EP0475284A1 - Procédé et dispositif pour agir sur des fluides au moyen d'une onde de choc de compression - Google Patents

Procédé et dispositif pour agir sur des fluides au moyen d'une onde de choc de compression Download PDF

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Publication number
EP0475284A1
EP0475284A1 EP19910115027 EP91115027A EP0475284A1 EP 0475284 A1 EP0475284 A1 EP 0475284A1 EP 19910115027 EP19910115027 EP 19910115027 EP 91115027 A EP91115027 A EP 91115027A EP 0475284 A1 EP0475284 A1 EP 0475284A1
Authority
EP
European Patent Office
Prior art keywords
fluids
section
pressure
nozzle
cross
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
EP19910115027
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German (de)
English (en)
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EP0475284B1 (fr
Inventor
Vladimir Vladimirowitsch Fissenko
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.)
Transsonic Ueberschall-Anlagen GmbH
Original Assignee
Transsonic Ueberschall-Anlagen GmbH
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 Transsonic Ueberschall-Anlagen GmbH filed Critical Transsonic Ueberschall-Anlagen GmbH
Priority to YU26292A priority Critical patent/YU26292A/sh
Publication of EP0475284A1 publication Critical patent/EP0475284A1/fr
Application granted granted Critical
Publication of EP0475284B1 publication Critical patent/EP0475284B1/fr
Anticipated expiration legal-status Critical
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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
    • B01F23/40—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
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/311—Injector mixers in conduits or tubes through which the main component flows for mixing more than two components; Devices specially adapted for generating foam
    • 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
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3122—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof the material flowing at a supersonic velocity thereby creating shock waves
    • 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
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3124—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow
    • B01F25/31243—Eductor or eductor-type venturi, i.e. the main flow being injected through the venturi with high speed in the form of a jet
    • 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
    • Y10T137/0324—With control of flow by a condition or characteristic of a fluid
    • Y10T137/0329—Mixing of plural fluids of diverse characteristics or conditions

Definitions

  • the invention relates to a method and a device for the action of a compression shock on fluids.
  • Fluids are to be understood as liquids, gases or vapors with or without solid particles dispersed therein.
  • the supersonic speed is achieved with the help of a Laval nozzle, at the outlet cross section of which there is an injection zone for the liquid component to be emulsified, which is followed by a diffuser-shaped channel in the direction of flow.
  • a mixing chamber is arranged, which is connected to the channel via a housing into which a feed line for a passive component opens.
  • the mixing chamber has a part which narrows in the flow direction and faces the outlet opening of the chamber and the Laval nozzle, which is adjoined by a cylindrical part which merges into an expanding part.
  • the cross section of the outlet opening of the diffuser-shaped channel is one to two times the cross section of the cylindrical part of the mixing chamber.
  • the object on which the invention is based is now to design the method and the device of the type mentioned at the outset in such a way that continuous, stable operation is ensured.
  • This object is achieved procedurally in that a two-phase mixture of two fluids, which is supplied at subsonic speed, is accelerated to its speed of sound, the two-phase mixture is expanded to supersonic speed and the two-phase mixture thereby accelerated to supersonic speed essentially via a compression shock is brought to a final pressure as a single-phase mixture which corresponds to the respective ambient pressure.
  • At least one further fluid is advantageously introduced into a mixture of at least two fluids before the two-phase mixture thus formed is accelerated to its speed of sound.
  • the static pressure p ck behind the compression stroke is expediently set such that it is greater than the static pressure P1 before the compression stroke and is less than half the sum of the static pressure P1 before the compression stroke and from the total pressure po behind the compression stroke or equal to half of this sum.
  • the intensity of the compression shock and thereby its effect can be further increased if heat and / or mass is added to the fluid mixture flowing at subsonic speed, which is still single-phase or already two-phase, before its speed of sound is reached. It can also be extracted together with it or only for heat and / or mass from the fluid mixture flowing at supersonic speed.
  • the above-mentioned object is achieved by a nozzle coaxially connected to a feed line for a mixture of at least two fluids, by an expansion chamber arranged downstream of the narrowest cross-section of the nozzle in the flow direction, by an outlet channel connected to the expansion chamber and having a constant cross-section, the hydraulic diameter of which is as large as the hydraulic diameter of the narrowest cross section of the nozzle or up to three times the hydraulic diameter of the narrowest cross section of the nozzle, and through an outlet connected to the expansion chamber and provided with a pressure relief valve.
  • a feed line for at least one further fluid can advantageously be arranged directly in front of the narrowest cross section of the nozzle in the flow direction.
  • the outlet channel of the expansion chamber is expediently arranged coaxially with the nozzle.
  • the narrowest cross section of the nozzle on the outlet side is formed by a diaphragm.
  • the opening pressure of the pressure relief valve is expediently adjustable.
  • the desired fluid effect can be achieved continuously with an optimized energy expenditure in a stable manner and without operational disturbances, essentially independently of changes in the external or final pressure.
  • homogeneous, finely dispersed mixtures with predetermined concentrations of the individual components can be produced from several components.
  • This also includes the homogenization of milk and the production of whole milk substitutes, the preparation of medicines and cosmetics as well as the production and mixing of bioactive products, the production of stable water-fuel emulsions, the production of paints, paints and adhesives, the transport of Fluids through pipelines and containers without deposits being formed, the increase in surface activity with guaranteed effectiveness, the preparation of stable hydrogen emulsions, the construction of effective cleaning systems due to a highly developed activation area with combinable application possibilities of the system.
  • the device can also be used as a pump and / or heat exchanger, for example as a condenser pump and heating pump of the mixer type, alone or in series connection, for the production of fundamentally new, closed and ecologically harmless systems in energy, metallurgy, chemical and biological industry with full utilization thermal energy, as pumps for contaminated wastewater and liquids that also contain solid particles, in cooperation with washing and cleaning systems for halls, tankers and hulls, as well as with water collection systems, fire extinguishing systems and equipment from fire-risk production sites, as well as for extracting explosive and toxic gases can be used in waste water and reservoirs.
  • a condenser pump and heating pump of the mixer type alone or in series connection
  • the device can be used in series connection of several units as a feed water pump and / or preheater, steam extracted as an energy source from intermediate stages of the turbine being supplied as fluid in order to be able to carry out the individual process steps.
  • the above-mentioned uses according to the invention are based on the phenomenon of increased compression in the homogeneous two-phase flow, the speed of sound being lower not only in the liquid but also in the gases or vapors.
  • This phenomenon enables the supersonic effects to be achieved when the Mach number is greater than 1, with extremely low energy input, the Mach number representing the compressibility of a flowing medium and corresponding to the ratio of the flow velocity of the fluid or a fluid mixture in relation to its local sound velocity. It is customary to achieve the Mach number greater than 1 in drive nozzles or turbines by increasing the flow velocity of the fluid, that is to say by increasing the counter of the ratio forming the Mach number.
  • the device shown in Fig. 1 for the action of a shock on fluids, which is used for the production of homogeneous mixtures of fluids, has a cylindrical housing 1 with an inlet section 20 in the form of a substantially cylindrical bore on one end face, which in one conically tapering nozzle 2 passes, which ends in a narrowest cross section 6.
  • the narrowest cross section 6 of the nozzle 2 is followed by a diffuser section of an expansion chamber 10, the cylindrical inlet section 20, the nozzle 2, its outlet cross section 6, the expansion chamber 10 and its diffuser section all being rotationally symmetrical with respect to the cylindrical housing 1 and coaxial with its axis 18 are arranged.
  • the cylindrical outlet channel 8 arranged in the expansion chamber 10 opposite the narrowest cross section 6 of the nozzle, the constant cross section of which has a diameter which may not be smaller than the narrowest cross section 6 of the nozzle 2 but which may not exceed a diameter, which is three times the diameter of the narrowest cross section 6.
  • a cylindrical outlet connector 17 is screwed with a slide 14, the outlet connector 17 has a constant cross section with a diameter that Outlet diameter of the diffuser channel 9 corresponds.
  • a feed line 4 is fastened in the form of a pipe section with a constant cross-section, onto which an inlet connection 15 with a slide 13 is screwed by means of a further threaded connection 19.
  • the cross section of the inlet connection 15 corresponds to that of the feed line 4, the arrangement of the feed line 4 and the inlet connection 15 likewise taking place coaxially with the axis 18.
  • a fluid supply line 3 with a slide 12 opens radially in the area of the beginning cross-sectional constriction of the nozzle 2.
  • An outlet connection 11 with a pressure relief valve 22, which is biased towards the expansion chamber 10, opens radially into the expansion chamber 10 .
  • the feed line 4 is axially adjustable with respect to the nozzle 2 via the screw connection at the inlet section 20 to the housing 1.
  • a supply line 4 with a cross section that initially narrows and then widens again is provided.
  • the nozzle 2 has in front of its narrowest cross-section on the outlet side, which in this embodiment is designed as an orifice 6, an interruption in the circumferential direction which is connected to an annular chamber 5, into which a further inlet connection 16 for a fluid opens, in which a Slider 7 is arranged.
  • the start-up process begins with the slide 7 and 12 being opened, whereby a first fluid through the nozzle 2 and after mixing with a through the inlet port 16 supplied second fluid through the narrowest cross-section designed as an aperture 6, the expansion chamber 10, the cylindrical outlet channel 8, the diffuser channel 9, the outlet port 17 and the open slide 14.
  • a third fluid or fluid mixture is now fed via the inlet connector 15 and the feed line 4 in the axial flow into the nozzle 2 and mixed with the first and second fluid, which through the fluid feed line 3 and the inlet connector 16 in a ring flow around the fluid or fluid mixture supplied through the feed line 4 are supplied.
  • Due to the further supply of fluid via the feed line 4 the pressure in the expansion chamber 10 increases to such an extent that the pressure relief valve 22 in the outlet port 11 opens and the mixture flows out through the outlet port 11 and through the outlet channel 8 in proportion to their flow cross sections.
  • the device is shown schematically, where I is the inflow cross section of the feed line 4 for the third fluid, 11 the narrowed cross section of the feed line 4 for the third fluid and IV the expanded outlet cross section of the feed line 4 for the third fluid.
  • the outlet cross section IV is enclosed by an inlet ring cross section 111 of the fluid supply line 3 for the first fluid, which forms the beginning of the nozzle 2, which ends in cross section V, which is from an inlet ring cross section of the Inlet 16 is surrounded for the second fluid.
  • In the axial flow direction of the fluids or of the fluid mixture follows the narrowest cross section VI formed by the orifice 6, to which the expansion chamber 10 connects, to which the pressure relief valve 22 is assigned.
  • the expansion chamber 10 is followed by the outlet channel 8 with its inlet cross-section VII, which remains constant over a short, fixed length up to the cross-section VIII and from there widens in the form of the diffuser channel 9 to the cross-section IX of the outlet port 17.
  • FIG. 3 shows the stage of the start-up process in which, after opening the slides 12 and 7, the slides 13 and 14 are also open and, due to the pressure in the expansion chamber 10, the pressure relief valve 22 has also opened.
  • the flow velocity w initially remains essentially constant despite the reduction in cross-section between the inflow cross-section I and the narrowed cross-section 11, and then drops to the outlet cross-section IV due to the cross-sectional widening and the fluid admixtures. Due to the reduction in cross-section of the nozzle 2, the flow velocity w increases up to the narrowest cross-section VI and still slightly in the expansion chamber 10.
  • the fluid mixture then flows out with appropriate flow rates through the outlet port 11 and the outlet channel 8, the flow velocity w of the fluid mixture in the diffuser channel 9 falling slightly towards the cross section of the outlet port 17.
  • the static pressure p remains essentially constant in the feed line 4 for the third fluid mixture up to the enlarged outlet cross section IV because of the axially downstream fluid admixtures despite the change in cross section.
  • the static pressure p falls to the cross-section V of the end of the nozzle 2 and to the narrowest cross-section VI in the form of the orifice 6. This is followed by a slight pressure drop in the expansion chamber 10 and in the outlet channel 8 up to the cross-section VIII, which is followed by a slight increase in pressure in the diffuser channel 9 up to the cross section IX of the outlet connector 17.
  • the pressure in the expansion chamber 10 begins to drop.
  • the flow velocity in the narrowest cross-section VI in the form of the orifice 6 increases, while the pressure in the narrowest cross-section VI decreases, so that the saturation pressure of vaporous or gaseous fluid components falls below, which leads to the formation of a two-phase mixture - unless a two-phase has Mixture was formed by supplying a liquid fluid - whose associated speed of sound is considerably lower than the speed of sound of the single-phase fluid mixture.
  • the axial course of the flow velocity w of FIG. 4 shows the sharp drop in velocity when the first fluid is admixed to form a two-phase mixture, the initial velocity of the fluids being in the subsonic range and the speed of sound in the narrowest cross-section VI given by the orifice 6 is reached on the two-phase mixture.
  • the flow velocity w between the cross sections VI and VII in the expansion chamber 10 with the pressure relief valve 22 closed is thus in the supersonic range, but reference is made to the speed of sound of the two-phase fluid mixture, which is substantially lower than the speed of sound of the corresponding single-phase mixture.
  • the fluid mixing of the fluids supplied with subsonic through the feed line 4, the fluid feed line 3 and the inlet connection 16 takes place first of all on the basis of the ring flows and the relative speeds.
  • a further mixing takes place through condensation during the transition to the two-phase state, through boiling and Evaporation in the area of the supersonic flows in the expansion chamber 10 and then in the compression shock, where a "smashing effect" finally brings about the final homogeneous mixture structure.
  • the strength of the shock and the functionality of the device in continuous mixing operation depends on the volume phase ratio before the shock.
  • the required volume phase ratio before the compression shock is set by appropriate selection of the ratio of the hydraulic diameter of the narrowest cross section of the nozzle 2 or the orifice 6 and the hydraulic diameter of the outlet channel 8.
  • the two-phase flow has a bubble-like, foam-like structure before the compression stroke. Because fat consists of surface-active particles, a compact film forms around each vapor bubble or gas bubble. In the compression stroke, the bubbles are now reduced until they disappear, the force of the specific pressure acting on the bubbles increasing many times over due to the reduced surface area of the bubbles. The bubbles disappear or implode in a very small space and in a very short time, which increases the effect per single bubble again. The end result is that the fat particles behind the shock are reduced to the size of microns and tenths of a micron, which cannot be achieved in a conventional manner.
  • the device described can easily be used as a mixer, homogenizer, saturator and degassing device.
  • one of the supplied fluids must have a temperature which is higher than that of the other fluids, or, when the fluids are mixed, heat must be introduced into the fluids to be mixed due to exothermic reactions in order for a conversion of Thermal energy in mechanical work is possible. In this case it turns out a higher total pressure of the mixing components at the outlet of the device than at the inlet.
  • the device as a pump combined with the effect as a heat exchanger is described below in connection with a system for regenerative feed water preheating in thermal power plants with steam turbines.
  • the feed water which is usually fed from the condenser into the boiler with the aid of special pumps and is heated by steam in surface-type heat exchangers, is preheated in stages, this steam being taken from individual stages of the steam turbine.
  • the surface heat exchangers and pumps with an electric drive can now be completely or partially dispensed with, which is explained with the use of a device according to the invention in a stage of a regenerative preheater.
  • the flow between the cross section VI and VII of Fig. 4 a vesicular foam-like structure of the mixture flow is achieved, which has an extremely developed surface in the heat exchange between the phases, which leads to an extreme increase in the heat flow from the heating leads to the medium to be heated, this heat flow being proportional to the temperature difference and to the specific surfaces. Increasing the latter results in large heat flows with small temperature differences between the heating and heating medium.
  • the device thus works as a heat exchanger, the external dimensions of which can be considerably smaller compared to known heat exchangers of the same output and whose efficiency is very high.
  • the developed surface of the phase segments due to the surface activity increases the flow effectiveness of all exchange processes, regardless of whether the heat exchange is a mass transfer or is based on a chemical or other process in which the flow effectiveness depends on the size of the surface activity.
  • the solubility of gases in liquids for selected components depends on the temperature and pressure in the liquid.
  • a drop in pressure in the liquid always allows a decrease in its gas content, the dependence of the temperature depends on several components, but is known.
  • the content of undesired gas in a liquid can be reduced to the required amount.
  • steam is supplied via the feed line 4 of FIG. 2 to that liquid which is to be degassed, or the liquid itself is supplied in a certain amount at a certain temperature.
  • the same liquid is introduced via the slide 12 and the fluid feed line 3 from FIG. 2 in the cross section IV of FIG. 4. It is necessary for the temperature of the mixture to be about 70 to 80 ° C, which corresponds to a minimum of solubility at this pressure.
  • the mixture with the temperature mentioned is accelerated in the nozzle 2 of FIG. 2 forming a conical chamber.
  • the pressure of the flow drops and falls below the gas saturation pressure in cross-section V of FIG. 4 at the prevailing temperature, a fluid which is removed from the liquid at the outlet of the device being fed to the mixture flow before this cross-section.
  • the two-phase mixture flow enters via the orifice 6 of FIG. 2 into the zone of the minimum pressure between the cross section VI and VII of FIG. 4.
  • Via the pressure relief valve 22 of FIG. 2 steam-gas mixture is now removed and passed into a special vacuum vessel.
  • the intensity and effectiveness of the degassing is thereby regulated via the pressure relief valve 22, namely by adjusting the pressure in the expansion chamber 10 between the cross section VI and VII.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Jet Pumps And Other Pumps (AREA)
  • Surgical Instruments (AREA)
  • Perforating, Stamping-Out Or Severing By Means Other Than Cutting (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Nozzles (AREA)
  • Processing Of Solid Wastes (AREA)
EP19910115027 1990-09-06 1991-09-05 Procédé et dispositif pour agir sur des fluides au moyen d'une onde de choc de compression Expired - Lifetime EP0475284B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
YU26292A YU26292A (sh) 1990-09-06 1992-03-16 Postupak i uredjaj za dejstvo na fluide putem udarnih talasa

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
BG92795/90 1990-09-06
BG9279590 1990-09-06

Publications (2)

Publication Number Publication Date
EP0475284A1 true EP0475284A1 (fr) 1992-03-18
EP0475284B1 EP0475284B1 (fr) 1994-07-06

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EP19910115027 Expired - Lifetime EP0475284B1 (fr) 1990-09-06 1991-09-05 Procédé et dispositif pour agir sur des fluides au moyen d'une onde de choc de compression

Country Status (11)

Country Link
US (2) US5205648A (fr)
EP (1) EP0475284B1 (fr)
JP (1) JPH078330B2 (fr)
KR (1) KR950000002B1 (fr)
AT (1) ATE108089T1 (fr)
CA (1) CA2050624C (fr)
DE (1) DE59102114D1 (fr)
DK (1) DK0475284T3 (fr)
ES (1) ES2056542T3 (fr)
RU (1) RU2016261C1 (fr)
YU (1) YU26292A (fr)

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EP0677313A3 (fr) * 1994-04-15 1996-10-02 Crown Chemtech Ltd Stripage de substances volatiles de fluides moins volatiles.
WO1999015263A1 (fr) * 1997-09-25 1999-04-01 Ge Bayer Silicones Gmbh & Co. Kg Procede et disposiitf pour preparer des emulsions a base de silicone
WO2000002653A1 (fr) * 1998-07-08 2000-01-20 Novafluid - Innovative Strömungs- & Wärmeübertragungs-Technologie Gmbh Procede et dispositif pour accroitre la pression ou l'enthalpie d'un fluide s'ecoulant a une vitesse supersonique
EP2145912A1 (fr) 2008-07-19 2010-01-20 Momentive Performance Materials GmbH Procédé de revêtement de substrats
WO2011040837A1 (fr) * 2009-09-30 2011-04-07 Fisionic Holding Limited Dispositif pour la préparation d'une émulsion eau-carburant
WO2013037592A1 (fr) * 2011-09-16 2013-03-21 Siemens Aktiengesellschaft Dispositif de mélange pour mélanger de la poudre agglomérante dans une suspension

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US5957760A (en) 1996-03-14 1999-09-28 Kreativ, Inc Supersonic converging-diverging nozzle for use on biological organisms
EP0800775B1 (fr) * 1996-04-12 2000-03-15 Societe Des Produits Nestle S.A. Dispositif et procédé de traitement d'un produit fluide par injection de vapeur et du produit fluide
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RU2155280C1 (ru) * 1999-04-08 2000-08-27 Фисенко Владимир Владимирович Газожидкостной струйный аппарат
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WO2011040837A1 (fr) * 2009-09-30 2011-04-07 Fisionic Holding Limited Dispositif pour la préparation d'une émulsion eau-carburant
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YU26292A (sh) 1995-10-24
US5205648A (en) 1993-04-27
JPH04256428A (ja) 1992-09-11
CA2050624C (fr) 1996-06-04
US5275486A (en) 1994-01-04
DK0475284T3 (da) 1994-08-01
EP0475284B1 (fr) 1994-07-06
KR950000002B1 (en) 1995-01-07
CA2050624A1 (fr) 1992-03-07
JPH078330B2 (ja) 1995-02-01
ES2056542T3 (es) 1994-10-01
DE59102114D1 (de) 1994-08-11
ATE108089T1 (de) 1994-07-15
RU2016261C1 (ru) 1994-07-15

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