EP2459307A2 - Réacteur de cavitation - Google Patents

Réacteur de cavitation

Info

Publication number
EP2459307A2
EP2459307A2 EP10725388A EP10725388A EP2459307A2 EP 2459307 A2 EP2459307 A2 EP 2459307A2 EP 10725388 A EP10725388 A EP 10725388A EP 10725388 A EP10725388 A EP 10725388A EP 2459307 A2 EP2459307 A2 EP 2459307A2
Authority
EP
European Patent Office
Prior art keywords
flow
cavitation
micro
section
reactor according
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.)
Withdrawn
Application number
EP10725388A
Other languages
German (de)
English (en)
Inventor
Dominik Maslak
Dirk Weuster-Botz
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.)
Technische Universitaet Muenchen
Original Assignee
Technische Universitaet Muenchen
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 Technische Universitaet Muenchen filed Critical Technische Universitaet Muenchen
Publication of EP2459307A2 publication Critical patent/EP2459307A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/006—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
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/41—Emulsifying
    • 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
    • B01F25/4335—Mixers with a converging-diverging cross-section
    • 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
    • B01F25/45—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads
    • 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
    • B01F25/45—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads
    • B01F25/452—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads characterised by elements provided with orifices or interstitial spaces
    • B01F25/4521—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads characterised by elements provided with orifices or interstitial spaces the components being pressed through orifices in elements, e.g. flat plates or cylinders, which obstruct the whole diameter of the tube
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/008—Processes for carrying out reactions under cavitation conditions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/34—Treatment of water, waste water, or sewage with mechanical oscillations
    • 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
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/0318—Processes

Definitions

  • the invention relates to a method and to a method using the cavitation reactor for generating hydrodynamic, homogeneous and oscillating cavitation bubbles. Furthermore, the invention encompasses a method for disinfecting a fluid, or the manipulation of biological membranes and cells, and a method for emulsifying or suspending or favoring the reaction of at least two substances.
  • Hydrodynamic cavitation is not yet developed in this respect.
  • the generation of hydrodynamic cavitation is limited to Venturi nozzles and their procedural description or modeling is based on fundamental fluid mechanical and geometric relationships and key figures.
  • the biologically interesting aspect of bubble oscillation is not considered in the field of hydrodynamic cavitation.
  • the pure intensity, described by the cavitation number, or the bubble collapse pressure as a measure of the effectiveness serves.
  • Cavitation describes the phenomenon of vapor bubble formation by local pressure reduction. It corresponds to the state change of a liquid into the gas phase at temperatures below the evaporation temperature. This effect is usually triggered by existing micro-gas bubbles or other impurities present in the water, such as particles or microbiological cells.
  • the local pressure reduction can be caused by changing the sound pressure (acoustically) or hydrodynamically by increasing the flow velocity. Usually mixed forms of vapor and gas bubbles are formed or both forms are present in a cavitation bubble. As long as there are favorable pressure conditions for the vapor pressure, or as long as rapidly changing pressure conditions are present, the bubbles undergo a period of oscillation with rapid and strong volume changes.
  • the initiation and the strength of the cavitation depend significantly on the flow velocity and the local turbulence.
  • An initiation for water and aqueous solutions at 20 ° C. and under atmospheric pressure conditions is possible as early as a velocity of 14 ms "1.
  • Characteristic of the hydrodynamic cavitation is often a turbulence-dependent pulsating generation of cavitation at corresponding surfaces and stalls or vortices. This generation is superimposed on the outside to a seemingly continuous cavitation. In reality, they dissolve However, usually swarms of bubbles and bubble fields in high frequency on corresponding surfaces or known from, until again builds a new front. This leads to a truly inhomogeneous and discontinuous impingement of the flow with cavitation or vapor bubbles.
  • a cavitation-induced transient perforation of tissue cells is known, which is used, for example, to infiltrate substances into cells.
  • the bubbles are often provided as stabilized microbubbles or also known as ultrasound contrast agents.
  • the excitation of these microbubbles is carried out by ultrasound of suitable intensity and frequency. Due to the rapid oscillations and pressure fluctuations of the oscillating bubbles, the cell membrane can be perforated in the short term and thus short-term stable hydrophilic pores in the cell membrane can be created. Through these pores, a diffusion process or mass transport into the cell can be significantly accelerated.
  • radical bladder collapse which can cause lasting damage to cells and even lethal ones, can also be seen.
  • cavitation is suitable for disrupting cells or for specifically destroying the cell envelopes and membranes.
  • the damage to e.g. Yeast cells are visualized by microscopic images.
  • studies on cell digestion behavior and protein release have been carried out under various process conditions and biochemical factors such as e.g. the growth state of E. coli.
  • cavitation usually arises by stall. This creates a temporally inhomogeneous state of vapor bubble formation with a change from three states: construction of bubble clusters, detachment of the flow and the bubble cluster and short-term homogeneous flow around the component or the edge without blistering.
  • the initiative generation of vapor bubbles usually occurs in the turbulent flow fields in the immediate vicinity of stall edges. A large part of the flow is spared from this initial generation of cavitation bubbles. Only the turbulent dynamics of the surrounding bubble clusters can cause further spontaneous cavitation formation in these zones.
  • known solutions can not maintain a temporally or spatially extended oscillation field for bubbles.
  • the task includes the optimization of the hydrodynamic cavitation, in order to create the most homogeneous bubble distribution in a liquid volume and stable, oscillating bubble fields over adjustable periods of time. This is intended to be a better and more economical compared to known methods and devices for hydrodynamic or acoustic cavitation Possibility for cell manipulation, reaction favoring or emulsion production can be achieved.
  • the object also includes the use for the mixing of liquids and solids for better stabilization or formation of a suspension.
  • for the comminution and deagglomeration of particles and for general enhancement of reactions that require a strong mixing and targeted energy input such as the catalytic conversion of substances and diffusion-limited reactions.
  • a cavitation reactor for the hydrodynamic generation of homogeneous, oscillating cavitation bubbles in a fluid, comprising forming a flow channel and arranged successively in the flow direction of the fluid, an acceleration section designed to increase a flow velocity, a diaphragm arranged transversely to the flow direction with a plurality of for the generation of cavitation bubbles formed micro-passages, wherein over a total, defined on a flowed side of the aperture flow cross-sectional area at least 10 micro-passages per cm 2 are formed, stabilizing an oscillation of cavitation bubbles formed stabilizing portion, and a collapse portion with at least one expansion of a flow cross-sectional area of the flow channel in the flow direction.
  • the aperture on which the cavitation is formed thus comprises a large number of micro-passages or micro-holes. Looking at the surface of the diaphragm facing the flow, at least 10 of these micro-passages per cm 2 can be seen here.
  • the micro-passages are distributed uniformly over the entire surface that has been flowed on.
  • the pressure of the fluid relative to a normal pressure at the end of the cavitation reactor is further increased by means of preferably a pump.
  • the speed of the fluid flow is preferably increased by a multiple.
  • the novel geometry according to the invention optimally combines one energetically efficient and spatially and temporally homogeneous generation of cavitation and vapor bubbles. Furthermore, the generated bubble field is stably maintained in a dynamically oscillating state in a region of high flow velocity and deliberately forced to a final collapse only very late. Thus, the theoretically described requirements for cell manipulation or membrane perforation by cavitation are met to a very high degree.
  • the flow cross-sectional area in the acceleration section continuously narrows in the flow direction.
  • a constant-running pump is used in front of the acceleration section. Due to the narrowing flow cross section in front of the aperture, the fluid is then accelerated.
  • the acceleration section comprises an inner nozzle cone which narrows in the flow direction and extends to the diaphragm, so that the flow cross-sectional areas in the acceleration section and the flow cross-sectional area of the diaphragm are annular.
  • the aperture can be advantageously attached to the end of this nozzle cone. As a result, a stable mounting of the aperture is possible. Furthermore, the nozzle cone allows a very narrow narrowing of the flow cross-sectional area in the acceleration section.
  • the nozzle cone converges before the acceleration section to a point pointing in the direction of flow.
  • the inflowing fluid is split into a ring shape as far as possible without turbulence.
  • the acceleration section for generating a twist in the fluid comprises helical wall elements.
  • a swirl is brought about for a better mixing of the flow lines.
  • the flow cross-sectional area decreases over the acceleration range, ie from the beginning of the acceleration range to the beginning of the diaphragm, by 70% to 99%, in particular 80% to 96%, in particular 90% to 93%.
  • the flow cross-sectional area of the preferably annular diaphragm has at least 26, in particular at least 50, in particular at least 100, in particular at least 150, in particular at least 200, micro-passages. The more micro-passages the aperture has, the more demolition edges are available for cavitation bubble formation.
  • the micro-passages each have a passage area ⁇ 3 mm 2 , in particular ⁇ 2 mm 2 , in particular between 0.01 mm 2 and 1 mm 2 , in particular between 0.1 mm 2 and 0.2 mm 2 .
  • the passage area of the micro-passages is to be measured when viewed perpendicularly to the flow cross-sectional area of the diaphragm, in which case the clear passage area is decisive.
  • the decisive factor here is that most of the micro-passages correspond to the given orders of magnitude.
  • At least 20, in particular at least 50, in particular at least 100, in particular at least 200, in particular at least 1000, micro-passages per cm 2 are formed over the entire flow cross-sectional area defined on the flowed-on side of the diaphragm.
  • the more micro-passages per area that is flown on, the more break-off edges are available for cavitation bubble formation.
  • the bubble and cavitation generation fluctuates over more micro-passages and the bubble clusters break at different times so that a quasi-spatial, temporal, stationary and homogeneous cavitation bubble field arises
  • the micro-passages of the diaphragm are round or angular, in particular square or diamond-shaped. Due to the different configuration of the micro-passages, a certain number of micro-passages per area can be arranged for a given size. It is both preferable to provide micro-passages of different shape within a diaphragm, as well as to form a diaphragm with micro-passages exclusively in a mold.
  • the diaphragm is designed as a micro-grid or micro-tissue.
  • a material with a diameter of 0.01 mm to 1, 0 mm, in particular from 0.1 mm to 0.3 mm, in particular of 0.2 mm is used for the micro-grid or micro-fabric.
  • the preferred micro-passages have a mesh size of 0.1 mm to 1, 7 mm, in particular 0.2 mm to 0.8 mm, in particular 0.4 mm.
  • the mesh size is defined as the inside width of the mesh.
  • the mesh width is thus the inside width between two adjacent parallel wires or fabric threads.
  • Other embodiments may be diamond-shaped and entirely Provide parallel alignment of the micro-passages in the diaphragm plane.
  • preferably parallel wires or rods are used.
  • a metal wire with a round or angular or triangular cross-section is used for the material of the micro-grid or micro-fabric. Due to the special configuration of the wire cross-section, the condition of the cavitation and in particular the turbulence and vortex formation and thus the detachment of the cavitation bubbles from the grid can be influenced.
  • the wire is used with an isosceles, triangular cross-section, wherein the wire is arranged in the grid such that the apex of the triangle turns counter to the flow direction and thus the flow along the two legs is split.
  • the aperture As an alternative to the design of the aperture as a micro-grid or micro-tissue, it is preferable to form the aperture as a micro-well plate, especially in the case of large flow cross-sections, the more stable micro-well plate can be used instead of the micro-grid or micro-tissue.
  • the micro-passages can also have the properties described above, be square in shape, diamond-shaped or rectangular or be formed as a one-dimensional columns.
  • the axial configuration can also be designed preferably in the form of triangles tapering in the direction of flow.
  • the thickness of the micro-hot plate should preferably be 0.1 times to 50 times a diameter or the edge length of a square or rectangular micro-passage, in particular 0.3 times to 5 times, in particular 0.5 times to 2 -fold.
  • micro-grid or a micro-tissue preferably with a linkage
  • this configuration can be used stably with large flow cross-sections.
  • a porous material is to be listed.
  • a porous material instead of micro-plates or micro-grids also a porous material form the diaphragm.
  • extremely small micro-passages can be realized in a confined space.
  • the flow cross-sectional area over the stabilization section increases slightly or is constant throughout. This very slight change of the Flow cross-section and the constant flow cross-section does not preclude that due to structural design shortly after the aperture a small jump-like flow cross-sectional widening can take place.
  • the flow cross-sectional area at the beginning of the stabilization section corresponds to 100% to 200%, in particular 110% to 150%, in particular 120% to 130% of the flow cross-sectional area of the preferably annular diaphragm.
  • the widening in relation to the permeable area of the micro-passages is preferably 200% to 1000%, in particular 250% to 600%, in particular 280% to 300%.
  • the axial length of this stabilizing section is preferably 3 to 75 times, preferably 5 to 45 times, preferably 7 to 15 times the tube diameter of this section. Due to this relatively small expansion after the aperture, on the one hand, the cavitation bubbles are kept stable oscillating, on the other hand, the cavitation bubbles have enough space to be distributed homogeneously.
  • the flow cross-sectional area in the collapse section widens in the collapsing section, which adjoins the stabilization section directly. It is preferable for the flow cross-sectional area in the collapse section to expand in a large step by 10 to 30 times the flow area of the stabilization section and / or in a plurality of small steps, preferably in the steps of 0.01 times to 1 times, in particular expands by 0.1 times to 0.3 times the diameter of the stabilizing section and / or with a constant opening angle and / or with different continuously or discontinuously merging opening angles, preferably angles of 2 ° -20 °, in particular angles of 4 ° - 10 °.
  • a defined and discrete end of the cavitation bubbles can be realized.
  • the cavitation reactor comprises a forward flow section arranged in the flow direction directly in front of the acceleration section and having flow rectifiers for calming the fluid.
  • the already described, pointing in the direction of flow tip of the nozzle cone extends into this forward section into it.
  • the invention further comprises a method for the hydrodynamic generation of homogeneous, oscillating cavitation bubbles in a fluid, comprising the following steps in the order given: accelerating the fluid, flowing a diaphragm with a plurality of micrometers through with the fluid for generating the cavitation bubbles, via an entire flow cross-sectional area defined on a flow-side of the orifice is formed at least 10 micro-passages per cm 2 , stabilizing an oscillation of the cavitation bubbles, and expanding a flow cross-sectional area of the fluid along the flow direction to collapse the cavitation bubbles.
  • the invention comprises a method for disinfecting a fluid, comprising the method just described for the hydrodynamic generation of homogeneous, oscillating cavitation bubbles, wherein prior to the flow of the plurality of micro-passages, the fluid is mixed with disinfectant, in particular disinfecting fluid.
  • a bacterial count in the fluid is determined before the fluid is displaced with disinfectant and / or after the flow cross-section has been widened.
  • the fluid circuit can be controlled according to these measurements.
  • the adaptation of the cavitation conditions or the amount of disinfectant, and a possibly required renewed passage of the cavitation reactor or a passage through a further downstream cavitation reactor can be regulated.
  • the invention further comprises a process for emulsifying or suspending or for promoting the reaction of at least two substances, in particular two liquids or a liquid and a solid or a liquid and a gas, comprising the already described method for the hydrodynamic generation of homogeneous, oscillating cavitation bubbles, wherein the Fluid is composed before the flow of the diaphragm from the at least two different substances.
  • ethanol and / or water and / or an adjuvant is added to the fluid.
  • the cavitation allows the smallest units of the liquids and / or solid particles to be mixed to be stirred through, so that a comminution of the droplets and / or solid units results, which leads to a stable emulsion or suspension.
  • cavitation increases the interface between two liquids so that they can optimally react with each other, or the mass transport across the phase boundary is favored.
  • the advantageous embodiments of the cavitation reactor according to the invention already described also find appropriate application to the process for emulsifying or favoring the reaction of diffusion-limited or catalytic reactions which are positively influenced by high mixing and turbulence.
  • biological materials in particular biological cells and their cell envelopes and membranes.
  • the cell-perforating effect of oscillating cavitation bubbles can advantageously be used in combination with disinfectants.
  • Most disinfectants can not pass the membrane of the cell or only with high diffusion pressure or high concentration. The effect is thus limited to the surface although the best site of action would be in the bacterial cell, e.g. at the DNA or RNA or intracellular enzymes and enzyme complexes, and there would more quickly lead to lethal inactivation.
  • Particularly advantageous is a combination of chlorine dioxide with oscillating cavitation.
  • an increase in inactivation since the transient perforation of the cell membrane, the chlorine dioxide can diffuse better and faster to the site of action in the cell.
  • the disinfectant from a template by metering pump in the main stream in an adjusted amount, dosed.
  • an ideal premix of the disinfectant already arises in the pump.
  • the invention comprises a method for hydrodynamically generated short-term cell and membrane manipulation, comprising the method for the hydrodynamic generation of homogeneous, oscillating cavitation bubbles, in the type of transient membrane perforation to increase the permeability for all substances that otherwise would have little or no permeability.
  • the already discussed advantageous embodiments of the method according to the invention for the hydrodynamic generation of homogeneous, oscillating cavitation bubbles naturally also find appropriate application to the method according to the invention for hydrodynamically generated short-term cell and membrane manipulation.
  • FIG. 1 shows a cavitation reactor 1 according to the embodiment.
  • the application refers to aqueous solutions that have been deliberately inoculated with bacteria.
  • the dimensioning of the reactor was carried out for a pilot laboratory scale.
  • the Treatable flow rates vary from 0.3 L s "1 - 0.5 L s ' 1 at pressure drops of 2.5 bar to 10 bar
  • the system is designed to be open and therefore still subject to atmospheric pressure
  • the temperature of the aqueous solution was in this case, 20 ° C.
  • the tube cross section before and after the cavitation reactor is 20 mm.
  • Both the reactor and the lead and tail are made of hydraulically smooth stainless steel (V4A, surface roughness ⁇ 2 ⁇ m)
  • V4A hydraulically smooth stainless steel
  • the acceleration section 5, the diaphragm 6, the stabilizing section 7 and the collapse section 8 directly adjoin one another and form a Flow channel 3.
  • the fluid flows from the acceleration section 5 to the collapse section 8. 6 cavitation bubbles 2 are generated at the aperture.
  • the cavitation bubbles 2 are extremely small and can therefore only be represented schematically in FIG.
  • the acceleration section 5 comprises a nozzle cone 9.
  • This nozzle cone 9 serves for further constriction of the flow cross-section along the flow direction 4 and is arranged rotationally symmetrical to a center axis 10 of the flow channel 3.
  • the nozzle cone 9 ends directly at the beginning of the diaphragm 6. This makes it possible that the diaphragm 6 with a screw 19 ( Figure 2) can be screwed onto the front end of the nozzle cone 9. With its outer circumference, the diaphragm 6 is supported on a lattice stop 18 (FIG. 2).
  • the collapsing section 8 initially comprises four smaller successive steps 20 and then four larger successive steps 21 for cross-sectional widening.
  • the end of the collapse portion 8 is formed as a flange 22.
  • FIG. 2 shows a section of the cavitation reactor 1 according to the embodiment and a section AA.
  • the aperture 6, formed as a micro-grid rests in the middle of the nozzle cone 9 and is screwed.
  • An outer peripheral edge of the panel 6 lies on the grid stop 18 on. This creates between the grid stop 18 and the nozzle cone 9 a flow cross-sectional area of the aperture 6 in ring form.
  • a first diameter 11 shows an initial diameter of the nozzle cone 9 at the beginning of the acceleration section 5.
  • a second diameter 12 also shows at the beginning of the acceleration section 5, the maximum inner diameter of the acceleration section 5.
  • This second Diameter 12 narrows along the flow direction 4 to the end of the acceleration section 5 to a third diameter 13.
  • the first diameter 11 narrows along the flow direction 4 to the end of the nozzle cone 9 and to the end of the acceleration section 5 to the fourth diameter 14th
  • the difference between the third diameter 13 and the fourth diameter 14 defines an annular surface.
  • the section in Figure 2 shows an overall diameter 15 of the diaphragm used 6.
  • FIGS. 1 and 2 in contrast to all other known apparatuses and geometries, effects the already described advantageous generation of the homogeneous, oscillating cavitation, e.g. for membrane poration or cell manipulation.
  • This stabilizing section 7 is initially designed as a pipe section with a further constant narrow cross-section, in order to keep the flow rate high enough.
  • the static pressure is still low enough to keep the oscillating cavitation bubbles 2 stable.
  • the cavitation bubbles 2 thus have a longer residence time in the apparatus and can also undergo several hundred oscillations.
  • the outlet or the collapse section 8 is formed in a slow cross-sectional widening in which the static pressure increases again and the cavitation bubbles 2 finally are forced to collapse. Depending on the flow rate, this range also falls on ever-increasing cross-sectional areas or the area of the bubble oscillation increases. In this Kollableitersabites 8 the typical pressure waves are released, as they are known from conventional cavitation. This additionally provides short-term high energies and shear stresses.
  • a flow to be provided in the flow direction 4 in front of the acceleration section 5.
  • the separation and the calming of the volume flow are on the annular gap by means of a tip and / or by means of flow straighteners. This is preferably done with a diameter of about 20 mm over a length of 75 mm.
  • the first diameter 11 is in the exemplary embodiment 10 mm
  • the second diameter 12 is 20 mm
  • the third diameter 13 is 6.4 mm
  • the fourth diameter 14 at 4 mm.
  • the acceleration section 5 extends over a length of 75 mm.
  • the mesh size of the micro-grating of the aperture 6 used in the embodiment is 0.4 mm with a wire thickness of 0.2 mm. This results in a free grid area of 44%.
  • the sixth diameter 16 is 5.6 mm and the stabilizing section 7 extends over 40 mm.
  • the four small steps 20 of the collapsing section 8 increase the cross section every 5 mm in steps of 0.2 mm.
  • the large steps 21 increase the cross section every 10 mm in increments of 1 mm.
  • cavitation reactor 1 may be provided to the flange 22 at the end of the Kollab istsabitess 8 preferably a spout with an initial diameter of 10 mm and an extension to 20 mm.
  • the cross-sectional increase in the collapse section 8 may preferably be configured in a helical manner, so that a very gentle increase in pressure is realized and thus an extended collapse zone is created in the axial direction.
  • the energy efficiency of the cavitation reactor according to the invention is compared with other types of cavitation generators of similar dimensions, with respect to the volume flow and the free cross-sectional area.
  • 3 shows a plot of the achievable cavitation number C v over the hydraulic power to be provided in kWh per m 3 of treated water.
  • the hydraulic power here corresponds to the product of volume flow and Pressure loss. The lower the C v values can be achieved with the lowest possible energy input, the better the conversion of the energy into the cavitation, ie, the farther left in FIG. 3 the corresponding curve runs, the more effective is associated cavitation generation.
  • the first curve 24 shows the measurement on the cavitation reactor 1 according to the invention according to the exemplary embodiment.
  • the second curve 25 shows cavitation with a 12-fold perforated plate designed for comparison purposes, with a diameter of 1.0 mm per hole and a free flow area of 9.5 mm 2 .
  • a third curve 26 shows measurement results of a pinhole with only one hole and diameter 3.3 mm and thus free flow area of 8.6 mm 2 .
  • a fourth curve 27 shows measurement results on a conventional venturi nozzle, with a diameter of 3.3 mm and a length of 100 mm. With the cavitation number of 0.2, an operating point 28 of the cavitation reactor 1 according to the exemplary embodiment is shown.
  • the cavitation reactor 1 according to the invention has a significantly higher efficiency in the cavitation yield at the operating point 28 (C v ⁇ 0.2) than a pinhole diaphragm with large and few holes or a simple Venturi nozzle. Only at very high volume flows and energy inputs are similar efficiencies achieved. However, the described advantages of homogeneous, oscillating bubble fields are only achieved by the variant according to the invention.
  • the diagram in FIG. 4 shows a measurement at the cavitation reactor 1 according to the exemplary embodiment and represents the cavitation number C v over the volume flow in Ls "1.
  • a fifth curve 29 shows pressure-corrected values of the cavitation number C v at the diaphragm 6.
  • a sixth curve 30 shows the course of the cavitation number above the volume flow in Kavitationsreaktor 1 at the end of the stabilizing section 7 at the diameter 6 of 5.6 mm.
  • the higher efficiency at the operating point 28 is due to the special property of homogeneous bubble generation in the lattice plane.
  • the operating point 28 is at a flow rate of about 0.32 L / s with full cavitation formation in the stabilization section 7.
  • a standard 5.6 mm venturi nozzle similar to the sixth diameter 16 would not yet cavitate.
  • the C v value would still be too high at about 1, 3 and the cavitation does not begin.
  • cavitation from the aperture 6 begins at approximately 0.2 L / s. If the volume flow is increased to a value of 0.315 L / s, the cavitation abruptly expands out of the lattice plane far into the stabilization section 7, although theoretically this would not be possible for a cavitation number of approximately 1.4 for this region. Only from the first extensions of the collapsing section 8 are the bubbles 2 forced to collapse. Until then, a homogeneous field of oscillating cavitation bubbles 2 extends, which is maintained even under non-cavitative conditions. If the volume flow is increased further, the cavitation zone extends further and further into the opening cone. The bubble collapse then happens e.g. only in the area of the 7.0 or 8.0 mm cross section.
  • the line perforating effect of oscillating cavitation bubbles 2 in combination with disinfectants can be practically applied. Most disinfectants can not pass the membrane of the cell or only with high diffusion pressure or high concentration. The effect is thus limited to the surface of the cell, although the best site of action in the bacterial cell, e.g. at the DNA or RNA or intracellular enzymes and enzyme complexes, and would lead there faster to lethal inactivation.
  • FIG. 5 shows a schematic representation of the cell perforation by means of hydrodynamic cavitation.
  • a cell membrane 32 is shown. Outside the corresponding cell is the outer space 31. Within the cell is the interior space 33.
  • an oscillating bladder 34 is shown with a minimum maximum diameter shown in dashed lines. By oscillating the bladder 34, the cell membrane 32 is at least temporarily opened, so that active ingredient can penetrate into the interior space 33 or can flow from the interior space 33 into the exterior space 31.
  • Figure 5 illustrates the mechanism underlying the increase in inactivation efficiency. By combining chlorine dioxide with oscillating cavitation, an increase in inactivation is thus observed, since the transient perforation of the cell membrane 32 allows the chlorine dioxide to diffuse better and faster to the site of action in the cell.
  • FIG. 6 shows a schematic process sequence for disinfecting a fluid by means of the cavitation reactor 1 according to the exemplary embodiment.
  • a first sampling 35 for determining the germ count and then a pressure-increasing device 36 are provided along the flow direction 4.
  • the cavitation reactor 1 connects.
  • a hold / contact time 37 is provided.
  • a second sampling 38 takes place for determining the germ count after cavitation.
  • chlorine dioxide is introduced as a disinfectant 39 from a reservoir into the main fluid flow by means of a metering pump 40.
  • the basic process flow is shown in FIG. 6.
  • the disinfectant 39 from a template by means of the metering pump 40 in the main stream, in an adjusted amount, dosed. In the metering pump 40, this already creates an ideal premix of the disinfectant 39.
  • the cavitation reactor 1 is run through and then still the corresponding holding / exposure time 37, which leads to the desired inactivation granted.
  • FIG. 7 shows a graph with the germ count in colony forming units ml '1 over time in minutes to illustrate the efficient disinfection method according to FIG.
  • the dashed line 41 in Figure 7 shows a specific inactivation rate according to standard inactivation for E. coli at 0.3 mg L "1 chlorine dioxide, whereas the four measurement points 42 show the measurement results when using the method according to FIG. It can be shown with the results according to FIG. 7 that after the passage through the cavitation reactor 1 a higher inactivation can be achieved than in the sole treatment with chlorine dioxide 39.
  • chlorine dioxide 39 With the combination of chlorine dioxide 39 and the cavitation reactor 1 according to the invention, more than 50% of chlorine dioxide 39 can be saved.
  • Optimizing the process conditions and process management can further reduce the amount of chlorine dioxide 39.
  • the chemical load of the process water is reduced by half, so that much fewer side reactions with harmful product formation occur.For many disinfectants unite Furthermore, the handling and stocking fills up.

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Abstract

L'invention concerne un réacteur de cavitation pour la production hydrodynamique de bulles de cavitation oscillantes homogènes dans un fluide, comportant les composants suivants formant un canal d'écoulement et disposés l'un derrière l'autre dans le sens d'écoulement: une section d'accélération conçue pour augmenter une vitesse d'écoulement; un obturateur disposé perpendiculaire à la direction d'écoulement présentant une pluralité de micro-passages destinés à produire les bulles de cavitation, au moins 10 micro-passages par cm2 étant créés sur l'ensemble d'une surface de section transversale, définie sur un côté de l'obturateur faisant face au flux; une section de stabilisation conçue pour stabiliser une oscillation des bulles de cavitation; et une section de rupture présentant au moins un élargissement de la surface de section transversale du canal d'écoulement dans le sens d'écoulement.
EP10725388A 2009-07-28 2010-06-09 Réacteur de cavitation Withdrawn EP2459307A2 (fr)

Applications Claiming Priority (2)

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DE102009034977A DE102009034977B4 (de) 2009-07-28 2009-07-28 Kavitationsreaktor sowie ein Verfahren zur hydrodynamischen Erzeugung homogener, oszillierender Kavitationsblasen in einem Fluid, ein Verfahren zur Desinfektion eines Fluids und ein Verfahren zum Emulgieren oder zum Suspendieren oder zur Reaktionsbegünstigung zumindest zweier Stoffe
PCT/EP2010/003469 WO2011012186A2 (fr) 2009-07-28 2010-06-09 Réacteur de cavitation

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DE102009034977A1 (de) 2011-02-03
WO2011012186A2 (fr) 2011-02-03

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