Search Images Maps Play YouTube News Gmail Drive More »
Sign in
Screen reader users: click this link for accessible mode. Accessible mode has the same essential features but works better with your reader.


  1. Advanced Patent Search
Publication numberUS3664638 A
Publication typeGrant
Publication dateMay 23, 1972
Filing dateFeb 24, 1970
Priority dateFeb 24, 1970
Publication numberUS 3664638 A, US 3664638A, US-A-3664638, US3664638 A, US3664638A
InventorsDevellian Richard D, Grout Kenneth M
Original AssigneeKenics Corp
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Mixing device
US 3664638 A
Abstract  available in
Previous page
Next page
Claims  available in
Description  (OCR text may contain errors)

May 23, 1972 K. M. GROUT ET AL MIXING DEVICE Filed Feb. 24, 1970 SPACING --S (Conduit Diameters) SPACING vs Re lo l0 l0 INVENTOR KENNETH M. GROUT RICHARD D.DEVELHAN FIG.6

United States Patent 3,664,638 MIXING DEVICE Kenneth M. Grout, Wakefield, and Richard D. Devellian, Rockport, Mass., assignors to Kenics Corporation, Danvers, Mass.

Filed Feb. 24, 1970, Ser. No. 14,266 Int. Cl. B01f 5/00 US. Cl. 259-4 3 Claims ABSTRACT OF THE DISCLOSURE A device for thoroughly mixing components of a fluidic material flowing through a conduit which contains a plu rality of curved sheet-like elements extending longitudinally through the conduit in which consecutive elements are curved in opposite directions and the adjacent edges of consecutive elements are spaced from each other by a distance dependent on the Reynolds number of the fluid and angularly displaced with respect to each other by an angle which diifers from 90 by an amount dependent on said distance.

BACKGROUND OF THE INVENTION (1) Field of the invention Mixing devices for mixing of a plurality of components of a fluid.

(2) Description of the prior art The prior art to which this invention relates is most closely represented by the US. patent to Armeniades et al. No. 3,286,992. While devices of the type described in that patent produce adequate mixing, the pressure drop required to produce the requisite flow velocity is often undesirably high. This is particularly true where it is necessary to transport fluidic materials long distances through the mixer conduit. The longer the distance, the more extreme are the problems of maintaining a homogenous mixture. Given time and distance, fluidic materials tend to classify themselves, when flowing in the conduit, by physical differences such as density, or thermally by producing a temperature gradient across the diameter of the conduit. In devices, such as shown in the Armeniades et al. patent, where the conduit is filled continuously with mixer blades, the pressure drop through the mixer may become prohibitively large when the nature of the fluidic materials and the results desired require relatively long mixer structures. One class of devices which requires long mixer conduits is that involving mixtures which need residence time to accomplish a necessary reaction to take place. Such reaction may be chemical or biological.

In view of the foregoing, it would be highly desirable to produce a device of the Armeniades et al. type in which the same or improved mixing action could be achieved with lower pressure drops. Furthermore, if the number of mixing blades could be reduced without reducing the degree of mixing, the expense of producing the devices would be reduced substantially.

SUMMARY OF THE INVENTION In the present invention the above limitations of the prior art have been eliminated by constructing a conduit in which the adjacent edges of consecutive curved sheetlike elements are spaced from each other by a distance, the optimum maximum length of which is a function of the Reynolds number of the fluid flowing through the conduit. At a Reynolds number of about such optimum maximum spacing preferably is about three diameters of the conduit. At a Reynolds number of about 200 to 300, the spacing may reach about six diameters. The leading edge of the downstream element should preferably inter- 3,664,638 Patented May 23, 1972 cept the body of fluid which has left the trailing edge of the upstream element along a line substantially at a right angle to the line along which said trailing edge had divided said body.

Said body of fluid continues to rotate after it leaves said trailing edge in the same direction which was imparted to it by the upstream element and further continues to rotate for many conduit diameter lengths down through the conduit. The pitch of the rotation of said fluid does not remain constant, but in fact, increases as its distance from said trailing edge increases. The rate of increase of the fluid pitch length is proportional to the Reynolds number of the fluid. It can then be determined that at a particular length of spacing, what should be the proper angle of the downstream mixer element in reference to the upstream mixer element. Said angle will differ from by an amount equal to the angle through which said body has rotated in the intervening space. If no increase in viscosity of the fluid occurs as it flows along the conduit, the spacing between successive elements can remain constant. If, however, the viscosity of the fluid increases, as in the case of certain reactions between components of the fluid, then the spacing between successive elements preferably decreases as such viscosity increases and the angle between successive trailing and leading edge pairs adjusted to produce the right angle interception of the rotating body, as described above.


FIG. 1 is a perspective view, partly in section, of a simple form of device according to this invention;

FIG. 2 is an enlarged partial view of the arrangement shown in FIG. 1;

FIG. 3 is a cross-sectional view along line 3-3 of FIG. 2.;

FIG. 4 is an exploded view of components from which the device of FIG. 1 may be constructed;

FIG. 5 is a cross-sectional view of an arrangement for illustrating the persistance of rotation of a fluid body in a mixer conduit; and

FIG. 6 is a graph showing the relationships, between the Reynolds number of the fluid flowing through the conduit and the spacing between the trailing and leading edges of successive curved elements to obtain minimum pressure drop without substantial loss of homogeneity.

DETAILED DESCRIPTION 'OF THE INVENTION In FIG. 1 and FIG. 2;, 10 is a hollow tube, preferably cylindrical in cross-section, and providing a conduit through which fluid components A and B are caused to flow in order to be thoroughly mixed. The fluid components are introduced at an upstream end 112. and discharged at a downstream end 14 at which the elements -A and B are thoroughly mixed into a homogeneous stream 16. Within the tube 10 are disposed a plurality of serially arranged curved elements 20, %130. Each of these elements are constructed of a thin flat sheet whose Width preferably, but not necessarily, equals the inner diameter of tube 10 and whose length is preferably 1.25 to several times its Width. Each sheet is twisted so that its upstream and downstream edges are substantially flat and are at a substantial angle to each other. This angle, as detailed in the Armeniades et al. patent, may vary between about 60 to about 210 These elements are positioned so that for each pair of successive elements (such as shown in FIG. 2), the downstream edge 32 of the first element and the upstream edge 34 of the next element are spaced from each other by a distance D which is predetermined as will be detailed below and are disposed with respect to each other by an angle a, (see FIG. 3) which likewise is predetermined as will be detailed below. If the upper and lower ends of the element 32 in FIG. 3 are designated as 1 and 2 and the corresponding ends of the element 34 in FIG. 3 are designated as 3 and 4, it will be seen that the angle will be the radial angle subtended by points ,1 and 4. A plenum chamber 36 is thus formed between said edges 32 and 34. Each element is twisted in the opposite sense to each adjacent element so that the direction of rotation of the body of fluid which passes along the elements is reversed for each successive element.

Typical arrangements for introducing and discharging the fluid elements and examples of the types of fluid components which may be mixed in a device of this general type are detailed in the Armeniades et al. patent and will not be repeated herein. It should be understood, however, that the fluid components may be any of a vast variety. For example they may be a gas and a liquid, parts of the same liquid at different temperatures, a liquid and finely divided solid particles or, of course, two or more different liquids.

In fact this invention has applicability to all flowable materials and therefore the term fluidic material will be used to designate the general class of liquids, gases and other flowable materials which it may be desired to mix. It is further to be understood that the terms fluid and fluidic material will be used interchangeably herein. It is to be understood, of course, that more than two fluidic material components may be mixed in devices according to this invention, the components A and B being merely illustrative.

When the incoming fluid stream encounters the upstream edge of the first element 20, it is split into two partial streams. The twisting configuration of the element imparts a double rotational motion to these partial streams and the mixing action starts to occur due to the eddy current motion within each partial stream. In devices constructed according to this invention it has been discovered that, as the partial streams leave the downstream edge 32 of the first element 20 and are permitted to merge into a common stream in the plenum chamber 36, the mixing activity increases substantially and persists as long as the common stream retains a substantial part of the rotation imparted to its two components by the element 20.

The nature of the continued rotation of the stream may be better understood from the illustration shown in FIG. 5. In this illustration, is shown a conduit 10 having a single mixer element 44 mounted therein. The left hand end of conduit 10 is the upstream end and the right hand end of conduit 10 is the downstream end. The mixer blade 44 is shown, by way of example, having a length of about 1.5 d, where d is the inner diameter of conduit 10, and turning the fluid body through about 180. The dotted curves extending from the downstream edge of element 44 represents the manner in which the rotation of the fluid body persists in its downstream flow. At the loops 46, 48, 50, 52 the fluid body will have rotated 90 from the position at which it left the trailing edge of element 44 and at the nodes 47, 49, 51 and '53 the fluid will have rotated 180 from such trailing edge position. The fluid body can be considered as having a pitch whose length is the distance between successive nodes. That pitch may be conveniently defined in terms of the inner diameter d of conduit 10.

In a conduit of uniform diameter, such as shown in FIG. 5, the velocity of the fluid flowing through the conduit will be substantially constant throughout its length. However, as the stream passes along the conduit, frictional forces, of a nature analyzed below, will progressively reduce the rotational velocity of the stream. As a result, as indicated in FIG. 5, the pitch of the stream increases progressively toward infinity as it flows along an extended conduit.

There are a number of factors which determine the rate at which such rotational velocity decreases as the fluid proceeds through such a plenum chamber. These are the frictional effects at the inner walls of tube 10', the viscosity of the fluid, its density and its flow rate. It will be recognized that these factors are all involved in the determination of the Reynolds number for any predetermined fluid which is passed through the device at a predetermined flow velocity. Thus the Reynolds number may be expressed as:

Re=pVd/,u. (Equation 1) where Re is the Reynolds number I 1 d is the inner diameter of the tube 10 at the plenum 36 V is the flow velocity p is the density of the fluid u is the viscosity of the fluid The rate at which the fluid pitch in FIG. 5 increases will be inversely proportional to the Reynolds number and likewise the actual length of each complete rotation or pitch will be inversely proportional to the Reynolds number. Therefore at low Reynolds number, where the viscosity is high and thus introduces large frictional losses, the rotation of the fluid is reduced at a greater rate making each such pitch length longer than at the higher Reynolds number Where the frictional effects are less and the rotational persistence of the fluid body is greater. Thus each arrangement of the kind shown in FIG. 5 will have a specific characteristic fluid pitch profile for each Reynolds number of fluid passage through the device. A practical and simple procedure for determining such pitch profile for each size of conduit and mixer blade configuration is to construct a full-size model, as shown in FIG. 5, with the conduit 10- made of a transparent material. Then a fluid is passed through the device at a predetermined Reynolds number, whereupon the pitch pattern can be seen and accurately measured. In some cases, it may be desirable to add a trace of additional particles such as air bubbles or colored droplets to enhance the visibility of the pitch pattern. In any event, each mixer structure will possess a characteristic fluid pitch profile for each Reynolds number.

In accordance with this invention it has also been found that for each Reynolds number a certain spacing S between successive mixer blades exists at which the pressure drop is a minimum without substantial loss of homogeneity in the fluid body. In FIG. 6 such spacing S is plotted, in terms of the diameter dof the conduit, against the Reynolds number; Preferably this invention will be used at Reynolds numbers at above about 100. At Re=l00, S is between about 5 and 6 diameters a, For spacings greater than S it has been found that various components of the fluid stream segregate themselves so that the degree of homogeneity of the stream deteriorates substantially. For the purposes of this invention the distance S istermed the homogeneity loss distance for each Reynolds number and such distance can be determined from the curve in FIG. 6. As previouslyindicated the fluid components may be portions of the fluid at diiferent temperatures, components with different densities, and the like. To the degree that some loss of homogeneity can be tolerated, the actual spacing between mixer blades can, be greater than S in order to achieve an even greater degree of pressure drop.

As the mixer blades are spaced closer than the distance S, some of the benefits of this invention may still be achieved although with some increase in pressure drop over the minimum possible pressure drop. However, the actual spacing between mixer blades must be substantial in order to achieve substantially reduced pressure drops over the prior art. In general the spacing between blades should be a substantial distance which is of the order of the homogeneity loss distance or less.

In order to achieve the best mixing action (referring to FIGS. 1, 2 and 3), the leading edge 34 should intercept the rotating body of fluid in the plenum 36 at right angles to the line along which the preceding trailing edge 32 had divided said body. In such case, the angle will differ from 90 by the angle through which the fluid will have rotated in the plenum 36 between the time it left the trailing edge 32 and reaches the leading edge 34. To determine such angle a for any device according to this invention, such device will have assigned to it a characteristic Reynolds number at which it will be designed to operate. The characteristic fluid pitch profile will then be determined as described above. Under the principles explained in connection with FIG. 6, a specific spacing between successive mixer blades will be chosen. This spacing will fix the point on the characteristic fluid pitch profile at which the leading edge of the downstream mixer blade will be located. If it is located at a loop of such profile, it will be seen that the fluid body will have rotated through 90 after leaving the upstream trailing edge and therefore the angle a will be 180. If such leading edge is located at a node the angle a will be 90. Therefore, as the position of the leading edge is moved from a node along one pitch length to a loop and then on to the next node, the angle a will increase from 90 to 180 and then back to 90.

If the viscosity of the fluid to be mixed remains constant as it flows through the length of tube 10, then the spacing between mixer elements and the angle or will be the same for each successive pair of elements. However, in some cases there may be a change in the viscosity of the fluid during its passage through the present mixer due to a reaction occurring in the fluid in such passage. Since the user will know the elements of the fluid which he desires to mix and also the velocity at which he will pass the fluid through the device, he will be able to predetermine the viscosity of the fluid at each point along the tube 10. By applying the teachings of this invention, as given above, a mixer with values of spacing and 0: adapted to match the changing Reynolds numbers along the tube can be constructed.

It will be seen that each device constructed according to this invention will be characterized by a specific Reynolds number or, in the case of varying viscosity, by a Reynolds number profile along the length of the device. This number or profile thus becomes a permanent characteristic of the device so that each such device can be said to possess a characteristic Reynolds number. Such term will be used in the above sense in the claims hereof. Thus any user of the device will know the limits of the viscosity and velocity of the fluid which he will mix by means of any given model of the device.

In order to construct a mixer having any characteristic Reynolds number, such a mixer may be assembled, for example, with components as shown in FIG. 4. Each curved element or mixer blade is initially mounted in a separate short length of tubing, the left hand turning element 20 being mounted in a short length of tubing 38 and the right hand turning element 21 in a short length of tubing 40. The spacing between each successive pair of elements is determined by the length of a simple piece of tubing 42 interposed between the lengths of tubing 30 and 40. Having predetermined the spacing by applying the principles of this invention, the length of 40 is so selected as to result in such spacing when the tubing members 38, 42 and 40 are assembled and secured to each other, in the order as indicated in FIG. 4. Likewise, having predetermined the angle a, the tubing elements are rotated on their axes with respect to each other until the desired angle is achieved, whereupon the members 38 and 40 are held fixed in such position until the parts have been secured to each other. Depending upon the material of which the members 38, 40 and 42 are made, any means of fastening such members together may be used, such as brazing, welding, gluing, plastic setting, clamping or the like.

It has been found that when a device as shown in Armeniades et al. is compared with a device constructed in accordance with this invention, a less expensive device results with a lower cost of operation due to fewer mixer elements and lower pump pressures required for the same mixing action.

What is claimed is:

1. A device for mixing fluid components which comprises:

(a) a conduit through which a stream of said components is adapted to flow, said conduit containing a plurality of curved sheet-like elements extending longitudinally within said conduit, each of said elements extending substantially to the inner walls of said conduit;

(b) successive elements being spaced from each other to provide a plenum between successive elements, whereby the body of fluid is caused to rotate by such elements and to continue to rotate as a body in the same direction as it passes along said plenum;

(c) the length of each plenum being of the order of or less than the characteristic homogeneity loss distance at the characteristic Reynolds number of said device;

(d) each successive element being curved in the opposite sense to that of the preceding element;

(e) the leading edge of each successive element being disposed to intercept said body at a substantial angle to the line of said body along which the trailing edge of the preceding element has divided said body of fluid.

2. A device according to claim 1 wherein said angle is substantially a right angle.

3. A device according to claim 1, wherein the characteristic Reynolds number of said device is greater than about References Cited UNITED STATES PATENTS 3,297,305 1/1-967. Walden 259-4 3,286,992 11/1966 Armeniades et al. 259-4 v FOREIGN PATENTS 735,033 8/1932 France 259-4 WALTER A. SCHEEL, Primary Examiner A. I. CANTOR, Assistant Examiner

Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3733057 *Sep 7, 1971May 15, 1973Cons Paper IncIn-line fluid mixer
US3799509 *Mar 2, 1972Mar 26, 1974Du PontMixer for a melt spinning apparatus
US3848507 *Oct 27, 1972Nov 19, 1974Ici Australia LtdPipeline for delivering cross-linked slurried explosives
US3860217 *Apr 26, 1973Jan 14, 1975Kenics CorpShear mixer
US3861652 *Nov 15, 1972Jan 21, 1975Du PontMixing device
US3871624 *May 18, 1972Mar 18, 1975Sulzer AgMixing apparatus and method
US3923288 *Dec 27, 1973Dec 2, 1975Komax Systems IncMaterial mixing apparatus
US3953002 *Sep 21, 1973Apr 27, 1976England Jr Herbert CMotionless mixing device
US3999592 *Apr 21, 1975Dec 28, 1976The Quaker Oats CompanyApparatus and method for manufacturing cores and molds with static mixer stage
US4026967 *Jun 25, 1976May 31, 1977E. I. Du Pont De Nemours And CompanyProcess for making grafted polymeric material
US4051065 *May 18, 1976Sep 27, 1977Nalco Chemical CompanyApparatus for dissolving water soluble polymers and gums in water
US4109318 *Apr 15, 1977Aug 22, 1978General Signal CorporationFluid injection and sampling device for an in-line blender
US4123178 *Mar 21, 1977Oct 31, 1978General Signal CorporationIn-line blender
US4179222 *Jan 11, 1978Dec 18, 1979Systematix Controls, Inc.Flow turbulence generating and mixing device
US4208136 *Dec 1, 1978Jun 17, 1980Komax Systems, Inc.Static mixing apparatus
US4216085 *Aug 18, 1978Aug 5, 1980Iowa Beef Processors, Inc.Flotation method and apparatus
US4281935 *Jan 25, 1980Aug 4, 1981E. I. Du Pont De Nemours And CompanyAdditive injection valve
US4284105 *Nov 9, 1979Aug 18, 1981Union Carbide CorporationDiscrete spiral flow imparting device
US4404173 *Sep 24, 1980Sep 13, 1983Unc Recovery CorporationApparatus for contacting substantially immiscible liquids
US4408038 *Mar 29, 1982Oct 4, 1983E. I. Du Pont De Nemours & Co.In-line coagulation process for fluoroelastomer emulsions
US4408893 *Apr 28, 1982Oct 11, 1983Luwa A.G.Motionless mixing device
US4439405 *Sep 27, 1982Mar 27, 1984Unc Recovery CorporationMethod for varying the mixing time and proportions in the contacting of substantially immiscible liquids
US4505957 *Dec 13, 1982Mar 19, 1985Nordson CorporationCoating by atomization of high (i.e., about 70-99% by weight) solids film-forming compositions
US4538920 *Mar 3, 1983Sep 3, 1985Minnesota Mining And Manufacturing CompanyStatic mixing device
US4747697 *Dec 22, 1986May 31, 1988Hisao KojimaFluid mixer
US4749527 *Sep 5, 1986Jun 7, 1988Rasmusen Hans CStatic aerator
US4776704 *Dec 15, 1986Oct 11, 1988Dentsply Research & Development Corp.Mixing and dispensing syringe
US4840493 *Nov 18, 1987Jun 20, 1989Horner Terry AMotionless mixers and baffles
US4848920 *Feb 26, 1988Jul 18, 1989Husky Injection Molding Systems Ltd.Static mixer
US4850705 *Sep 22, 1988Jul 25, 1989Horner Terry AMotionless mixers and baffles
US5053202 *Aug 2, 1990Oct 1, 1991Olin CorporationStatic mixer configuration
US5063000 *May 3, 1989Nov 5, 1991Mix Thomas WPacking elements
US5225168 *Sep 3, 1991Jul 6, 1993Caterpillar Inc.Static mixing apparatus
US5370273 *Oct 16, 1991Dec 6, 1994Minnesota Mining And Manufacturing CompanyMulti-component applicator assembly
US5407607 *Nov 9, 1993Apr 18, 1995Mix; Thomas W.Structured packing elements
US5549820 *Mar 4, 1994Aug 27, 1996Eastman Kodak CompanyApparatus for removing a component from solution
US5578254 *Apr 14, 1995Nov 26, 1996Mix; Thomas W.Structured packing elements
US5688401 *May 16, 1996Nov 18, 1997Eastman Kodak CompanyApparatus for removing silver from spent photoprocessing solution
US5695645 *May 16, 1996Dec 9, 1997Eastman Kodak CompanyMethods for removing silver from spent photoprocessing solution
US5759603 *Nov 15, 1996Jun 2, 1998Kellogg CompanyProcess for producing a food product having a distinct phase
US5830943 *Jul 23, 1996Nov 3, 1998Dsm N.V.Process for the preparation of a modified polymer for powder paints
US5997516 *Dec 18, 1995Dec 7, 1999Imperial College Of Science, Technology & MedicineModified cannula
US6077470 *Oct 14, 1998Jun 20, 2000The Penn State Research FoundationMethod and apparatus for balancing the filling of injection molds
US6079868 *Mar 2, 1998Jun 27, 2000Advanced Bio Surfaces, Inc.Static mixer
US6312670 *Apr 2, 1998Nov 6, 2001R. Eric MontgomeryTooth bleaching compositions
US6322773 *Aug 13, 1999Nov 27, 2001R. Eric MontgomeryTooth-bleaching compositions
US6365080Jun 9, 1999Apr 2, 2002Ronald J. PariseMethod of making a multi-portion mixing element
US6503438Jun 28, 2001Jan 7, 2003Beaumont Runner Technologies, Inc.Method and apparatus for balancing flowing conditions of laminar flowing materials
US6506949Mar 1, 2001Jan 14, 2003Dow Global Technologies, Inc.Process for ring nitrating aromatic compounds in a tubular reactor having static mixing elements separated by coalescing zones
US6511635 *May 24, 1999Jan 28, 2003Total Raffinage Distribution S.A.Fluid state catalytic cracking reactor having solid fastened packing element for homogeneously distributing particle flow
US6514543 *Oct 31, 2001Feb 4, 2003R. Eric MontgomeryTooth bleaching compositions
US6536628 *Oct 31, 2001Mar 25, 2003R. Eric MontgomeryTooth-bleaching compositions
US6596242 *Nov 8, 1999Jul 22, 2003Shell Oil CompanyReactor riser of a fluidized-bed catalytic cracking plant
US7041218Jun 9, 2003May 9, 2006Inflowsion, L.L.C.Static device and method of making
US7045060Dec 5, 2003May 16, 2006Inflowsion, L.L.C.Apparatus and method for treating a liquid
US7303732Jul 3, 2002Dec 4, 2007Dow Global Technologies Inc.Tubular reactor having static mixing elements separated by coalescing zones
US7331705Dec 5, 2002Feb 19, 2008Inflowsion L.L.C.Static device and method of making
US8123394Oct 11, 2006Feb 28, 2012Evonik Degussa GmbhMixer for liquid colorants and method for mixing liquid colorants
US8137729Dec 14, 2006Mar 20, 2012General Mills, Inc.Method of making complexed fat compositions
US9038725Jul 10, 2012May 26, 2015Halliburton Energy Services, Inc.Method and system for servicing a wellbore
US9421506 *Jun 14, 2013Aug 23, 2016Nov North America I/P, LlcStatic mixer
US20020141951 *Nov 1, 2001Oct 3, 2002R. Eric MontgomeryTooth bleaching compositions
US20030009064 *Jul 3, 2002Jan 9, 2003Gillis Paul A.Tubular reactor having static mixing elements separated by coalescing zones
US20050094482 *Oct 20, 2004May 5, 2005Nordson CorporationMethod and apparatus for producing closed cell foam
US20070140045 *Oct 11, 2006Jun 21, 2007Degussa AgMixer for liquid colorants and method for mixing liquid colorants
US20090162507 *Dec 14, 2006Jun 25, 2009Zietlow Philip KMethod of making complexed fat compositions
US20110220371 *Mar 11, 2010Sep 15, 2011Halliburton Energy Services, Inc.System and method for fluid treatment
US20130336084 *Jun 14, 2013Dec 19, 2013Chemineer, Inc.Static Mixer
DE2549424A1 *Nov 4, 1975May 26, 1976Ford Werke AgGeraet zum verspruehen eines fluids mittels eines druckgases, insbesondere mit druckluft betriebene spruehpistole
DE102011006793A1 *Apr 5, 2011Oct 11, 2012Behr Gmbh & Co. KgAbgaskühler
EP0311409A1 *Oct 6, 1988Apr 12, 1989Ceske Vysoke Uceni Technicke V Praze, RektoratArrangement for continuous mixing of fluids
EP1023152A1 *Oct 14, 1998Aug 2, 2000The Penn State Research FoundationMethod and apparatus for balancing the filling of injection molds
EP1023152A4 *Oct 14, 1998Jun 19, 2002Penn State Res FoundMethod and apparatus for balancing the filling of injection molds
WO1984002088A1 *Nov 29, 1983Jun 7, 1984Merix CorpPacking unit
WO1999019129A1 *Oct 14, 1998Apr 22, 1999The Penn State Research FoundationMethod and apparatus for balancing the filling of injection molds
WO2001064333A2 *Mar 1, 2001Sep 7, 2001The Dow Global Technologies Inc.Tubular reactor, process for conducting liquid/liquid multiphase reactions in a tubular reactor, and a process for ring-nitrating aromatic compounds
WO2001064333A3 *Mar 1, 2001Feb 21, 2002Dow Chemical CoTubular reactor, process for conducting liquid/liquid multiphase reactions in a tubular reactor, and a process for ring-nitrating aromatic compounds
WO2007081637A2Dec 14, 2006Jul 19, 2007General Mills, Inc.Method of making complexed fat compositions
WO2015080834A1 *Nov 3, 2014Jun 4, 2015Phillips 66 CompanySequential mixing process for improved desalting
WO2016043614A3 *Aug 31, 2015Jun 16, 2016Micula ViorelModular system for swirly driving and controlled orientability of hot air flows
U.S. Classification366/338, 422/257, 138/42
International ClassificationB01F5/06, F28F13/00, F28F13/12
Cooperative ClassificationA61M2025/0073, B01F5/061, F28F13/12, B01F5/0615
European ClassificationF28F13/12, B01F5/06B3B6B, B01F5/06B3B
Legal Events
Oct 29, 1990ASAssignment
Effective date: 19870331
Oct 29, 1990AS06Security interest
Effective date: 19870331