SHEAR PROCESSING OF TiO2 SLURRIES

Abstract: A process for enhancing the optical efficiency of TiO2 slurries starting from base TiO2 particles having less than about 65 weight % particles, greater than 0.6 microns, and shear processing a slurry at a solid content of at least 83 % by weight.

Description: SHEAR PROCESSING OF TiOj SLURRIES BACKGROUND OF THE INVENTION This invention relates to the preparation of titanium dioxide in an aqueous slurry and more particularly an improved slurry suitable for production of paper or paperboard applications having enhanced optical properties. Certain finishing steps are required to be performed on conventional Tiθ2 slurries such as filtering, washing, drying, micronizing and reslurrying. Conventional finishing steps are more expensive and laborious. Conventional slurries are prepared using pigment that has been micronized so the particles are relatively easy to disperse in water. Base Tiθ2 as defined hereinbelow is highly aggregated and agglomerated. If the solids concentration is high, the viscosity becomes too high and dry base Tiθ2 particles cannot be readily incorporated into the slurry. Heretofore, base Tiθ2 has not been used to directly process a slurry at greater than 83% solids concentration. For example, U.S. Patent 5,356,470 describes a sluπy process operating at 79-83% solids content and a process for media milling pigment slurries to eli ninate or reduce oversize particles with a particle size distribution between 10-44 microns for enhanced smoothness of paper and paperboard applications. No mention is made therein regarding opacity or a uniform, narrow particle size distribution of smaller particles. One important property of Tiθ2 is its ability to opacify. An efficient, economical process that directly produces a slurry with a naπow particle size distribution by operating at a high solids concentration with dry base Tiθ2 particles readily incoφorated into the slurry is therefore needed. Concomitantly, there is a need to produce an aqueous Tiθ2 slurry with improved optical efficiency. The present invention meets these needs. SUMMARY OF THE INVENTION In accordance with this invention there is provided a process for preparing an improved Tiθ2 slurry directly from base Tiθ2 comprising viscous shear processing of base Tiθ2 particles having less than about 65 weight % greater than 0.6 microns, at a solids content of above about 83% by weight, so as to achieve deagglomeration and dispersion of the slurry, while still permitting sufficient fluidity to permit incorporation of the particles into the slurry. Alternatively, viscous shear processing may also be carried out at lower % solids content at higher shear rates . The slurry may be subjected to polishing grind and dispersion. The process is characterized by the following advantages which cumulatively render this process preferable to processes previously employed: 1. Tiθ2 slurry particles having a naπow particle size distribution; 2. improved optical efficiency of the Tiθ2 . 3. elimination/reduction of conventional finishing steps; 4. may be operated continuously to give greatly increased production capacity, more efficient equipment use, and lower cost operation; and 5. improved rheological properties. It has been found that the process of this invention is more efficient and more economical over the processes found in the prior art. Concomitantly, the present process produces product of improved quality and enhanced value in use. DETAILED DESCRIPTION Base Pigment Manufacture. The Tiθ2 used to prepare the pigment can be of a conventional rutile or anatase variety, produced by either a chloride or a sulfate process. The chloride process for producing ΗO2 pigment by reacting oxygen-containing gas, TiC-4 and AICI3 (in amount sufficient to form 0.1-1.5% AI2O3 ) in a vapor phase is known. The oxygen-containing gas can also contain a vaporized alkali metal salt such as CsCl or KCl, etc. which is one of the tools used to control particle growth as described for example in U.S. Patent 5,201,949, the teachings of which are hereby incorporated by reference. Alternatively, in the sulfate process, sulfuric acid and ore containing titanium are dissolved and the resulting solution goes through a series of steps to yield Tiθ2- "Base ΗO2" or oxidation discharge is refeπed to herein as ΗO2 directly removed from an oxidation section of the chloride process. In the sulfate process, "base ΗO2" or calciner discharge refers to ΗO2 after a calcination step and before any surface treatments are applied. A prefeπed starting material includes rutile pigment from the chloride process as produced in U.S. Patent 4,214,913, the teachings of which are hereby incorporated by reference. Base ΗO2 particles have on the order of less than about 65% by weight of their particle size greater than 0.6 microns as measured by a laser scattering particle size distribution analyzer, as described hereinbelow. It is a desirable aspect in carrying out the invention that a deagglomerated base ΗO2 is used. There are numerous references in the literature, in combination or alone, which describe the preparation of a base Tiθ2 such as U.S. Patent 4,462,979, U.S. Patent 4,661,322, U.S. Patent 4,937,064, and U.S. Patent 3,505,091, the teachings of which are hereby incorporated by reference. The preparation of the deagglomerated base ΗO2 will depend on the reactor design, flow rate, temperatures, pressures, production rates, flue diameter, velocity in the flue and rate of cooling the reaction mass, but can be determined readily by testing to obtain the desired effects on agglomeration and particle size. For example, in the chloride process the lower the velocity in the flue, the lower the turbulence thereby achieving the deagglomerated base Tiθ2- Preferably, large diameter flues aid in obtaining the deagglomerated base ΗO2. Typically, such deagglomerated base Tiθ2 particles have on the order of about less than 50% by weight greater than 0.6 microns, and preferably less than 40% by weight greater than 0.6 microns as measured by a laser scattering particle size distribution analyzer. Vicscous Shear Processing The term "viscous shear processing" as used herein means mechanical energy applied to a high solids slurry of high viscosity such that it is barely fluid. The particles interfere with each other as they try to flow. This generates local shear rates that are higher than the thick slurry can tolerate thus producing apparent localized dilatancy, i.e., the rapid increase in shear stress for a slight increase in shear rate. These high shear stress zones then break up the agglomerates resulting in improved dispersion. Shear stress zones of increased intensity can provide increased energy to break up the more strongly held agglomerates. Shear zones of increased intensity can occur by increasing the fluid viscosity, preferably by increasing the volume fraction of pigment relative to liquid (such as water) volume fraction. Theoretical maximum deagglomeration would occur at highest possible pigment volume fraction, i.e., 92% Tiθ2 in water converted to weight fraction. The improved slurry is produced by viscous shear processing of the base Tiθ2 particles, preferably deagglomerated base Tiθ2 particles, at a sufficiently high solids content so as to achieve deagglomeration and dispersion of the slurry, while still permitting sufficient fluidity to permit incorporation of the particles into the slurry. Typically, such slurries have at least above about 83% to 92% by weight of solids, preferably above about 83% to 89% by weight of solids and more preferably about 83.5% to 88% by weight of solids. Commercially available dispersants/surfactants such as sodium and potassium pyrophospate, sodium hexametaphosphate, sodium, potassium or ammonium polyphosphate, aliphatic carboxylic acid, citric acid, polyhydroxy alcohols and polyacrylates and the like, and alcohol amines such as l-amino-2- ethanol, 2-amino-l-ethanol, l-amino-2-propanol, 2-amino-2-methyl-l-propanol, diethanolamine, di-isopropanolamine, 2-methylamino-l-ethanol, monoisopropanolamine and triethanolamine and the like, or mixtures thereof are used to produce a stable dispersion. The amount of dispersant/surfactant is not especially critical. Typically, the amount may range from about 0.01 to about 5 % by weight. The process can be carried out continuously or batchwise. For batch slurry processing, the base Tiθ2 is typically added to a tank, i.e., a vessel which already has water and at least one surfactant present. The amount of the starting materials added will be dependent on the size of the tank. The solids level in the tank is slowly increased over time as slurry viscosity increases. As the desired % solids are finally reached, viscous shear processing is carried out as described below, and is continued until substantially complete and desired deagglomeration and dispersion is obtained. The time for complete and desired deagglomeration to occur once the final solids concentration is obtained can vary but is typically very fast, e.g., about 2 to 30 minutes, preferably 2 to 10 minutes. Then, the slurry typically is diluted to a point sufficient to permit slurry handling and transfer. It will be appreciated by those skilled in the art that the slurry is diluted to a desired percent solids of the resulting final slurry product. For example, it may be desirable that the slurry is diluted to less than about 78% solids, preferably about 70-73% sohds, more preferably about 72% solids at a pH greater than 7, preferably between 8 and 10. Additional dispersants may be added during the dilution. The slurry may be screened to remove grit. A particular advantage of this invention is the operation of a highly efficient continuous process that is preferably operated in a single tank. Dry base ΗO2 is continuously and simultaneously added to a tank along with water and at least one dispersant, such that the tank is always maintained at the % solids for good viscous shear processing to occur. Simultaneously with the addition of new material, a portion of the material in the tank is continuously withdrawn by any suitable means, typically from the bottom of the tank by gravity flow, a conveying screw or the like. The material that is withdrawn is immediately diluted with water to give sufficient fluidity for subsequent processing. A dispersant such as an alcohol amine is added simultaneously or separately with the addition of water. Mixing of the viscous material and water takes place in a disperser, separate tank, pump or the like. One advantage of continuous operation is that the process tank is operating at the more efficient viscous shear condition (at final desired sohds content). In batch mode, time is spent charging water and surfactants, increasing solids content to obtain sufficient viscous conditions, diluting to final % solids and transferring diluted slurry from the process tank. In carrying out viscous shear processing of this embodiment, increased agitator speed is used for improved incorporation of the dry pigment particles. Increased speed will enhance the surface vortex which is responsible for drawing the dry pigment particles into the slurry phase for incorporation and subsequent deagglomeration. Increasing the pigment % solids to increase viscous shear can adversely effect the vortex making pigment incorporation more difficult, but this can be offset by increasing the agitator speed. Increased agitator speed has added benefit that the increased speed gives increased shear rate, further enhancing viscous shear processing. Increased agitator energy (power input) is desirable to process the more viscous (higher solids concentration) material with its more intense viscous shear zones. The net result is improved viscous shear conditions that further enhance deagglomeration and result in a final slurry with improved particle size distribution and improved fluid flow properties, as measured by high shear rheology. Specific agitator characteristics depend on the equipment, production rate, blade configuration, etc. For example, agitator tip speed, i.e., linear velocity of an outer tip of a blade on an agitator typically could range from about 4 ft/sec to 55 ft/sec, preferably 6 to 45 ft/sec, and more preferably 14 to 45 ft/sec. Using agitator blades with less pumping action, tip speeds in excess of 55 ft/sec up to about 150 ft/sec may be required. For small scale processing, agitator rpm will be very high but due to small blade diameter, agitator tip speeds could be as low as 4 ft/sec. An energy input of up to about 33 kWh/T of material processed may be used, preferably up to 22 kWh/T, and more preferably between 4 to 11 kWh/T. By using a less agglomerated base pigment, the increase in agitator power required can be rm ' nimized, or the increased agitator power can be used to operate at even higher % solids, giving even further improvement in the viscous shear processing. In an alternative embodiment of the present invention, viscous shear processing is achieved by increasing the shear rate by using high agitator speed while maintaining the slurry solids at about 83% and below. The lower the sohds and less viscous the slurry, the greater the agitator speed required to give shear rates capable of deagglomeration and dispersion. Slurry that has greater fluidity due to its lower solids concentration can be advantageously processed by using greatly increased shear rates. Using a 2 to 25 fold increase in agitator tip speed will produce shear rates capable of viscous shear processing on slurry that is about 78 to 83% sohds. Contemplated shear rates are in excess of 28 ft/sec. It is beheved that even higher shear rates would be capable of accomplishing comparable viscous shear deagglomeration at further reduced slurry % solids, for example, below 78% sohds. It will be appreciated by those skilled in the art that viscous shear processing below 74% solids using a very high agitator speed is possible but not economically advantageous due to extremely high shear rates required. Prefeπed in caπying out this alternative embodiment is equipment with a naπow gap between a stationary surface and a moving surface such as a colloid mill, high speed disperser, rotor- stator mixer or the like. TypicaUy, slurries processed above and before a pohshing grind and dispersion step have a particle size distribution as defined by a geometric standard deviation (GSD), as described hereinbelow, of less than about 1.70, and have ΗO2 particles less than about 40% greater than 0.6 microns, preferably less than 35% greater than 0.6 microns, and more preferably less than 20 to 25% greater than 0.6 microns as measured by a laser scattering particle size distribution analyzer. Polishing Grind and Dispersion After viscous shear processing, the diluted slurry may be subjected to a pohshing grind and dispersion step. The pohshing step is desirable to grind larger particles and further deagglomerate smaller particles for further improved narrow particle size distribution. This may be carried out by a media mill. Contemplated equivalents include a ball mill, colloid mill, attrition mill, Manton-Gaulin mill, high speed disperser, rotor-stator mixer and the like as described in greater detail in Perry's Chemical Engineers Handbook (6th ed.) pp 8-30 to 8-46, the teachings of which are hereby incoφorated by reference. Prefeπed is media milling as described in greater detail in U.S. Patent 5,356,470, the teachings of which are hereby incoφorated by reference. U.S. Patent 5,356,470 showed that media milling was beneficial primarily for controlling large oversize particles within the 10-44 micron range to give improved board coating smoothness. Polishing media milling produces additional synergistic benefits when used in conjunction with continuous operation of the viscous shear processing for substantially complete dispersion. Process equipment is commercially available. In carrying out the invention, the titanium dioxide slurry from viscous shear processing is fed into a grind chamber which is filled with beads. Many types of media or different sizes may be used, with one of ordinary skill in the art being able to adjust the media to produce the desired result based on the size distribution of the particles in the starting material. Typically, a media nominal size range is about 0.3 to 2.5 mm in diameter, preferably about 0.6 to 1.6 mm in diameter, and more preferably 0.6 to 1.0 mm. It has been found that smaller size media and/or increased tip speed reduces the size of particles greater than 0.6 microns, particularly between 0.6 to 2.0 microns, preferably between 0.6 to 1.0 microns. The media is stiπed in the grind chamber by a series of discs attached to a rotating shaft. Typically, a media mill disc tip speed is in the range of about 1800 to 3200 ft/min, preferably about 2000 to 3000 ft/min and more preferably about 2500 to 2800 ft/min. Average residence times in the media mill will vary depending on the size of the media mill. Typically, average residence times will be between about 1 to 10 minutes, preferably about 2 to 5 minutes on a 200L size media mill. If a smaller size media mill is used, a shorter residence time can be used. The motion of the media is peφendicular to the direction in which the slurry is pumped, and therefore the Tiθ2 particles are sheared by the media. Typically, a screen keeps the media inside the grind chamber but allows the Tiθ2 slurry out of the mill. Optionally, the product of the mill can be further screened. Typically, slurries processed according to the invention have, subsequent to polishing grind and dispersion, a naπow particle size distribution as defined by the GSD of less than about 1.64, preferably less than about 1.55, more preferably about 1.35 to 1.50. In addition, Tiθ2 particles having less than about 35% greater than 0.6 microns, preferably less than about 25 and more preferably less than about 10 to 20 % greater than 0.6 microns as measured by a laser scattering particle size distribution analyzer may be achieved. A prefeπed overall process is as follows: Base Viscous Shear Pohshing Grind Improved ΗO2 Pigment — — > Processing (above - > & Dispersion - > Slurry 83% solids diluted to desired % sohds) The resulting improved Tiθ2 slurries are suitable for use in paper, paperboard apphcations, many paint applications, and aqueous inks. The ability for ΗO2 to opacify as measured by light scattering efficiency of Tiθ2 is in part controlled by particle size and uniform dispersion. Suφrisingly, it has been discovered that a naπow particle distribution around or approaching the optimum particle size results in significant enhancements of Tiθ2 scattering efficiency. When Tiθ2 slurry made by the process of this invention is incoφorated into other and varied paper coating applications, optical efficiency improvement will vary ranging from about 3% to greater than 20% with substantially no adverse impact on other paper attributes such as print gloss, shade, grit, etc. To give a clearer understanding of the invention, the following Examples are construed as illustrative and not limitative of the underlying principles of the invention in any way whatsoever. EXAMPLES COMPARATIVE EXAMPLE 1 Base Tiθ2 and slurry was made according to the general teachings of U.S. Patent 5,356,470. 682 grams of water was added to a vessel along with about 11 grams of amino alcohol, and about 24 grams of polyacrylate surfactant. Then over about 20 minutes, 2830 grams of the base Tiθ2 having a particle size of 53 weight % greater than 0.6 microns was added to form a slurry. The slurry with a sohds concentration of about 80% was ground for an additional 30 minutes. The vessel contents were diluted to about 72% solids by adding 409 grams of water and adjusted to a pH of about 9 with amino alcohol. The slurry was screened to 325 Mesh (44 microns) to remove grit. This slurry was then fed to a 1.5 hter Dyno-Mill KDL-Pilot media mill (CB Mills, Buffalo Grove, EL). The media mill was filled to 85% capacity with 1.2- 1.6 mm SEPR ER 120 (Zirconia: Vitreous Silica) grinding media. The mill was operated at mid-speed setting with a disc tip speed of 2000 ft/min. Slurry was continuously fed at a rate of 0.335 liters/min, and the average residence time was about 2 minutes. The slurry was separated from the media by flowing through the rotating gap media separator at the end of the mill. COMPARATIVE EXAMPLE 2 Base Tiθ2 pigment was made as follows. A stream of oxygen preheated to a temperature of 1550°C was introduced into one end of a tubular reactor operated at 44 psig pressure. An alkali metal salt was added to the oxygen stream to control particle size. Titamum tetrachloride vapor stream containing sufficient aluminum trichloride to provide one per cent AI2O3 in the titanium dioxide was introduced into the reactor at 450°C. PCI3 in a vapor phase was added subsequently. The temperature of the reaction mass, upon completion of the reaction to form ΗO2 was in excess of 1500°C. The particle size of the base ΗO2 was 56-65 weight % greater than 0.6 microns measured as described below. Base Tiθ2 was directly made into an aqueous slurry as follows. The 20 t/hr of ΗO2 were added to a continuously stiπed tank, along with about 5 t/hr of water, 180 pph amino alcohol, and 116 pph polyacrylate. The tank was operated with a mixer tip speed of 28 ft/sec, a typical power input of 6 kWh/T ΗO2, and average residence time of about 30 minutes, with a typical solids concentration of 80-81% to achieve slurry deagglomeration. The discharge of the tank was continuously diluted with about 3 t/hr of water, and about 90 pph amino alcohol is added to dehver a product slurry with about 72% sohds and a pH at about 9. The slurry was screened to 325 Mesh (44 microns) to remove grit. This slurry was then fed to a HM-200 media mill (Premier Mill Coφ., Reading PA). The media mill was filled to about 85% capacity, with 1.2-1.6 mm SEPR ER 120 (Zirconia: Vitreous Sihca) grinding media. Slurry was fed at a rate of 10 gpm, and the mill was operated with a disc tip speed of 2000 ft/min. The average residence time was about 3 minutes. The power input was 7.2 kWh/T. Exiting the mill, the slurry was separated from the media by media retaining screens that are part of the mill. EXAMPLE 3 Base Tiθ2 pigment was made the same as Comparative Example 2 except at the exit of the reactor, the flue diameter was immediately expanded by 60 % and the reactor pressure was increased by up to about 11 % thereby decreasing linear velocity by about 40 % from Comparative Example 2. A 14 ppm increase of an alkali metal salt was added to the oxygen stream to control the particle size. These modifications reduced the base pigment agglomeration. The particle size of the deagglomerated base ΗO2 was 35-40 weight % greater than 0.6 microns measured as described below. The deagglomerated base Tiθ2 was directly made into an aqueous slurry as follows. The 20 t/hr of Tiθ2 were added to a continuously stirred tank, along with about 4 t/hr of water, 180 pph amino alcohol, and 116 pph polyacrylate. The tank was operated with a mixer tip speed of about 33 ft/sec, a typical power input of 7.5 kWh/T ΗO2, and average residence time of about 30 minutes, with a typical solids concentration of 83-85% to achieve slurry deagglomeration and dispersion. The discharge of the tank was continuously diluted with about 4 t/hr of water, and about 90 pph amino alcohol is added to deliver a product slurry with about 72% solids and a pH at about 9. The slurry was screened to 325 Mesh (44 microns) to remove grit. The slurry was then fed to a HM-200 media mill as Comparative Example 2 except the improved rheological properties of the slurry reduced the media mill power required to 6.9 kWh/T. EXAMPLE 4 Same as Example 3 except the media mill was filled to 85% capacity, with 0.8-1.0 mm SEPR ER 120 (Zirconia: Vitreous Silica) grinding media. Slurry was fed at a rate of 10 gpm, and the mill was operated with an increased disc tip speed of 2500 ft/min and the power input was 9.1 kWh/T. EXAMPLE 5 Base ΗO2 pigment was made according to Example 3. The particle size of the deagglomerated base pigment was 38 weight % greater than 0.6 microns. The base pigment was converted into a slurry batchwise. Pre-mixed surfactant was prepared, consisting of 20 grams of water, about 4 grams of poiyacylate, and about 2 grams of amino alcohol. Water (63 grams) was added to a vessel. Agitation was provided by an IKA mixer using a 2.1" diameter blade operating at 700 φm (6 ft/sec). Base pigment (500 grams) along with surfactant premix was added to the vessel. Addition rate was slowed as slurry solids and viscosity increased resulting in 85.6% solids. Agitation was continued for 5 minutes to obtain a uniform deagglomerated slurry. Then 100 grams of water and about 1 gram of amino alcohol were added to dilute the slurry to about 73% sohds. After 325 mesh screening, the slurry was media milled using a 1.5 hter Dynomill. The mill was filled to 85% capacity with 0.8 to 1.0 mm grinding media. The disc tip speed was 2800 ft/min. EXAMPLE 6 Batchwise slurry was produced according to Example 5 except that additional pigment and surfactant premix was used to further increase the % sohds to 86.4% solids for viscous shear processing. The slurry was diluted, screened and media milled as in Example 5. PARΗCLE SIZE MEASUREMENTS (a) Laser Scattering Particle Size Distribution Analyzer The particle size of the base Tiθ2 and the slurry product was measured using a laser scattering particle size distribution analyzer, LA-900 instrument (available from Horiba, Kyoto, Japan), calibrated according to the manufacturer's recommendations. The base Tiθ2 prior to dispersion in the tank was prepared as a 3% solids slurry in 0.2 g/L TKPP solution. This mixture was sonicated for 10 minutes on a 7 power setting using a Sonicator Ultrasonic Liquid Processor Model XL 2020 (available from Heat Systems, Inc., Farmingdale, NY) and then the particle size of the base ΗO2 was measured using the Horiba instrument described above. The slurry product was taken directly and mixed with water to a point the LA-900 would operate, as recommended by the manufacturer and then the particle size was measured using the Horiba instrument described above. Average (mass median) particle size is reported as D50. The %>0.6 is the fraction of particles greater than 0.6 microns in size, that is, the amount of particles on a weight basis that are >0.6 microns and would be expected to be deficient in optical efficiency. The width of the particle size distribution is given as the Geometric Standard Deviation (GSD) and is defined as the square root of Dg4/Di6- 1 weight % of particles are smaller in size than the value called D and 84 weight % of particles smaller in size than the value called Dg Ideal mondisperse particles have a minimum GSD of 1.0. (b) X-ray Sedimentometer Previously, particle size measurements have been provided with a Micrometrics 5000 Analyzer, SEDIGRAPH® (Micrometritics Instrument Coφ.), i.e., x-ray sedimentometer, which gives reproducible results, but different absolute values. All data herein and in the claims were determined using the Horiba laser scattering particle size distribution analyzer, but typical results are provided below for ease of comparison of Horiba (1) and SEDIGRAPH® (2) data. Sample D5Q(1) -DipO) %>0.6 m %> 0.6(2) Base .68 .39 58 25 Deagglomerated Base .52 .36 39 12 The slurry samples were prepared in a typical paper coating formulation and coated on Mylar® to measure the optical properties of the coating at 460 and 550 nm. Measurement at 550 nm, a wavelength in the middle of the green region of the visible spectrum, provides a good measure of opacity of the paper coating. Opacity is the primary attribute provided by ΗO2 in paper apphcations. ΗO2 also contributes to paper brightness and results are reported in the blue region (460 nm) where brightness was measured. Comparison of ΗO2- containing coatings versus Tiθ2-free coatings allows calculation of the optical scattering efficiency also refeπed to as hiding power of the titanium dioxide present in the coating, reported as S(Tiθ2). The relative efficiency of the Tiθ2 is determined by assigning the Comparative Example 2 a value of 100. Alternatively, relative scattering efficiency can be compared by measuring optical density of dilute suspensions in water. Below in Table 1 are the data for the Comparative Examples 1-2 and Examples 3-6 in paper coatings. TABLE 1 Particle Size Distribution @460nm @550nm Description DSfo- %>0.6 GSD Comparative Example 1 .445 29.4 1.64 .71 107 .57 104 Comparative Example 2 .483 33.3 1.61 .663 100 .550 100 Example 3 .380 16.4 1.50 .754 114 .596 108 Example 4 .367 13.2 1.46 .770 116 .598 109 Example 5 .338 8.8 1.42 .788 119 .630 114 Example 6 .322 6.7 1.40 .812 122 .649 118 Comparative Examples 1 and 2 show that the productivity advantages of continuous viscous shear processing are realized at a sacrifice in scattering efficiency. The examples of this invention show that even higher light scattering performance can be achieved while maintaining the productivity advantages of the continuous process. Relative to Comparative Example 2, Example 3 demonstrated a 8% improvement in opacification and 14% efficiency of Tiθ2 in the blue region of the spectrum. Example 4 provides further improvements. Example 5 demonstrated a further 5% improvement obtained by processing at 85.6% solids in viscous shear processing of slurry. Example 6 showed an even further improvement by processing at elevated % solids. The particle size distribution between 0.6-1.0 microns and 1.0-2.0 microns was determined using the same technique as described above. The data are summarized below in Table 2. TABLE 2 Example % 0.6-1.0 microns % 1.0-2.0 microns Comparative Example 1 19.8 9.1 Comparative Example 2 23.2 10.1 Example 3 12.6 3.8 Example 4 10.6 2.6 Example 5 8.3 1.7 Example 6 62 1.0 RHEOLOGY Another property improvement is reduction of high shear viscosity. Samples of the slurry feed to the media mill and slurry product were measured for viscosity using a Hercules High Shear Viscometer at a shear rate of about 10,000 reciprocal seconds. Results are reported below in Table 3. TABLE 3 Example High Shear Viscositv Ccp " . Slurrv Feed to Media Mill Slurrv Product Comparative Example 1 33.4 19.4 Comparative Example 2 46.3 24.1 Example 3 30.8 20.9 Example 4 30.8 18.8 Example 5 NM* 10.6 Example 6 NM 11.6 *NM = not measured EXAMPLES 7A AND 7B Samples were prepared using the same base pigment as Example 5 and 6. For Example 7 A the slurry step was identical to Example 5 except that the batch viscous shear processing was done at 83.7% solids. For Example 7B a continuous viscous shear processing was used similar to Example 3. Both examples were media milled using the method of Example 5. These examples were measured for particle size distribution, prior to and subsequent to media milling. Results are provided in Table 4. TABLE 4 Particle Size Distribution % Reduction Media Mill Feed After Media Milling From Media Milling % Improvement Ex. D50 %X).6 GSD 250 %X).6 GSD D50 %X).6 GSD in Hiding Power 5 .342 10.0 1.434 .338 8.8 1.421 1.7% 12.0% 0.9% 1.2 6 .336 9.0 1.429 .322 6.7 1.403 4.1% 25.5% 1.9% 1.4 7A .383 16.9 1.509 .373 14.5 1.474 2.6% 14.2% 2.6% 2.0 7B .417 23.2 1.573 .379 15.8 1.490 9.1% 31.8% 6.5% 5.0 The benefit of media milling continuous processed slurry (Example 7B) is significantly greater than media milling batch processed slurry as shown by the much larger relative change in particle size distribution that occurs from media milling. Batch processing at increased % solids (Example 5 and 6) showed only minor improvement in particle size distribution from media milling, demonstrating that the relative improvement from media milling is less as viscous shear processing is operated at increased % sohds. EXAMPLE 8 Base ΗO2 (as used in Examples 5 to 7) was batch processed. An JXA mixer with a 3.4" diameter blade operated at 700 φm for a 10.3 ft/sec blade tip speed was used to produce a slurry using 2500 grams of base pigment. A total of 569 grams of water was initiaUy added to the vessel along with about 7 grams of alcohol amine and 7 grams of polyacrylic surfactant. After pigment addition was competed, the slurry which was analyzed at 81.7% solids. The slurry was mixed for an additional 5 minutes to assure uniform deagglomeration. A 350 gram sample was withdrawn for dilution, screening and pH adjustment to 9. The remaimng slurry was than subjected to 1400 φm agitator speed (about 21 ft/sec tip speed). As the speed was increased, viscous shear processing lasting for about 1 minute occuπed as the increased shear rate produced further deagglomeration. After mixing for an additional two minutes to assure uniformity, a further 350 gram sample was taken. The remaining material was then mixed for 5 minutes using a 3 inch diameter agitator blade at 3000 rpm, for a 40 ft/sec tip speed. Again a 350 gram sample was removed. Finally, the remaining material was subject to a 257 ft/sec tip speed in a Waring Blender with a 3 inch diameter blade operated at 18000 φm. All samples were diluted to 72% sohds for high shear rheology measurements. The high shear rheology and particle size were run on the samples. EXAMPLE 9 An identical procedure to Example 8 was followed, except that more water was used for the initial slurry preparation so that the solids concentration was 80%. A further identical procedure was followed, except the solids concentration was only 78%. The samples were not media milled. Sample results are provided in Table 5. Examples 7A and 5 results are prior to media milling and are provided in Table 5. TABLE 5 High Shear Particle Size Distribution Relative Ex. Solids ft/sec Viscositv (cp) D50 ΩΣ GSD Hiding Power 8 81.7% 10 19.7 .407 21.4 1.553 105 20 18.2 .382 16.7 1.502 107 40 14.8 .365 13.4 1.467 109 257 13.7 .355 11.3 1.440 110 9 80% 20 19.8 .400 19.7 1.541 NM* 40 17.1 .392 18.1 1.516 NM 257 16.0 .382 16.2 1.490 NM 78% 20 22.01 .463 30.0 1.608 102 40 20.1 .436 25.6 1.576 NM 257 18.2 .412 21.0 1.532 107 7A 83.7% 10 15.0 .383 16.9 1.509 109 5 85.6% 10 10.6 .342 10.0 1.434 112 NM* = not measured Comparable viscous shear deagglomeration to the material processed at 85.6% occuπed at only 82% solid but required 25 times the shear rate. Using only 80% sohds, but operating at 25 times the shear rate gave comparable performance to 83.7% processed material. Even at only 78% sohds, operating at 257 ft/sec tip speed gave acceptable product. This demonstrated that using greatly increased shear rate at lower slurry % sohds can result in improved properties. Having thus described and exemplified the invention with a certain degree of particularity, it should be appreciated that the following Claims are not to be limited but are to be afforded a scope commensurate with the wording of each element of the Claims and equivalents thereof.

Claims: CLAIMS What is claimed is: 1. A process for preparing an improved Tiθ2 slurry directly from base Tiθ2, comprising: viscous shear processing base Tiθ2 particles having less than about 65 weight % greater than 0.6 microns, at a sohds content of above about 83% by weight, so as to achieve deagglomeration and dispersion of the slurry, while still permitting sufficient fluidity to permit incoφoration of the particles into the slurry. 2. The process of claim 1 wherein the process is carried out continuously or batchwise. 3. The process of claim 2 wherein the base Tiθ2 is rutile produced by a chloride process. 4. The process of claim 1 or claim 2 or claim 3 further comprising the step of: pohshing grind and dispersion of the viscous shear processed sluπy until the ΗO2 particles have a narrow particle size distribution as defined by a geometric standard deviation of less than about 1.64. 5. The process of claim 4 wherein the ΗO2 particles have less than about 35 weight % greater than 0.6 microns. 6. The process of claim 4 wherein the pohshing grind and dispersion is carried out with a media mill. 7. The process of claim 1 wherein viscous shear processing is carried out with an agitator tip speed of about 4 to 150 ft./sec. 8. The process of claim 7 wherein viscous shear processing is carried out with an energy input of up to about 33 kWh/T Tiθ2- 9. The process of claim 1 wherein the solids content is 83-89% by weight. 10. The process of claim 6 wherein a media nominal size ranges between about 0.3 to 2.5 mm in diameter and a media mill disc tip speed of about 1800 to 3200 ft./min. 11. A process for enhancing the optical efficiency of Tiθ2 slurries on paper and paperboards, comprising the steps of: (a) preparing base Tiθ2 particles having less than about 50 weight % greater than 0.6 microns; (b) slurrying the base Tiθ2 particles at a solids content of above about 83 to 92% by weight, at a agitator speed and agitator power so as to achieve viscous shear deagglomeration and dispersion of the slurry, while still permitting sufficient fluidity to permit incoφoration of the particles into the sluπy; (c) diluting the slurry to a point sufficient to permit slurry handling and transfer; and (d) media milling the slurry with a media nominal size range between about 0.6 to 1.6 mm and a media mill disc tip speed of about 2000 to 3000 ft/min until the Tiθ2 particles have a naπow particle size distribution as defined by a geometric standard deviation of less than about 1.64 and have less than about 30 weight % greater than 0.6 microns. 12. The process of claim 11 wherein the process is carried out continuously. 13. The process of claim 12 wherein step (c) occurs simultaneously as slurry is continuously removed from step (b). 14. A Tiθ2 slurry made by the process of claim 4 or claim 5 or claim 11 wherein the optical efficiency of the Tiθ2 is increased at least 3% when incoφorated into paper and paperboards. 15. The process of claim 1 wherein the solids content is 78 to 83% and a viscous shear processing is carried out at a shear rate of greater than 28 ft/sec. 16. The process of claim 15 wherein the process is carried out continuously or batchwise. 17. A process for preparing aqueous Tiθ2 slurries, comprising the steps of: (a) preparing base ΗO2 particles having less than about 40 weight % greater than 0.6 microns; (b) viscous shear deagglomerating and dispersing the ΗO2 particles from step (a) in water and at least one dispersant at a sohds content of above 83 to 88% by weight, at a sufficient agitator speed so as to achieve substantial incoφoration of the particles into the slurry; (c) diluting the slurry to less than about 78% solids; and (d) media milling the slurry with a media nominal size range between about 0.6 to 1.0 mm and a media mill disc tip speed of about 2500 to 2800 ft/min. until the ΗO2 particles have a naπow particle size distribution as defined by a geometric standard deviation of less than about 1.55 and have less than about 25 weight % greater than 0.6 microns.

Inventors: GOROWARA RAJEEV LOCHAN, JOHNSON ROBERT WILLIAM, OTT MICHAEL WARREN, GOROWARA, RAJEEV, LOCHAN, JOHNSON, ROBERT, WILLIAM, OTT, MICHAEL, WARREN
Applicants: DU PONT, E.I. DU PONT DE NEMOURS AND COMPANY
Application year: 1996
Main classification: C09D17
IPC codes: C09C1, C09C3, C09D17