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similar approach is followed when designing limited agitation zones in larger vessels: for example, a low consistency extraction zone in a high-density pulp storage tower. These procedures are not linked directly to suspension rheology, although suspension rheology certainly dictated the correlations. Adjustments can be made depending on the pulp type used (through factors). However, these design procedures provide no indication of the degree of motion generated in the suspension. (Indeed, the original data upon which the correlations were developed are not given.) Computational uid dynamics permits solution of the entire suspension ow eld, although considerable computer power is needed. CFD has been applied to pulp suspension agitation by Bakker and Fasano (1993), who treated the pulp suspension as a Bingham uid. Calculations were rst performed assuming turbulent ow. The turbulent shear rate was then compared with the shear rate required to disrupt the ber network. If the shear was insuf cient, calculations were redone for laminar ow. Calculated suspension velocities of less than 0.001 m/s were treated as being stationary. The simulation solutions corresponded to visual observations made in a laboratory chest, although the size of the agitated region was underpredicted. Turbulent motion was often limited to the immediate vicinity of the impeller. Clearly, more work needs to be done in the area of macroscale mixing of ber suspensions. Links are needed between suspension rheology, the desired process outcome (i.e., degree of suspension motion), and the chest design. The ability to design a blending system with known process dynamics is needed. This would also enable the synergism between process control and mixing to be fully exploited. Pulp processing devices are also used to mix and simultaneously produce physical changes to the pulp. One example of this is in repulping operations.

Conclusion from Test #2: cipherEx1.D results from a monoalphabetic sub-stitution. Having rejected T and M . . . Test #3: ` Use the k-test to determine that the encipherment is Vigenere.

Most industrial mixers can be broadly classi ed into the following categories: Tumbling mixers (V-cone, double cone, etc.) Agitated mixers Paddle and plow mixers Ribbon mixers (vertical and horizontal) Screw mixers (vertical and horizontal and orbiting types) Sigma-blade and Z-blade mixer Forberg mixer Gravity silo blenders Pneumatic blenders High intensity mixers Henschel mixer Paddle mixer High-intimacy or high-shear mixer Muller mixer Compaction rollers A brief description, typical operating ranges, and practical application information for these mixers follow.

the left color slider and the right color slider. The Location percentage value defines how close you click to either end with 0% on the left and 100% on the right. In other words, the closer you click to the left end, the closer that color is to the left slider. If you then click the square marker, it becomes selected. You can tell when a gradient marker is selected because the small triangle above it turns dark. When selected, you can change its color by selecting a new color in the Color panel. You can add up to 32 color stops between the two end colors. When a color stop is selected, typing a different percentage in the Location field on the right changes the color stop s position. When a color stop is selected, you can also change its opacity by typing a value in the Opacity field in the lower left of the panel.

When the Scale Strokes & Effects feature is on, it automatically increases and reduces line weights and applied effects relative to an object when you uniformly scale that object manually. For example, if a path has a stroke weight of 1 point and you reduce the path uniformly by 50%, the stroke weight changes to 0.5 points.