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EP0475284B1 - Verfahren und Vorrichtung zur Einwirkung eines Verdichtungsstosses auf Fluide - Google Patents

Verfahren und Vorrichtung zur Einwirkung eines Verdichtungsstosses auf Fluide Download PDF

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Publication number
EP0475284B1
EP0475284B1 EP19910115027 EP91115027A EP0475284B1 EP 0475284 B1 EP0475284 B1 EP 0475284B1 EP 19910115027 EP19910115027 EP 19910115027 EP 91115027 A EP91115027 A EP 91115027A EP 0475284 B1 EP0475284 B1 EP 0475284B1
Authority
EP
European Patent Office
Prior art keywords
fluids
nozzle
pressure
cross
shock wave
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP19910115027
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0475284A1 (de
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/de
Application granted granted Critical
Publication of EP0475284B1 publication Critical patent/EP0475284B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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 understood to mean 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 a diffuser in the direction of flow Channel is subordinate.
  • 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 accelerated to supersonic speed is brought to a final pressure which corresponds to the respective ambient pressure, essentially as a single-phase mixture, by means of a compression shock.
  • 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 is set behind the compression stroke so that it is greater than the static pressure p 1 before the compression stroke and is less than half the sum of the static pressure p 1 before the compression stroke and from the total pressure p 0 behind the compression stroke or equal to half of this sum.
  • the intensity of the compression shock and thereby its effect can be 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 it reaches its speed of sound. It can also be extracted together with this or only for the heat and / or mass of 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 downstream of the narrowest cross-section of the nozzle in the direction of flow, 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 upstream 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 effect of fluid can be achieved continuously, with 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 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 the energetics, metallurgy, chemical and biological industry with full utilization of the thermal energy, as pumps for polluted waste water and liquids, which also contain solid particles, can be used in conjunction 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 facilities, as well as for extracting explosive and toxic gases in waste water and reservoirs.
  • 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 the energetics, metallurgy, chemical and biological industry with full utilization of the thermal energy, as pumps for polluted waste water and liquids, which also contain solid particles, can be used in conjunction with washing and cleaning systems
  • 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 common for the Mach number to be greater than 1 in drive nozzles or turbines by increasing the flow speed of the fluid, that is, by increasing the numerator 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 may not exceed a diameter, which is three times the diameter of the narrowest cross section 6.
  • a cylindrical outlet port 17 is screwed with a slide 14, the outlet port 17 has a constant cross section with a diameter that Outlet diameter of the diffuser channel 9 corresponds.
  • a supply line 4 in the form of a pipe section with a constant cross-section is fastened, onto which an inlet connection 15 with a slide 13 is screwed via 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 opens radially with a pressure relief valve 22 which is biased towards 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 in communication with an annular chamber 5 into which a further inlet connection 16 for a fluid opens radially, in which a Slider 7 is arranged.
  • the flow velocity w and the static pressure p of the fluid or the fluids or the fluid mixture in the axial direction of the device of FIG. 2 show the startup of the device or its stable operation for continuous operation Mixture formation explained in detail.
  • 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 supplied 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.
  • the device is shown schematically, I being the inflow cross section of the feed line 4 for the third fluid, II 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 III 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 surrounded by an inlet ring cross section of the inlet connection 16 for the second fluid.
  • the axial flow direction of the fluids or of the fluid mixture is followed by 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 II, and then drops to the outlet cross-section IV due to the cross-sectional expansion and the fluid admixtures. Due to the reduction in the 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 nozzle 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 nozzle 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 in the nozzle 2 up 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, whereupon a slight increase in pressure in the diffuser channel 9 up to the cross section IX the outlet connector 17 follows.
  • 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 - if not a two-phase Mixture was formed by supplying a liquid fluid - whose associated speed of sound is significantly 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 initially on the basis of the ring currents 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 the supersonic flows in the expansion chamber 10 and then in the compression stroke, 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.
  • fat consists of surface-active particles, a compact film forms around every vapor bubble or gas bubble.
  • the vesicles are now reduced in size in the compression shock until they disappear, the force of the specific pressure acting on the vesicles increasing many times over due to the reduced surface area of the vesicles.
  • the bubbles disappear or implode in a very small space and in a very short time, which increases the effect per single bubble.
  • 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 heat must be introduced into the fluids to be mixed due to exothermic reactions in order to convert them Thermal energy in mechanical work is possible.
  • a higher total pressure of the mixing components occurs 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.
  • 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 that the temperature of the mixture be around 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.
  • Steam-gas mixture is now removed via the pressure relief valve 22 of FIG. 2 and into a special vacuum vessel headed.
  • 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)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Processing Of Solid Wastes (AREA)
  • Nozzles (AREA)
  • Perforating, Stamping-Out Or Severing By Means Other Than Cutting (AREA)
EP19910115027 1990-09-06 1991-09-05 Verfahren und Vorrichtung zur Einwirkung eines Verdichtungsstosses auf Fluide Expired - Lifetime EP0475284B1 (de)

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
BG9279590 1990-09-06
BG92795/90 1990-09-06

Publications (2)

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

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EP19910115027 Expired - Lifetime EP0475284B1 (de) 1990-09-06 1991-09-05 Verfahren und Vorrichtung zur Einwirkung eines Verdichtungsstosses auf Fluide

Country Status (11)

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

Cited By (6)

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EP0555498A1 (en) * 1992-02-11 1993-08-18 April Dynamics Industries 1990 Ltd. A two-phase supersonic flow system
WO1993016791A2 (en) * 1992-02-11 1993-09-02 April Dynamics Industries Ltd. A two-phase supersonic flow system
EP0677313A2 (en) * 1994-04-15 1995-10-18 Crown Chemtech Limited Stripping of volatile substances from less volatile fluids
US5824266A (en) * 1996-04-12 1998-10-20 Nestec S.A. Apparatus for treating a fluid product by injection of steam and the fluid product
US6523991B1 (en) 1998-07-08 2003-02-25 Jaber Maklad Method and device for increasing the pressure or enthalpy of a fluid flowing at supersonic speed
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US6095675A (en) * 1999-11-02 2000-08-01 Paul Ling Tai Multi-port venturi mixer
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CA2050624C (en) 1996-06-04
RU2016261C1 (ru) 1994-07-15
DK0475284T3 (da) 1994-08-01
YU26292A (sh) 1995-10-24
US5275486A (en) 1994-01-04
ATE108089T1 (de) 1994-07-15
EP0475284A1 (de) 1992-03-18
DE59102114D1 (de) 1994-08-11
US5205648A (en) 1993-04-27
JPH04256428A (ja) 1992-09-11
ES2056542T3 (es) 1994-10-01
CA2050624A1 (en) 1992-03-07
JPH078330B2 (ja) 1995-02-01

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