevorzugt zwischen 1000 mPas und 1.000.000 mPas auf (gemessen in einem Kegel-Platte- Viskosimeter nach DIN 53019 bei einem Schergefälle von 1 s"1). Um ein Gas oder Gasgemisch in dem Fluid zu dispergieren, wird mechanische Energie in das Gemisch eingetragen. Dieser Energieeintrag wird durch statische Mischelemente realisiert. In der Mischtechnik ist die Verwendung von modularen Systemen üblich. Ein Mischer setzt sich aus einer Reihe von modularen Mischelementen zusammen. Zur Erhöhung der Mischwirkung kann die Zahl der Mischelemente in einem Mischer erhöht werden. Üblicherweise werden die Mischelemente zur Ausbildung eines statischen Mischers in ein Rohr eingebracht. Es sei daraufhingewiesen, dass die vorliegende Erfindung nicht auf Mischer beschränkt ist, die aus einer Anordnung modularer Mischelemente aufgebaut sind, sondern auch auf Mischer in kompakter Bauform Anwendung findet. Die erfindungsgemäße Vorrichtung zeichnet sich dadurch aus, dass sie über eine Anzahl n an aneinandergrenzenden Zonen verfügt, wobei n eine ganze Zahl größer oder gleich 3 ist. In jeder Zone liegen statische Mischelemente vor. Jede Zone Z; weist eine Länge Lt und eine Querschnittsfläche At auf. Dabei ist i ein Index, der die ganzen Zahl von 1 bis zur Anzahl n der Zonen durchläuft. Die Länge Lt einer Zone Z; entspricht der Länge der hintereinander angeordneter Mischelemente in dieser Zone; die Querschnittsfläche At entspricht der Querschnittsfläche der in der Zone Z; vorliegenden Mischelemente. Aus der Querschnittsfläche At lässt sich ein effektiver Durchmesser Dt nach Gleichung 1 errechn n: Liquid is generally understood here to mean a medium which can be conveyed through the device according to the invention. This may, for example, also be a melt or a dispersion (eg emulsion or suspension). In the following, the term fluid is used. The fluid is preferably of higher viscosity, ie it has a viscosity between 2 mPas and 10,000,000 mPas, more preferably between 1,000 mPas and 1,000,000 mPas (measured in a cone-plate viscometer according to DIN 53019 at a shear rate of 1 s "1). in order to disperse a gas or gas mixture in the fluid is entered mechanical energy into the mixture. This energy input is realized by static mixing elements. in the mixing art, the use of modular systems is common. a mixer is composed of a series of In order to increase the mixing effect, the number of mixing elements in a mixer can be increased.Usually, the mixing elements are introduced into a tube to form a static mixer.It should be noted that the present invention is not limited to mixers consisting of a mixing element Arrangement of modular mixing elements are constructed, but also on mixers in a compact Ba uform application finds. The device according to the invention is characterized in that it has a number n of contiguous zones, where n is an integer greater than or equal to 3. There are static mixing elements in each zone. Each zone Z; has a length L t and a cross-sectional area A t . Where i is an index that traverses the integer from 1 to the number n of zones. The length L t of a zone Z; corresponds to the length of the mixing elements arranged one behind the other in this zone; the cross-sectional area A t corresponds to the cross-sectional area of that in the zone Z; present mixing elements. From the cross-sectional area A t to an effective diameter D can t according to equation 1 errechn n:
Der effektive Durchmesser D, entspricht bei einem kreisförmigen Querschnitt dem Durchmesser des Kreises. Bei einem nicht-kreisförmigen (z.B. rechteckigem) Querschnitt entspricht der effektive Durchmesser Dt dem Durchmesser eines Kreises mit einer Fläche, die der Querschnittsfläche entspricht. The effective diameter D, corresponds in a circular cross section to the diameter of the circle. For a non-circular (eg, rectangular) cross section, the effective diameter D t is the diameter of a circle having an area corresponding to the cross-sectional area.
Das Verhältnis Lj/Dj ist eine für die jeweilige Zone Z; charakteristische Kennzahl. The ratio Lj / Dj is one for the respective zone Z; characteristic index.
Ein Mischelement verfügt über innere Strukturen und Kanäle zwischen diesen Strukturen. Wird ein Fluid durch ein Mischelement gefördert, so bewirken die Strukturen und Kanäle, dass das Fluid in Teilströme aufgeteilt, verteilt, geschert und ggf. verwirbelt wird und so die Teilströme miteinander vermischt werden. Der mittlere Durchmesser eines Kanals wird nachfolgend mit dem Buchstaben di abgekürzt. Unter einem mittleren Kanaldurchmesser di wird der über alle Kanäle arithmetisch gemittelte effektive Kanaldurchmesser verstanden, wobei sich der effektive Kanaldurchmesser analog dem effektiven Durchmesser einer Zone Z; nach Gleichung 1 berechnen lässt. A mixing element has internal structures and channels between these structures. If a fluid is conveyed through a mixing element, the structures and channels cause the fluid to be divided, distributed, sheared and, if necessary, fluidized into partial flows, thus mixing the partial flows with one another. The mean diameter of a channel is subsequently abbreviated by the letter di. A mean channel diameter di is understood to mean the channel diameter arithmetically averaged over all channels, the effective channel diameter corresponding to the effective diameter of a zone Z; can be calculated according to equation 1.
Das Verhältnis djlDj zwischen dem mittleren Kanaldurchmesser di und dem effektiven Durchmesser Dt der Mischelemente in einer Zone Z; ist ebenfalls eine charakteristische Kennzahl für die jeweilige Zone Z;. Der Parameter at bezeichnet dabei die offene Querschnittsfläche, genauer die Projektionsfläche des freien Querschnitts. So ergibt sich beispielsweise aus Fig. la die offene Querschnittsfläche a, aus der Summe der Projektionsflächen der einzelnen freien Querschnittsflächen der offenen Kanäle, durch die das Fluid durchströmen kann (Gleichung 3). The ratio djlDj between the mean channel diameter di and the effective diameter D t of the mixing elements in a zone Z; is also a characteristic index for the respective zone Z; The parameter a t denotes the open cross-sectional area, more precisely the projection surface of the free cross-section. Thus, for example, from FIG. 1a, the open cross-sectional area a, results from the sum of the projection areas of the individual free cross-sectional areas of the open channels, through which the fluid can flow (equation 3).
N  N
(3) Der Parameter m ist dabei ein Zählparameter, N ist die Anzahl der einzelnen freien Querschnittsflächen. (3) The parameter m is a counting parameter, N is the number of individual free cross-sectional areas.
Die nach dem Stand der Technik zur Gasdispergierung eingesetzten statischen Mischer verfügen über Mischeinbauten, die über die Länge des Mischers gleichbleibend sind. Hier liegt nur eine einzige Zone vor, deren Länge L der Länge des Mischers und dessen effektiver Durchmesser D dem effektiven Durchmesser des Mischers entspricht. Um die Dispergierwirkung eines solchen Mischers zu erhöhen, kann beispielsweise die Länge L erhöht werden. Mit der Länge des Mischers steigt der Druckverlust Δρ über den Mischer linear an. Der mechanische Energieeintrag Eabs ist gemäß Gleichung (4) proportional zum Druckverlust, wobei V der Volumenstrom des Fluids ist. The static mixers used in the prior art for gas dispersion have mixing internals that are consistent throughout the length of the mixer. Here there is only a single zone whose length L corresponds to the length of the mixer and whose effective diameter D corresponds to the effective diameter of the mixer. In order to increase the dispersing effect of such a mixer, for example, the length L can be increased. With the length of the mixer, the pressure drop Δρ increases linearly via the mixer. The mechanical energy input E abs is proportional to the pressure loss according to equation (4), where V is the volume flow of the fluid.
Eabs = Ap · V (4) Der Druckverlust Δρ und damit der mechanische Energieeintrag lässt sich in gleicher Weise auch durch eine Reduzierung des effektiven Durchmessers D erhöhen. E abs = Ap · V (4) The pressure loss Δρ and thus the mechanical energy input can be increased in the same way by a reduction of the effective diameter D.
Die erfindungsgemäße Vorrichtung zeichnet sich durch eine Anzahl n an Zonen aus. Jede Zone Z; ist durch einen spezifischen mechanischen Energieeintrag Et charakterisiert, der in ein Fluid, das die jeweilige Zone durchströmt, eingetragen wird. Der spezifische mechanische Energieeintrag Et ist der auf die Kennzahl Lj/Dj normierte mechanische Energieeintrag Eabs. Dabei ist erfindungsgemäß Ei < E2 < ... < E„. The device according to the invention is characterized by a number n of zones. Each zone Z; is characterized by a specific mechanical energy input E t , which is registered in a fluid flowing through the respective zone. The specific mechanical energy input E t is the mechanical energy input E abs normalized to the characteristic Lj / Dj. Here, according to the invention Ei <E 2 <... <E ".
E = E"bs ' D (5) E = E "bs' D (5)
L  L
Die Zahl n der Zonen in einer erfindungsgemäßen Vorrichtung ist nicht limitiert. Sie kann gegen unendlich laufen, wenn die Zonen infinitesimal klein werden und ein kontinuierlich steigender spezifischer Energieeintrag über die Länge der Vorrichtung vorliegt, wie es z.B. bei einem konisch enger werdenden Rohr der Fall sein könnte. Es ist denkbar, dass vor oder hinter den Zonen Zi bis Z„ weitere Zonen existieren, die frei wählbare spezifische Energieeinträge aufweisen. The number n of zones in a device according to the invention is not limited. It can run to infinity if the zones become infinitesimally small and there is a continuously increasing specific energy input along the length of the device, as might be the case, for example, with a conically narrowing tube. It is conceivable that further zones exist before or after the zones Zi to Z "which have freely selectable specific energy inputs.
So ist eine besonders bevorzugte Ausführungsform der erfindungsgemäßen Vorrichtung dadurch gekennzeichnet, dass es eine erste Zone Z0 gibt, die einen höheren spezifischen Energieeintrag leistet als die in Fließrichtung nachfolgende Zone Zi (Eo>Ei). Erfindungsgemäß folgen auf die Zone Zi weitere Zonen Z2 bis Zn, wobei für die entsprechenden spezifischen Energieeinträge Ei bis E„ gilt: Ei<E2<...<E„. Thus, a particularly preferred embodiment of the device according to the invention is characterized in that there is a first zone Z 0 , which provides a higher specific energy input than the downstream in the flow direction zone Zi (Eo> Ei). According to the invention following the zone Zi more zones Z 2 to Z n, where "applies: Egg <E 2 <... <E" for the respective specific energy inputs Ei-E.
Überraschend wurde festgestellt, dass durch eine solche Anordnung von Zonen durch die Zone Z0 Primärblasen erzeugt werden, die in den darauffolgenden Zonen weniger stark zur Koaleszenz neigen und somit eine effektivere Dispergierung erreicht wird. Surprisingly, it has been found that such an arrangement of zones through the zone Z 0 produces primary bubbles which are less prone to coalescence in the subsequent zones and thus a more effective dispersion is achieved.
In einer bevorzugten Ausführungsform verfügt die erfindungsgemäße Vorrichtung über eine Anzahl n an Mischzonen, die hintereinander angeordnet sind, wobei der mittlere Kanaldurchmesser dt in den Mischzonen in Fließrichtung kleiner wird. Durch kleinere Kanäle wird ein höherer Druckverlust pro Länge erzeugt, der gleichbedeutend mit einem zunehmenden spezifischen Energieeintrag ist. In a preferred embodiment, the device according to the invention has a number n of mixing zones, which are arranged one behind the other, wherein the mean channel diameter d t in the mixing zones in the flow direction is smaller. Smaller channels produce a higher pressure loss per length, which is equivalent to increasing specific energy input.
Bevorzugt umfasst diese Ausführungsform ein zylinderförmiges Rohr, in das Mischelemente eingebracht sind. Der effektive Durchmesser Dt der Mischelemente ist dabei bevorzugt über die gesamte Rohrlänge konstant, während der mittlere Kanaldurchmesser dt in aufeinanderfolgenden Zonen in Fließrichtung kleiner wird. Es gilt Dx = D2 = ... = Dn und d > d2 > ... > dn . This embodiment preferably comprises a cylindrical tube into which mixing elements are introduced. The effective diameter D t of the mixing elements is preferably constant over the entire tube length, while the mean channel diameter d t in successive zones in the flow direction is smaller. We have D x = D 2 = ... = D n and d> d 2 >...> d n .
Bevorzugt werden Mischelemente des gleichen Typs verwendet, z.B. SMX-Mischer mit unterschiedlichen Kennzahlen d/D. Preferably, mixing elements of the same type are used, e.g. SMX mixers with different ratios d / D.
In einer weiteren bevorzugten Ausführungsform verfügt die erfindungsgemäße Vorrichtung über eine Anordnung von Mischelementen, die in Fließrichtung bei konstantem Verhältnis di/Dj einen zunehmend geringeren effektiven Durchmesser Dt aufweisen. In a further preferred embodiment, the device according to the invention has an arrangement of mixing elements which have an increasingly smaller effective diameter D t in the flow direction at a constant ratio di / Dj.
., d, d^ d- d ., d, d ^ d-d
Es gilt -L = -2- = -!- ... = -2- und D. > D2 > ... > £> . We have -L = -2- = -! - ... = -2- and D.> D 2 >...>£>.
D2 Dn 1 2 Bevorzugt umfasst diese Ausfuhrungsform ein zylinderförmiges Rohr, in das Mischelemente eingebracht sind, die in Fließrichtung einen zunehmend kleineren effektiven Durchmesser Dt besitzen. D 2 D n 1 2 Preferably, this embodiment comprises a cylindrical tube into which mixing elements are introduced, which have an increasingly smaller effective diameter D t in the flow direction.
Die Mischelemente, deren Außendurchmesser kleiner ist als der Innendurchmesser des Rohres sind dabei bevorzugt mit einem Mantelrohr umschlossen, dessen Außendurchmesser annähernd dem Innendurchmesser des Rohres entspricht, um sie passend in das Rohr einbringen zu können. An den Übergangsstellen von einem Mischelement mit einem großen Durchmesser zu einem Mischelement mit einem kleinen Durchmesser sind bevorzugt Übergangsmantelrohre vorhanden, die über einen in Richtung des Mischelements mit kleinem Durchmesser konisch verjüngendem Innendurchmesser verfügen. Diese Übergangsmantelrohre können einstückig mit den Mantelrohren verbunden oder separat ausgeführt sein.  The mixing elements, whose outer diameter is smaller than the inner diameter of the tube are preferably enclosed with a jacket tube, the outer diameter of which approximately corresponds to the inner diameter of the tube in order to be able to fit into the tube. At the transition points from a mixing element with a large diameter to a mixing element with a small diameter, transition jacket tubes are preferably present, which have a conically tapering in the direction of the mixing element with a small diameter inner diameter. These transition jacketed tubes can be integrally connected to the jacket pipes or executed separately.
In einer weiteren bevorzugten Ausführungsform verfügt die erfindungsgemäße Vorrichtung in jeder Zone Z; über eine Anordnung von Mischelementen unterschiedlichen Typs, die bei gleichem Verhältnis Lj/Dj in Fließrichtung in jeder Zone Z; einen zunehmenden Druckverlust verursachen. In a further preferred embodiment, the device according to the invention has Z in each zone; via an arrangement of mixing elements of different types which, with the same ratio Lj / Dj in the flow direction in each zone Z; cause an increasing pressure loss.
Bevorzugt sind die Mischelemente in ein zylinderförmiges Rohr eingebracht. Sie verfügen bevorzugt über den gleichen effektiven Durchmesser Dj. Preferably, the mixing elements are introduced into a cylindrical tube. They preferably have the same effective diameter Dj.
Sollten die Außendurchmesser der Typen von Mischelementen variieren, so ist es denkbar, diejenigen Mischelemente, deren Außendurchmesser kleiner ist als der Innendurchmesser des Rohres, mit einem Mantelrohr bzw. Ring zu umschließen, dessen Außendurchmesser annähernd dem Innendurchmesser des Rohres entspricht, um sie passend in das Rohr einbring en zu können . Auch die oben beschriebene Verwendung von Übergangsmantelrohren ist hier vorteilhaft.  If the outer diameters of the types of mixing elements vary, it is conceivable to surround those mixing elements whose outer diameter is smaller than the inner diameter of the tube with a jacket tube or ring whose outer diameter corresponds approximately to the inner diameter of the tube to fit into the To be able to introduce pipe. The above-described use of transition jacketed pipes is advantageous here.
E s i st denkbar, die verschiedenen aufgeführten Ausführungsformen miteinander zu kombinieren. It is conceivable to combine the various embodiments listed with one another.
Die erfindungsgemäße Vorrichtung eignet sich zur Dispergierung von Gas in einer Flüssigkeit, z.B. zum Eintrag eines Schleppgases in eine Polymerschmelze oder zum Aufschäumen von flüssigen Medien. Das Gas kann mit Röhrchen oder dünnen Kapillaren, die sich vorzugsweise in Fließrichtung vor der Statikmischerkaskade befinden, zugegeben werden. Weiterhin kann das Gas auch durch einen porösen Körper zugegeben werden. Ein poröser Körper kann beispielsweise folgende Geometrien umfassen: eine Fritte und/oder einen porösen, gesinterten Körper und/oder ein ein- oder mehrlagiges Sieb. The device according to the invention is suitable for the dispersion of gas in a liquid, for example for introducing a towing gas into a polymer melt or for foaming liquid media. The gas may be added with tubes or thin capillaries, preferably in the flow direction before the static mixer cascade. Furthermore, the gas may also be added through a porous body. A porous body may comprise, for example, the following geometries: a frit and / or a porous, sintered body and / or a single or multi-layer sieve.
Der poröse Körper kann beispielsweise in Form eines Zylinders, in Form eines Quaders, einer Kugel oder eines Würfels oder in konischer Form, z.B. als Kegel, ausgeformt sein. Diese Vorrichtungen sorgen für eine feine Vordispergierung des Gases sowie ggf. auch für eine Verteilung des Gases über den Querschnitt.  The porous body may, for example, be in the form of a cylinder, in the form of a cuboid, a sphere or a cube or in conical form, e.g. as a cone, be formed. These devices ensure a fine predispersion of the gas and possibly also for a distribution of the gas over the cross section.
Die Kapillare bzw. der p orö s e K örp er weist einen mittleren effektiven Lochinnendurchmesser von vorzugsweise 0, 1-500 μιη, bevorzugt 1 - 200 μιη, besonders bevorzugt 10-90 μιη auf. The capillary or the porous body has a mean effective internal hole diameter of preferably 0.1 to 500 μm, preferably 1 to 200 μm, particularly preferably 10 to 90 μm.
Als poröse Körper können beispielsweise poröse Sinterkörper aus Metall zum Einsatz kommen, wie Frittenkörper, welche in der Chromatographie verwendet werden, z.B. die Sinterkörper der Fa. Mott Corporation (Farmington, USA). Weiterhin können gewickelte Drahtgewebe zum Einsatz kommen, beispielsweise die gewickelten Drahtgewebe der Fa. Fuji Filter Manufacturing Co., Ltd. (Tokyo, Japan), Handelsname: Fujiloy®. Weiterhin können Siebe oder mehrlagige Gewebe zum Einsatz kommen, wie z.B. die Metall- Drahtgewebe- Verbundplatten der F a . H äv er & Boecker Drahtweberei (Oelde, Deutschland), Handelsname: Häver Porostar. Porous bodies which may be used are, for example, porous sintered bodies of metal, such as frit bodies used in chromatography, for example the sintered bodies of Mott Corporation (Farmington, USA). Furthermore, wound wire mesh can be used, for example, the wound wire mesh from Fuji Filter Manufacturing Co., Ltd. (Tokyo, Japan), trade name: Fujiloy ®. Furthermore, sieves or multi-layered fabrics can be used, such as the metal wire mesh composite panels of F a. Häv er & Boecker Wire Weaving (Oelde, Germany), trade name: Häver Porostar.
Diese Vorrichtungen dienen der Verteilung des Gases über den Rohrquerschnitt und einer für die Gasdispergierung günstigen Vordispergierung über die engen Poren. Der effektive Durchmesser Dt der in den porösen Sinterkörpern oder Sieben oder gewickelten Drahtgeweben eingesetzten Löchern beträgt bevorzugt 1-500 μηι, besonders bevorzugt 2 - 200 μηι, ganz besonders bevorzugt 10-90 μιη. These devices serve the distribution of the gas over the pipe cross-section and a predispersion for the gas dispersion over the narrow pores. The effective diameter D t of the holes inserted in the porous sintered bodies or wires or wound wire meshes is preferably 1-500 μm, particularly preferably 2-200 μm, very particularly preferably 10-90 μm.
Die Erfindung wird nachstehend anhand von Beispielen näher erläutert ohne sie jedoch hierauf zu beschränken. The invention is explained in more detail below by means of examples without, however, limiting them thereto.
Fig. 1 zeigt Bespiele von drei unterschiedlichen erfindungsgemäßen statischen Mischern (No. l , No. 2 und No. 3): Fig. 1(a) von oben, Fig. 1(b) von der Seite (Schnittzeichnung) und Fig. 1 (c) in der Anordnung nach Einbau in ein Rohr oder Gehäuse. Die Angaben für wi und bi bezeichnen die Länge bzw . Breite des projizierten Querschnitts der freien Strömungskanäle. Di bezeichnet den lichten Durchmesser und DM den Außendurchmesser der statischen Mischelemente. Li bezeichnet die gesamte Länge eines geometrisch gleichförmigen Mischerabschnitts und Ii die Länge eines einzelnen Mischelements. Fig. 1 shows examples of three different static mixers according to the invention (No. 1, No. 2 and No. 3): Fig. 1 (a) from above, Fig. 1 (b) from the side (sectional drawing) and Fig. 1 (c) in the arrangement after installation in a pipe or housing. The data for wi and bi indicate the length resp. Width of the projected cross section of the free flow channels. Di denotes the clear diameter and DM the outer diameter of the static mixing elements. Li denotes the entire length of a geometrically uniform mixer section and Ii the length of a single mixing element.
No. 1 stellt einen Kenics-Mischer dar. No.2 zeigt einen handelsüblichen SMX- Statikmischer ohne bzw. mit äußerem Ring. No. 3 zeigt einen Mischer mit Stegstruktur und äußerem Ring (DE 29923895U1 und EP1 189686B1). No. 1 shows a Kenics mixer. No.2 shows a commercially available SMX static mixer without or with an outer ring. No. 3 shows a mixer with web structure and outer ring (DE 29923895U1 and EP1 189686B1).
Fig. 2 zeigt drei verschiedene Beispiele (A, B und C) von Varianten erfindungsgemäßer Statikmischer, mit einzelnen Zonen (gekennzeichnet durch die Längenangaben Li, L2, L3), dadurch gekennzeichnet, dass der auf das jeweilige Verhältnis Lj/Dj der einzelnen Zonen normierte mechanische Energieeintrag Et auf ein Fluid, das die jeweilige Zone Z; durchströmt, in Fließrichtung zunimmt. Die Fließrichtung wird durch den dicken Pfeil angegeben. Fig. 2 shows three different examples (A, B and C) of variants of static mixer according to the invention, with individual zones (characterized by the lengths Li, L 2 , L 3 ), characterized in that the respective ratio Lj / Dj of the individual Zones normalized mechanical energy input E t to a fluid containing the respective zone Z; flows through, increases in the flow direction. The flow direction is indicated by the thick arrow.
Fig. 2 A zeigt eine Abfolge von statischen Mischern mit geometrisch ähnlicher Struktur und einer Anordnung von Mischelementen, die in Fließrichtung bei konstantem Verhältnis d einen zunehmend geringeren effektiven Durchmesser Dt aufweisen. FIG. 2A shows a sequence of static mixers with a geometrically similar structure and an arrangement of mixing elements which have an increasingly smaller effective diameter D t in the direction of flow at a constant ratio d.
Es gilt ^L = ^ = ^L und n > D > D We have ^ L = ^ = ^ L and n>D> D
D2 D3 D 2 D 3
Fig . 2 B zeigt eine Aus führungsform mit einem zylinderförmigen Rohr, in das Mischelemente eingebracht sind, bei denen der effektive Durchmesser Dt über die gesamte Rohrlänge konstant ist, während der mittlere Kanaldurchmesser d; in aufeinanderfolgenden Zonen in Fließrichtung kleiner wird. Es gilt Dx = D2 = D3 und dx > d2 > d3 . Es werdenFig. 2 B shows an embodiment with a cylindrical tube into which mixing elements are introduced, in which the effective diameter D t is constant over the entire tube length, while the mean channel diameter d; becomes smaller in successive zones in the flow direction. D x = D 2 = D 3 and d x > d 2 > d 3 . It will
Mischelemente des gleichen Typs verwendet, z.B. SMX-Mischer mit unterschiedlichen Kennzahlen d/D. Fig. 2 C zeigt eine Anordnung von Mischelementen unterschiedlichen Typs, die bei gleichem Verhältnis Lj/Dj in Fließrichtung in jeder Zone Z; einen zunehmenden Druckverlust verursachen. Als Beispiel ist hier in der ersten Zone mit der Länge LI ein Kenics-Mischer dargestellt. In der zweiten Zone mit der Länge L2 befindet sich ein SMX-Mischer. In der dritten Zone mit der Länge L3 befindet sich ebenfalls ein SMX-Mischer mit geringeren effektiven Durchmesser Dt im Vergleich zu dem Mischer in der zweiten Zone. Used mixing elements of the same type, eg SMX mixers with different ratios d / D. Fig. 2C shows an arrangement of mixing elements of different types which, with the same ratio Lj / Dj in the flow direction in each zone Z; cause an increasing pressure loss. As an example, here in the first zone of length LI is a Kenics mixer shown. In the second zone of length L2 is an SMX mixer. In the third zone of length L3 is also an SMX mixer with smaller effective diameter D t compared to the mixer in the second zone.
Fig. 3A zeigt eine erfindungsgemäße Vorrichtung mit drei Zonen und einem Vormischer sowie einer Gasdosierung über eine Kapillare. Vor dem Vormischer befindet sich der Bereich, bei dem das Fluid dosiert wird (L) sowie eine Vorrichtung zur Dosierung von Gasen (G) über eine Kapillare (Ca). Fig. 3A shows a device according to the invention with three zones and a premixer and a gas metering via a capillary. Before the premixer is the area where the fluid is metered (L) and a device for metering gases (G) via a capillary (Ca).
Fig. 3B zeigt eine Gasdosierung mittels porösem Sinterkörper (der dahinter liegende Mischer ist hier nicht eingezeichnet). Vor dem Vormischer befindet sich der Bereich, bei dem das Fluid dosiert wird (L) und eine Vorrichtung zur Gasdosierung (G) über einen porösen Sinterkörper (PS), welcher sich innerhalb des Strömungsquerschnitts befindet. FIG. 3B shows a gas metering by means of a porous sintered body (the mixer behind it is not shown here). In front of the premixer is the area where the fluid is metered (L) and a device for gas metering (G) via a porous sintered body (PS), which is located within the flow cross section.

Claims

Patentansprüche claims
Vorrichtung zur Dispergierung von Gas in eine Flüssigkeit mit einer Anzahl n an aufeinander folgenden Zonen Zi, Z2, ... , Zn mit statischen Mischelementen, wobei jede Zone Z; eine Länge Lt und einen effektiven Durchmesser Dt aufweist, dadurch gekennzeichnet, dass die einzelnen Zonen so ausgeführt sind, dass der auf das jeweilige Verhältnis Lj/Dj normierte mechanische Energieeintrag Et, der auf eine Flüssigkeit wirkt in Fließrichtung von Zone zu Zone zunimmt, wobei n eine ganze Zahl größer oder gleich 3 ist und i ein Index ist, der die ganzen Zahl von 1 bis zur Anzahl n der Zonen durchläuft. Apparatus for dispersing gas into a liquid having a number n of successive zones Zi, Z 2 , ..., Z n with static mixing elements, each zone Z; has a length L t and an effective diameter D t , characterized in that the individual zones are designed so that the normalized to the respective ratio Lj / Dj mechanical energy input E t , which acts on a liquid increases in the flow direction from zone to zone where n is an integer greater than or equal to 3 and i is an index that traverses the integer from 1 to the number n of zones.
Vorrichtung nach Anspruch 1 , dadurch gekennzeichnet, dass der mittlere Kanaldurchmesser dj in den in Fließrichtung aufeinander folgenden Zonen Zi bis Zn kleiner wird. Apparatus according to claim 1, characterized in that the mean channel diameter dj in the successive zones Zi to Z n in the flow direction is smaller.
Vorrichtung nach Anspruch 1 , dadurch gekennzeichnet, dass die in den Zonen Zi bis Zn vorliegenden Mischelemente dasselbe Verhältnis djlDj und einen in Fließrichtung von Zone zu Zone zunehmend geringeren effektiven Durchmesser aufweisen. Apparatus according to claim 1, characterized in that the mixing elements present in the zones Zi to Z n have the same ratio djlDj and an increasingly smaller in the flow direction from zone to zone effective diameter.
Vorrichtung nach Anspruch 1 , dadurch gekennzeichnet, dass die Zonen Zi bis Zn über Mischelemente unterschiedlichen Typs verfügen, die bei gleichem Verhältnis LJDi in Fließrichtung von Zone zu Zone einen zunehmenden Druckverlust verursachen. Apparatus according to claim 1, characterized in that the zones Zi to Z n have mixing elements of different types, which cause an increasing pressure loss at the same ratio LJDi in the flow direction from zone to zone.
Vorrichtung nach einem der vorangegangenen Ansprüche, dadurch gekennzeichnet, dass es eine erste Zone Z0 gibt, die einen höheren spezifischen Energieeintrag E0 leistet als die in Fließrichtung nachfolgende Zone Zi. Device according to one of the preceding claims, characterized in that there is a first zone Z 0 , which makes a higher specific energy input E 0 as the downstream in the flow direction zone Zi.
Vorrichtung nach einem der Ansprüche 1 bis 5, weiterhin umfassend ein Röhrchen oder eine dünne Kapillare zur Zuführung von Gas in die Vorrichtung, dadurch gekennzeichnet, dass das Röhrchen oder die dünne Kapillare vor der Anordnung aus Mischelementen angebracht ist. Vorrichtung nach einem der Ansprüche 1 bis 5, weiterhin umfassend einen porösen oder siebförmigen Körper zur Zuführung von Gas in die Vorrichtung, dadurch gekennzeichnet, das der Körper vor der Anordnung aus Mischelementen angebracht ist. Device according to one of claims 1 to 5, further comprising a tube or a thin capillary for supplying gas into the device, characterized in that the tube or the thin capillary is mounted before the arrangement of mixing elements. Device according to one of claims 1 to 5, further comprising a porous or sieve-shaped body for supplying gas into the device, characterized in that the body is mounted before the arrangement of mixing elements.
Verfahren zur Dispergierung von Gas in eine Flüssigkeit, bei dem Gas und Flüssigkeit gemeinsam durch eine Mischvorrichtung gefördert werden und dabei eine Anzahl n an aufeinander folgenden Zonen Zi, Z2,... ,Zn mit statischen Mischelementen durchströmen, wobei jede Zone Z; eine Länge Lt und einen effektiven Durchmesser Dt aufweist, dadurch gekennzeichnet, dass der auf das jeweilige Verhältnis Lj/Dj normierte mechanische Energieeintrag Et, der auf das Gas- Flüssigkeits-Gemisch wirkt, in Fließrichtung von Zone zu Zone zunimmt, wobei n eine ganze Zahl größer oder gleich 3 ist und i ein Index ist, der die ganzen Zahl von 1 bis zur Anzahl n der Zonen durchläuft. Method for dispersing gas into a liquid, in which gas and liquid are jointly conveyed through a mixing device and thereby flow through a number n of successive zones Zi, Z 2 , ..., Z n with static mixing elements, each zone Z; has a length L t and an effective diameter D t , characterized in that the normalized to the respective ratio Lj / Dj mechanical energy input E t , which acts on the gas-liquid mixture increases in the flow direction from zone to zone, wherein n an integer greater than or equal to 3, and i is an index that traverses the integer from 1 to the number n of zones.
Verfahren nach Anspruch 8, dadurch gekennzeichnet, dass die Flüssigkeit eine Viskosität zwischen 2 mPas und 10.000.000 mPas, besonders bevorzugt zwischen 1000 mPas und 1.000.000 mPas aufweist. A method according to claim 8, characterized in that the liquid has a viscosity between 2 mPas and 10,000,000 mPas, more preferably between 1000 mPas and 1,000,000 mPas.
EP11723393.2A 2010-08-24 2011-05-19 Device and method for gas dispersion Active EP2608875B1 (en)

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