EP0865310A4

EP0865310A4 - A dynamically enhanced v-blender

Info

Publication number: EP0865310A4
Application number: EP96936994A
Authority: EP
Inventors: Priscilla A Robinson; Fernando J Muzzio; Dean Brone; Kevin Connor; Carolyn Wightman
Original assignee: Merck and Co Inc; Rutgers State University of New Jersey
Current assignee: Merck and Co Inc; Rutgers State University of New Jersey
Priority date: 1995-10-30
Filing date: 1996-10-25
Publication date: 1998-12-30
Also published as: EP0865310A1; WO1997016240A1; JPH11514569A; AU7476896A; AU717407B2; CA2236009A1

Abstract

A study was done to compare the performance of a conventional V-blender to a V-blender that incorporates perturbations of the particle flow by rocking the mixing vessel during its normal rotation. Mixing was investigated using glass beads with sizes from 66ν to 600ν in vessels of approximately one liter volume. Mixture uniformity was assessed qualitatively, using two different methods. One method involved a transparent mixing vessel where it was possible to see particle flow patterns and assess the state of the mixture at its surface during the entire experiment. The second method involved disposable aluminum mixing vessels, where the mixture was solidified by infiltrating the mixture with a binder. By slicing the solidified structure, it was possible to assess the entire state of the mixture including its interior structure after the completion of each experiment. Mixture uniformity was also assessed quantitatively using image analysis of the slices. For both particles sizes, the extent of mixing was greatly enhanced using the rocking V-blender compared to the conventional V-blender.

Description

TITLE OF THE INVENTION

A DYNAMICALLY ENHANCED V-BLENDER

BACKGROUND OF THE INVENTION V-blenders are widely used in many industries requiring blending, granulating, and drying of powders. V-blenders (also referred to as twin shell blenders) are a type of tumbling mixer consisting of two hollow cylindrical shells or legs, usually of equal length joined at a 90 degree angle (Figure 1). The mixing vessel is typically connected to a rotating shaft which causes a tumbling motion of the powders within the vessel or shell. The rotating shaft is usually parallel to the ground and peφendicular to the plane of symmetry of the blender. The V-blender may be fitted with an intensifier bar which rotates as much as 100 times the speed of the shell. The intensifier bar is typically positioned along the axis of rotation of the shell. V-blenders are used both in the laboratory as small-scale product development units and in manufacturing as large-scale production units.

Many existing V-blenders use constant speed tumbling motion to mix powders, e.g., V-blenders manufactured by Paul O. Abbe Inc. (Little Falls, NJ), Bowers Process Equipment Inc. (Stafford, ON), Gemco (Middlesex, NJ), Jaygo, Inc. (Mahwah, NJ), Lowe Industries Inc., (Cadiz, KY), Patterson Industries Ltd. (Scarborough, ON), and Patterson-Kelley (East Stroudsburg, PA). In most cases, a mixture is considered well mixed when the standard deviation of samples taken from the mixture are equal to the standard deviation of a random mixture or fall within an acceptable variation for a particular application.

There have been numerous reports of incomplete or slow mixing in these devices. Gray found that a mixture of sand and ilmenite continued to improve its mixedness even after 1000 revolutions at 24 φm. (Gray, J., "Solids Mixing Equipment", Chem. Eng. Progr., 53, (1957), 25). Wiedenbaum et al. found that a random mixture of same- sized sand and salt particles was not obtained even after 5000 revolutions at 24 φm. (Weidenbaum, S.S., et al., "Mixing of Solids in a Twin Shell Blender", Ceramic Age, 79, (1963), 39) Chowhan and Linn found that it took approximately 1100 revolutions at 24 φm to obtain a well mixed system of a cohesive drug with a free flowing excipient. (Chowhan, Z.T., et al., "Mixing of Pharmaceutical Solids, Powder Technology 24, (1979), 237) Cahn, et al. needed 1000 revolutions at 24 φ to obtain a well mixed system of same sized CaCθ3 and Siθ2 particles. (Cahn, D.S., et al., "Blender Geometry in the Mixing of Solids", Ind. Eng. Chem., PD&D, 4, (1965), 318) Carstensen and Patel found that a system of same-sized lactose and cornstarch was not sufficiently mixed in 500 revolutions at 24 φm. (Cartensen, J.T., et al., "Blending of Irregularly Shaped Particles, Powder Technology, 17, (1977), 273) Harnby found that a mixture of millet and salt exhibited significant segregation after 1000 revolutions at 33 φm. (Harnby, N., "A Comparison of the Performance of Industrial Solids Mixers Using Segregating Materials, Powder Technology, 1 , ( 1967) 94) Samyn and Murthy found that 1 18μ aspirin and 87μ lactose took 60 minutes to mix, although the rotation rate was not specified. (Samyn, J.C., et al., "Experiments in Powder Blending and Unblending, J. Pharm. Sci. 63, (1974) 371). The main type of segregation in these experiments was found to be axial segregation. A conventional V-blender has no mechanism to induce flow in this direction, hence segregated regions may persist for long times. Three variations from the conventional V- blender may improve mixing by perturbing the axial flow. These include V-blenders with (1 ) legs of different lengths (P-K Cross- Flow™ Blender, Patterson Kelley, East Strousburg, PA), (2) the rotating shaft mounted parallel to the ground but offset from the orthogonal to the plane of symmetry of the blender (Challenger ™ Offset™ V-Blender, Lowe Industries, Inc., Cadiz, KY), and (3) rotating blades mounted to rotate in the plane of the 'V of the blender (Chopper blades, Lowe Industries, Inc., Cadiz, KY)

An improved mixing method is disclosed in this patent application, consisting of a V-blender wherein mixing is enhanced by a controlled axial flow perturbation. As an example, perturbations are introduced by rocking the device with respect to its axis. Such perturbations produce a convective axial flow, resulting in large accelerations of the mixing process. It is claimed that similar enhancements could also be obtained by using other means to perturb the flow of particles.

SUMMARY OF THE INVENTION

The invention relates to a method for enhancing the mixing of solids using a V-blender and a controlled axial flow perturbation. Also within the scope of this application is the V-blender apparatus capable of introducing a controlled axial flow perturbation to enhance the mixing of solids.

BRIEF DESCRIPTION OF THE FIGURES The file of this patent contains at least one drawing executed in color. Copies of this patent with color drawing(s) will be provided by the Patent and Trademark Office upon request and payment of the necessary fee.

Figure 1.

Schematic of a V-blender (twin shell blender) mixing vessel.

Figure 2.

Schematic of a Plexiglas V-blender mounted within a Plexiglas cylinder (a) frontal view and (b) side view at a 90 degree angle to frontal view.

Figure 3.

Vessel loading procedure: (a) plunger inserted, (b) red beads are added to one leg, (c) green beads are added to second leg, and (d) vessel turned to upright position.

Figure 4.

Initial conditions for mixing experiments, beads are initially segregated into the two legs. Figure 5.

Schematic of V-blender mounting for the metal vessel (a) frontal view and (b) side view at a 90 degree angle to frontal view.

Figure 6.

Schematic of infiltration apparatus including fluid reservoir, pump, and solution delivery system.

Figure 7.

Slicing pattern for solidified mixtures.

Figure 8.

Exterior structure of 600 micron particles mixed at 16 φm for (a) 5 minutes without rocking, (b) 45 minutes without rocking, and (c) 5 minutes with a rocking ratio of 3.14 revolutions per rocking cycle where the rocking motion is at +/-10 degrees.

Figure 9. Interior mixing patterns of 66 micron particles mixed at 16 φm for 10 minutes with (a) no rocking and (b) a rocking ratio of 3.14 revolutions per rocking cycle where the rocking motion is at +/-10 degrees.

Figure 10. Schematic of the image analysis equipment setup.

Figure 1 1.

Schematic of a slice with the field subdivisions.

Figure 12.

Influence of mixing parameters on the bead composition profile after mixing at 16 φm for 10 minutes (a) without rocking and (b) with rocking at +/-10 degrees at a rocking ratio of 3.14 revolutions per rocking cycle. Figure 13.

Photographs of the solidified left edge slice (top), center slice (middle), and right edge slice (bottom) where the red and green beads were initially in the left and right legs, respectively for (a) pure rotation and (b) rotation with rocking.

Figure 14.

Probability distribution functions of red bead concentrations for: solidified left edge slice Fig. 14(A) pure rotation and Fig. 14(B) rotation with rocking (sheet 14/17); solidified center slice Fig. 14(C) pure rotation and Fig. 14(D) rotation with rocking (sheet 15/17); and solidified right edge slice Fig. 14(E) pure rotation and Fig. 14(F) rotation with rocking(sheet 16/17).

Figure 15.

Probability distribution functions of the overall red bead concentration for (a) pure rotation and (b) rotation with rocking (sheet 17/17).

DETAILED DESCRIPTION OF THE INVENTION

The invention relates to a method for mixing solids in a V- blender comprising controlled axial flow perturbations.

An embodiment of this method is where the controlled axial flow perturbation is selected from the group consisting of: (a) rotation of the shell with a rocking motion,

(b) time-dependent rotation speed of the shell with a rocking motion,

(c) time-dependent, reversible rotation direction of the shell with a rocking motion, (d) rotation of the shell with a ribbon rotation, and

(e) rotation of the shell with a time-dependent direction of rotation of the ribbon attached to an intensifier bar. The method wherein the controlled axial flow perturbation s introduced by combined rotation of the shell with rocking motion, which is defined by a rocking angle of about 0 degrees to about +10 degrees or -10 degrees, a speed of rotation of about 0 to about 50 φm, and a rock to roll frequency of about 0 to about 31.4. The preferred conditions for the combined rotation of the shell with rocking motion are defined by a rocking angle of about +10 degrees to about -10 degrees, and a rock to roll frequency of about 1.8.

The method wherein the controlled axial flow perturbation is introduced by combined time-dependent rotation speed of the shell with rocking motion, and is defined by a speed of rotation of about 0 to about 50 φm, a frequency of rotation rate changes per revolution of about 0 to about 1 , a rocking angle of about 0° to about +10 degrees or - 10 degrees, and a rock to roll frequency of about 0 to about 31.4.

The method wherein the controlled axial flow perturbation is introduced by combined time -dependent rotation direction of the shell with a rocking motion, and is defined by a speed of rotation of about 0 to about 50 φm, and a frequency of rotation direction changes per revolution of about 0 to about 1 , rocking angle of about 0° to about +10 degrees or -10 degrees, and a rock to roll frequency of about 0 to about 31.4. The method wherein the controlled axial flow perturbation is introduced by combined rotation of the shell with ribbon rotation, and is defined by a speed of the shell of about 0 to about 50 φ and a ribbon speed of about 0 to about 3600 φm.

The method wherein the controlled axial flow perturbation is introduced by combined rotation of the shell with time -dependent ribbon rotation speed, and is defined by a speed of the shell of about 0 to about 50 φm, a ribbon speed of about 0 to about 3600 φm and frequency of ribbon rotation direction changes per shell revolution of about 0 to about 1. A V-blender wherein a controlled axial flow perturbation is introduced by:

(a) combining rotation of the shell with a rocking motion,

(b) combining a time-dependent rotation speed of the shell with a rocking motion, (c) combining a time-dependent rotation direction of the shell with a rocking motion,

(d) combining a rotation of the shell with a ribbon rotation, and

(e) combining a rotation of the shell with a time-dependent ribbon rotation direction.

The ribbon rotation is defined as the rotation of a ribbon which is attached to an intensifier bar of a V-blender.

In order to examine the effects of we 11 -controlled flow perturbations on mixing processes inside a partially filled V-blender, a custom-designed mixing apparatus was built. Rotational and rocking motions (Fig. 2) were independently controlled using two stepping motors (Arrick Robotics, Hurst, TX) interfaced to a computer (Gateway 2000, North Sioux City, South Dakota). One motor was directly linked to the drive shaft and enabled the mixing vessel to rotate. The other motor was linked to the frame that housed the drive shaft by means of a screw shaft. It enabled the frame to rotate partially around a pivot and imparted a vertical rocking motion on the mixing vessel. A motor- control computer program was developed to enable precise independent control of both the rotational and rocking frequencies. The program synchronized movement of both motors.

Two types of experiments were used to demonstrate the mixing enhancements obtained by application of rocking motion. In the first experiment, direct visualization of the mixing processes was achieved using commercially available Plexiglas V-blender vessels (Patterson Kelley Company Inc., East Stroudsburg, PA) that were 3 inches in diameter, 6 inches long and had a 90 degree angle connection between shells. These Plexiglas V-blender vessels were fitted inside a 10 inch diameter Plexiglas cylinder, which was suspended on top of two rollers and held in place from above by a third, freely rotating roller (Fig. 2). During a given experiment, the rotation rate, mixing time and number of rotations per rocking cycle were specified, with the remaining parameters necessary to control the motors then being calculated. Each rocking cycle consisted of a 10 degree downward tilt, followed by a rise back to the horizontal position and a 10 degree tilt in the opposite direction. A cycle was complete when the mixer returned to the horizontal position.

Red and blue 600μ glass beads (Jaygo Inc., Union, NJ) were used in the direct visualization experiments. The total loading for each experiment was 50% of the total vessel volume. The vessels were loaded axially, with one color being loaded into each shell. This was done one color at a time. First a plunger was inserted into one end of the twin shell (Fig. 3a). A measured amount of red beads was added into the other end of the shell (Fig. 3b) and the plunger depth was then adjusted until the level of beads was at the centerline of the twin shell. A measured amount of green beads was then carefully added on top of the layer of red beads (Fig. 3c) so that the red/green interface between the beads was maintained along the centerline of the twin shell. Finally, the vessel was carefully turned upright (Fig 3d) and the ends of the twin shell were closed with caps. A photograph of the initial condition for an experiment is shown in Fig. 4.

The second type of experiment was designed to facilitate examination of the structure of the mixture throughout the entire volume of the powder bed. At the end of the mixing experiment, the structure of the mixture was preserved by infiltrating the voids between particles with a polymer solution, which was allowed to cross-link, yielding a solidified monolith. This monolith was subsequently sliced to reveal the internal structure of the mixture. These solidification experiments were carried out in custom-made aluminum twin shell vessels (American Aluminum Co., Mountainside, NJ) that had identical dimensions and were loaded in the same manner as the Plexiglas V- blender vessels. In order to achieve a wider range of rotational and rocking speeds, one of the rollers in the computer-controlled drive was replaced by a shaft with a mounting extension. The twin shell vessels were housed inside a frame attached to the mounting extension (Fig. 5). Red and green 66μ glass beads (Potters Industries Inc., Parsippany NJ) were used in the solidification/slicing experiments. After the mixing run was completed, the twin shell vessel was carefully removed from the mixing apparatus without disturbing the mixture. It was then placed into an infiltration apparatus where it was held in a secure horizontal position. The infiltration apparatus, shown in Fig. 6, consisted of a fluid reservoir, a pump, and tubing connected to a nozzle. The infiltration medium used was a commercially available mixture of SD alcohol 40, water, octylacrylamide, acrylates and butylaminometh- acrylate copolymer (Rave®, Chesebrough Ponds USA Co., Greenwich, CT). The medium was pumped slowly onto the mixture to avoid trapping air in the system. The nozzle was placed at the centerline of the vessel near the wall allowing the medium to flow gently onto the powder bed, which pushed the air out slowly through the open ends of the vessel. Repeated experiments have shown that the infiltration process does not cause any disturbances to the mixture. The embedded mixtures were allowed to dry for a period of about two weeks.

The solidified structures were removed from the vessels and sliced using a bandsaw. First the mixing vessel was sliced along the centerline while the vessel still contained the mixture. The two shells were then cut along the top surface of the solidified beads. After briefly heating the shells, the solidified structures were easily detached from the shell walls and removed from the vessels. The structures were then sliced in half inch intervals along the axis of rotation as shown in Fig. 7. Each experiment resulted in about fourteen sections.

The effect of rocking motion on mixing in a twin shell mixer is shown in Fig. 8. Figure 8a is the state of the mixture after five minutes of pure rotation at 16 φm. A comparison between Fig. 8a and the initial condition (Fig. 4) shows that only a minimal amount of mixing has occurred. Even after 45 minutes of mixing without rocking (Fig. 8b), the red and green beads were not completely mixed. In contrast, Fig. 8c shows the state of the mixture after 5 minutes of mixing at 16 φm with rocking. A ratio of 3.14 revolutions per rocking cycle was used in this experiment. In this case the beads appear to be very well mixed.

The interior mixing patterns were determined for a similar set of conditions and are shown in Fig. 9. After slicing, the slices were rotated 90 degrees to reveal the mixing structure along the axis of rotation. Figure 9a is a photograph of an experiment carried out with a rotation rate of 16 φm for a total mixing time of 10 minutes with no rocking. As can be seen in the photograph, the composition of each slice along the axis of rotation varies greatly from one end of the structure to the other. Figure 9b is a photograph of an experiment carried out using rocking. The experiment corresponds to a rotation rate of 16 φm, the same total mixing time as before (10 minutes) and a ratio of 3.14 revolutions per rocking cycle. In this case the composition is essentially the same for all slices. The entire structure is extremely well mixed; it is only upon careful inspection that one can determine which end of the mixer was initially red and which was initially green. Quantitative mixing data is obtained from the slices using image analysis. Mixture sections are sequentially recorded as digital 8 bit gray-scale images, and analyzed using numerical algorithms. Figure 10 depicts the image analysis equipment setup. A 6510 CCD monochrome camera (Cohu Inc., San Diego, CA) with a Computer 55 mm F/2.8 telecentric video lens (Edmund Scientific Company, Barrington, NJ) is mounted vertically above the image. Sufficiently uniform illumination of the field of view is attained by a fiber optic ring light (Volpi Manufacturing USA, Auburn, NY). This light source is supplied by a 150- watt halogen bulb housed in an Intralux 6000-1 controller (Volpi Manufacturing USA, Auburn, NY). For mixtures of red and green glass beads, a shaφ cut filter (R-60, Newport Coφoration, Irvine, CA) is used to attenuate the shorter wavelengths (690 NM or less) while transmitting the longer wavelengths. Use of such a filter maximizes gray scale contrast of the red and green components. The red component becomes the brightest; the green component, the darkest. Each slice is scanned with the aid of a programmable xy-table (Unidex Aerotech Inc., Pittsburgh, PA) operated remotely by a computer. The video signal is digitally displayed as an 8 bit image (256 gray levels) on an RS-170 picture monitor (Sony Trinitron Model No. PVM-1342C, Sony Coφ., Tokyo, Japan). The output signal from the monitor is sent to an MV20 image processing board (Datacube Inc., Danvers, MA) where the signal is converted from analog to digital. The image is displayed as a gray-scale image on a Sun Workstation (Sun, Mountain View, CA), where an image processing software program (recently developed at the Center for Computer Aids for Industrial Productivity, Rutgers University, Piscataway, NJ) handles the video signal, data retrieval, and storage.

During acquisition, a slice of the mixture is partitioned into separate fields of view, each 5 mm by 6.7 mm. Figure 1 1 shows a sketch of a slice with these field subdivisions. Each field contains approximately 10,000 particles and is digitized into 480 x 512 pixels, with each pixel possessing a gray level on a scale from 0 to 255. During processing, each field of view is further subdivided into regularly spaced regions, hereon called "patches". The local composition is measured for each of these small patches by computing the mean gray level intensity of the pixels in the patch. The patches become the smallest area evaluated in the experiments. Therefore, the patch size determines the scale of examination in the mixing analysis. Although averaging within patches "blurs" some of the image detail, the patches are small, and the large number of patches used in the analysis (10^ to lt)4 per slice) gives a detailed characterization of the composition statistics of the entire mixture.

Statistics such as the mean, mode, and standard deviation are computed for each patch. These data and the raw pixel values of the field image are written in separate files for post-processing and analysis. After the data is collected for a field, the program executes a command to move the xy-table to the next field address. This sequence of data collection and move commands is repeated until the entire slice is scanned.

A quantitative comparison between pure rotation and rotation with rocking is shown in Figure 12, both experiments were carried out under the same conditions as in Figure 9. Composition versus axial position is shown for both conditions. The most striking feature of the graphs is the large disparity in composition between the left half of the twin shell and the right half for the case of pure rotation. Each location in the left half of the shell (originally red) contains at least 70 percent red particles. In the right half of the shell (originally green) all slices contain less than 40 percent red particles. In this case each half of the twin shell is fairly well mixed, however the entire mixture is quite segregated. In the case where rocking is used, the composition of all slices are close to 50 percent. This point can be further illustrated by comparing the left edge, center and right edge slices of each experiment (Figure 13). The qualitative differences seen in the photographs are shown quantitatively in Figure 14. The probability distribution functions for the pure rotation case are quite distinct from each other, demonstrating a lack of mixing in the axial direction. Both experiments show that once particles cross the boundary from one shell to the other, they become mixed relatively quickly as evidenced by the standard deviation of samples within those slices ranging from 5.8% to 6.3%. The center slice in the pure rotation case (Figure 14, view a-2) shows a greater amount of segregation than any other slice due to the slow diffusive mixing of particles across the centerline of the mixer. Correspondingly its standard deviation (9.5%) of sample compositions is 50% greater than any other slice. The case with rocking shows that each slice has approximately the same standard deviation (6%) and has a composition within 10% of the overall mean (52% red). The overall probability density functions for both mixtures are shown in Figure 15. The distribution for the pure rotation case is bimodal, while the case with rocking has a normal distribution. While the means of both mixtures are essentially the same (52% red), the relative standard deviation of the case with pure rotation is 23.9% compared to 6.9% for the case with rocking.

Based on evidence from both the visualization experiments and the solidification experiments, it is apparent that once the beads cross the boundary between a given pair of adjacent slices, the beads become mixed within the slice relatively quickly. Hence, it is the slow motion along the axis that limits the mixing process in a conventional V- blender. The effect of the rocking motion is to add a convective flow to the system in the axial direction. It is apparent from the experimental evidence that a V-blender such as the one described in this application, in which axial convective motion across the centerline of mixing vessels is added, will greatly enhance the rate of mixing and hence reduce the mixing time.

The techniques described in this application can be applied directly to the design of small scale lab equipment. Although size and weight concerns may prevent the application of rocking to large scale equipment, axial flow perturbations could be used in a different manner to yield similar enhancements. One method of accomplishing this is to use a rotating ribbon attached to an intensifier bar which could be retrofitted in large scale equipment. Efficient mixing would be accomplished by repeatedly reversing the direction of rotation of the ribbon, creating an axial flow across the center boundary necessary to enhance mixing in the same manner as if rocking had been applied.

The effects of flow perturbations on the mixing rate in a V- blender were examined. Rocking motion perturbs the rotational particle flow by adding a convective flow component in the axial direction. Mixing is greatly enhanced by such flow perturbations. On a laboratory scale, same size particles are mixed faster and more thoroughly using a rocking V-blender than a conventional V-blender. Commerical V-Blenders can be modified so as to produce the axial flow perturbations described herein and create an improved V- blender capable of enhanced mixing. An example of such modification is wherein an intensifier bar in a V-blender is fitted with a rotating ribbon capable of creating a controlled perturbation of the flow. In addition, the motors for the shell and/or intensifier bar could be replaced with a variable speed reversible motors equipped with programmable controllers.

Claims

WHAT IS CLAIMED IS:

1. A method for mixing solids in a V-blender comprising controlled axial flow perturbations.

2. The method as recited in Claim 1 , wherein the controlled axial flow perturbation is introduced by combining:

(a) rotation of the shell with a rocking motion,

(b) time-dependent rotation speed of the shell with a rocking motion,

(c) time-dependent, reversible rotation direction of the shell with a rocking motion,

(d) rotation of the shell with a ribbon rotation, and

(e) rotation of the shell with a time-dependent direction of rotation of the ribbon attached to an intensifier bar.

3. The method as recited in Claim 2, wherein the controlled axial flow perturbation is introduced by combining rotation of the shell with rocking motion.

4. The method as recited in Claim 3, wherein the controlled axial flow perturbation is introduced by combined rotation of the shell with rocking motion, which is defined by a rocking angle of about 0 degrees to about +10 degrees or -10 degrees, a speed of rotation of about 0 to about 50 φm, and a rock to roll frequency of about 0 to about 31.4.

5. The method as recited in Claim 4, wherein the controlled axial flow perturbation is introduced by combined rotation of the shell with rocking motion, which is defined by a rocking angle of about +10 degrees to about -10 degrees, a speed of rotation of about 0 to about 50 φm, and a rock to roll frequency of about 1.8. 6. The method as recited in Claim 2, wherein the controlled axial flow perturbation is introduced by combining time- dependent rotation speed of the shell with rocking motion.

7. The method as recited in Claim 6, wherein the controlled axial flow perturbation is introduced by combined time- dependent rotation speed of the shell with rocking motion, which is defined by a speed of rotation of about 0 to about 50 φm, a frequency of rotation speed changes per revolution of about 0 to about 1 , a rocking angle of about 0° to about +10 degrees or - 10 degrees, and a rock to roll frequency of about 0 to about 31.4.

8. The method as recited in Claim 2, wherein the controlled axial flow perturbation is introduced by combining time- dependent rotation direction of the shell with a rocking motion.

9. The method as recited in Claim 8, wherein the controlled axial flow perturbation is introduced by combined time- dependent rotation direction of the shell with a rocking motion, which is defined by a speed of rotation of about 0 to about 50 φm, a frequency of rotation direction changes per revolution of about 0 to about 1 , a rocking angle of about 0° to about +10 degrees or - 10 degrees, and a rock to roll frequency of about 0 to about 31.4.

10. The method as recited in Claim 2, wherein the controlled axial flow perturbation is introduced by combining rotation of the shell with ribbon rotation.

1 1. The method as recited in Claim 10, wherein the controlled axial flow perturbation is introduced by combined rotation of the shell with ribbon rotation, which is defined by a speed of the shell of about 0 to about 50 φm and a ribbon speed of about 0 to about 3600 φm. 12. The method as recited in Claim 2, wherein the controlled axial flow perturbation is introduced by combining rotation of the shell with time-dependent ribbon rotation speed.

13. The method as recited in Claim 12, wherein the controlled axial flow perturbation is introduced by combined rotation of the shell with time-dependent ribbon rotation speed, which is defined by a speed of the shell of about 0 to about 50 φm, a ribbon speed of about 0 to about 3600 φm and frequency of ribbon rotation direction changes per shell revolution of about 0 to about 1.

14. A V-blender wherein a controlled axial flow perturbation is introduced by:

(a) combining rotation of the shell with a rocking motion, (b) combining a time-dependent rotation speed of the shell with a rocking motion,

(c) combining a time-dependent rotation direction of the shell with a rocking motion,

(d) combining a rotation of the shell with a ribbon rotation, and (e) combining a rotation of the shell with a time-dependent ribbon rotation direction.