Patent Application
20050092203
The present invention relates to processes for preparing pigment flushes, particularly flushes for ink compositions. The present invention also relates to methods for preparing ink bases and finished ink compositions.
Syntheses of many organic pigments include a coupling step in a dilute aqueous medium to produce a slurry of the pigment product, which is typically followed by filtering the slurry in a filter press to concentrate the pigment. The press cake that results is then either dried to provide a dry, particulate pigment or else is “flushed” with an organic medium such as an oil and/or resin to transfer the pigment particles from the aqueous press cake to the oil or resin phase. Flushing assists in keeping pigment particles non-agglomerated and easier to use in making inks or coatings. The flushing process requires additional time and materials over simply drying the pigment. If the pigment is used in an ink or coating composition, however, it must first be well-dispersed in an appropriate organic medium in order to achieve the desired color development and stability, and thus the flushing process is advantageous because it accomplishes the transfer without intermediate steps of drying the pigment and grinding the pigment in the organic medium to produce the pigment dispersion.
In the past, pigment flushes have usually been prepared by batch processes in which the press cake is kneaded with an organic phase such as an oil and/or a resin, for example in a sigma blade mixer or dough mixer, to flush the pigment particles from the water phase to the organic medium phase and displace the water as a separate aqueous phase. The displaced water is separated and the dispersion of the pigment in the varnish can be used as a pigment paste in preparing an ink or paint.
The batch process has many shortcomings. First, the steps of adding varnish, kneading the dough to displace the water, and pouring off the water must usually be repeated a number of times in order to obtain the optimum yield and a product with the desired low water content. This is a labor-intensive process that requires careful monitoring. Further, in order to remove residual water, the batch must be further treated, such as by heating and stripping under vacuum. For many pigments, the heat history from processing to remove the residual water may result in a color shift. Further, the process is time-consuming and inefficient. Finally, it is difficult to reduce the water content below about 3% by weight, even with the vacuum stripping.
Continuous flush processes have been suggested in the past, but those processes have also had shortcomings. Higuchi et al., U.S. Pat. No. 4,474,473 describe a process for continuously flushing pigment press cake on equipment that includes co-rotating, twin screw extruder. The process requires a press cake that has a pigment content of 35 weight percent or more. The '473 patent discloses that press cakes having a pigment content of from 15 to 35 weight percent cannot be used in the continuous process because of problems with obtaining constant flow feeding. The range of 15 to 35 weight percent, however, is the range of pigment content that is typically obtained for press cakes. While dilution of the press cake with water to form a liquid slurry of low pigment content was previously suggested, the '473 patent takes the opposite direction of increasing pigment content to 35% or more to provide a “lump cake” that is apparently suitable for constant flow feeding as a free-flowing solid. Increasing the pigment content of the manufactured press cake, however, requires a time-consuming process of shaping the press cake and drying it with circulating air until the desired water content is obtained.
An example of the methods using diluted press cake is Rouwhorst et al., U.S. Pat. No. 4,309,223. This patent discloses a process of preparing a pigment flush from a press cake using a single screw extruder. The process uses a slurry containing only about 0.5% to 10% by weight pigment. When so much water is added during the flushing process it is difficult to get a clean break or separation between the phases. In addition, more aqueous waste is produced. Finally, it is often the case that the single screw extruder does not provide a sufficient amount of mixing shear to adequately flush the press cake.
Anderson et al., U.S. Pat. No. 5,151,026, discloses an extruder apparatus for removing liquid from an aqueous mass of comminuted solids such as crumb rubber, wood pulp, and ground plastic materials that are cleansed during recycling processes. The water is squeezed out of the aqueous mass in a pinch point. The pinch point pressure results from applying a backward force by means of a reverse-threaded section of the screw immediately at the liquid extraction location. The Anderson process removes from water relatively large solid pieces that do not appear to associate or agglomerate. Unlike the Anderson process, the pigment flush process concerns transfer of fine pigment particles from aqueous press cake to an organic phase, usually including a resin, followed by separation of the two liquid phases (aqueous and organic). Two key considerations in the flush process are clean separation of the organic and aqueous phases and good dispersion of the pigment particles. The pinch point method is unsuitable for the two-phase pigment flushing process because the pinching force would interfere with the necessary phase separation between aqueous and organic phases. The pigment particles also have a tendency to agglomerate. The pinch point would thus be unsuitable for the additional reason that squeezing the pigment would cause undesirable agglomeration of the pigment particles, which would in turn impair dispersion of the pigment.
The invention provides a process for continuous production of pigment flush from conventional press cake. In a first step, at least one pigment press cake is homogenized to a fluidized mass. In a second step, the homogenized press cake is fed at a controlled rate into a twin screw extruder. The twin screw extruder may receive more than one stream of fluidized press cake. An organic medium, which may include organic components selected from solvent, varnish, oil, and/or resin, is also fed into the extruder, and the press cake and organic medium are mixed in a first zone of the extruder to wet the pigment with the organic medium, displacing water from the press cake and producing a crude pigment flush. The displaced water is removed in a second zone of the extruder. The second zone of the extruder includes a port for removing the displaced water, especially by draining the water, and preferably includes a dam that retains the pigment flush in the second zone for a time sufficient to allow most of the displaced water to be removed from the crude flush mass. The extruder preferably include a third zone that has one or more vacuum ports to draw off residual water clinging to the pigment flush.
The invention also provides a method for continuous production of an ink base or a finished ink from a pigment press cake. The method includes the steps just outlined for the process of the invention for producing a pigment flush and at least one additional step of introducing into the extruder, at some point before the pigment dispersion is discharged, preferably after the optional vacuum zone, one or more additional ink components, such as a varnish, pigmented tinting or toning compositions, solvent, and/or additives, to make an ink base or a finished ink composition.
The invention offers an advantage over previous processes in that it provides continuous processing of conventional press cakes. Press cakes are usually prepared having pigment contents of from about 15% to about 35%. Because the present invention can process press cakes as prepared, it is possible to eliminate a cumbersome preliminary evaporation step to increase pigment content of the press cake to the point at which the press cake can be flushed or a diluting step in which the press cake is reduced to a very low solids slurry for processing using the prior art methods.
The invention offers a further advantage of providing more control for a continuous flushing process, which results in increased consistency of color and other properties of the pigment dispersion.
The invention offers a still further advantage of providing a continuous process for manufacturing ink base or a finished ink product from a continuous feed of conventional press cake.
The invention provides a process in which a pigment in press cake form is flushed by transferring the pigment particles from the aqueous press cake to an organic medium, especially to an oil or resin phase. The press cake may be from the synthesis of any of a number of organic pigments. Examples of suitable press cakes include, without limitation, press cakes of diarrylide yellow pigments (e.g., Pigment Yellow 12), phthalocyanine pigments, calcium lithol red, alkali blue, barium lithol red, rhodamine yellow, rhodamine blue, and so on. Press cakes of organic pigments typically have a water content by weight of from about 12% to about 30%, although press cakes such as those of certain blue pigments may have a water content as high as 45%.
The invention further provides a step of applying shear to a press cake to produce a fluidized press cake and a step of continuously feeding the fluidized press cake into a twin screw extruder. The method of the present invention can be carried out as shown in
The feed component of the press cake feed system feeds the fluidized press cake to the extruder. Preferably, the feed component includes a pump. The pump may be any type suitable for the viscosity of the fluidized press cake. Examples of suitable pumps include, without limitation, lobe pumps, gear pumps, or other positive displacement pumps.
The feed component introduces the fluidized press cake to port 19 at the beginning of an extruder shown in the preferred example of
The extruder is a twin-screw extruder, with the screws being driven by motor 18. The screws are preferably co-rotating. At least one fluidized press cake is fed into the extruder through port 19. In one preferred embodiment, a second fluidized press cake is fed into the extruder through a port 19 or through a second port 119. A liquid organic medium, preferably including at least an oil, a resin, or resin solution, is also fed into the extruder, which may be through port 19 or through a second port 119. The liquid organic medium is sufficiently hydrophobic to allow a non-aqueous phase to form in the process. Types of organic materials that are suitable to prepare pigment are well-known in the art. If the extruder has two different fluidized press cake feeds by ports 19 and 119, the organic medium may be fed through either or through yet another separate port.
Typical kinds of resins and oils that may be used for flushing varnishes include, without limitation, alkyd resins, phenolic resins, polyesters, hydrocarbon resins, maleic resins, rosin-modified varnishes of any of these, polyamide resins, polyvinyl chloride resins, vinyl acetate resins, vinyl chloride/vinyl acetate copolymer resins, chlorinated polyolefins, polystyrene resins, acrylic resins, polyurethane resins, ketone resins, vegetable oils including linseed oil, soybean oil, neatsfood oil, coconut oil, tung oil, mineral oils, and so on. Combinations of such resins and oils may also be employed. The resin, oil, or combination thereof may be combined with a hydrophobic organic solvent or liquid, including high boiling petroleum distillates.
As mentioned, the organic medium may be introduced in the same barrel, or section, of the extruder as the fluidized press cake, whether in the same port or a different port. Alternatively, the organic medium may be introduced in another section close to the front of the extruder in the first zone, as shown in
The fluidized press cake and organic medium are mixed in one or more sections of the first zone of the extruder to wet the pigment with the organic medium, displacing water from the press cake and producing a crude pigment flush. A special screw section with a plurality of kneading disks may be used in the first zone where the flushing takes place. In one preferred embodiment of the invention, the screw profile in the first zone tapers from a deep channel used in the section or sections having a feeding port gradually to a shallow channel in a later (downstream) section or section of the first zone. The length of the first zone of the extruder in which the fluidized press cake and the organic medium are mixed is sufficiently long so that the pigment is flushed completely. The rotational speed of the screw also is a factor for efficient flushing. A preferred range for rotational speed of the screw is from about 150 to about 550 rpm, and a more preferred range for rotational speed is from about 450 to about 550 rpm.
The displaced water and the crude pigment flush continue in the extruder to the second zone of the extruder where at least a portion of the displaced water is removed. In the second zone, preferably a major portion of the displaced water is removed, more preferably at least about 80%, still more preferably at least about 90%, and even more preferably all but a residual amount of water that clings to the pigment flush is removed. Referring to
One important feature of the second zone is a dam that retains the pigment flush for a time sufficient to allow most of the displaced water to drain from the crude flush mass. The dam causes the kneaded press cake/organic medium to dwell over the port long enough to allow more of the displaced water to drain from the kneaded pigment. A portion of the mixture of press cake and organic medium is carried into the dammed section of the extruder and remains in that section until the portion works its way out of the pocket of retained material and is carried into the next section by the grabbing action of the screw.
Because more of the water is drained from the flush in a liquid phase instead of being evaporated, as compared to prior methods, the final product contains a lower concentration of salts. The dam thus improves the purity of the product.
The third zone of the extruder, which is optional but preferred, includes one or more vacuum ports 24 connected to vacuum at valves 25 to draw off residual water clinging to the pigment flush. The water is drawn off as water vapor. Suitable vacuum ports are known to be used with extruders and typically can include a section 26 containing a screw turned by motor 27 in the vacuum port to help retain the flush in the extruder. A vacuum pump is typically connected to the vacuum port to provide the reduced pressure. The profile of the screw used for the vacuum section preferably has a shallow channel, which tends to increase the efficiency of vacuum dehydration by shaping the material in a thin layer form.
The present process is particularly advantageous for preparing flushes of pigments that are heat-sensitive, including, without limitation, diarrylide and rhodamine pigments such as diarrylide yellow, rhodamine yellow, and rhodamine blue. Because the time during which the pigment is exposed to higher temperatures is minimized by the process of the invention, pigments that may discolor when exposed to heat may be made more reproducibly and without significant color degradation.
The pigment flush produced by the inventive process may be used to prepare an ink composition according to usual methods. Additional resins, oils, solvents or other components of the organic medium may be added after the vacuum port to adjust the composition of the pigment flush. Ports can be provided in an additional fourth zone for the addition of one or more further materials.
Alternatively, the pigment flush may be made into an ink base or a finished ink composition as a further step of the continuous process of the invention by introducing additional materials such as varnish, other resins, organic solvent and/or additives into the extruder at some point before the pigment flush is discharged, preferably after the vacuum zone, such as into a port on the extruder. The flushed pigment dispersion and other ink component(s) are combined in the extruder so that the output from the extruder is an ink base or ink composition. Typical resins used as ink varnishes that may be added include, without limitation, alkyd resins, polyesters, phenolic resins, rosins, cellulosics, and derivatives of these such as rosin-modified phenolics, phenolic-modified rosins, hydrocarbon-modified rosins, maleic modified rosin, fumaric modified rosins; hydrocarbon resins, vinyl resins including acrylic resins, polyvinyl chloride resins, vinyl acetate resins, polystyrene, and copolymers thereof; polyurethanes, polyamide resins, and so on. Combinations of such resins may also be employed. Suitable examples of organic solvents that may be added include, without limitation, aliphatic hydrocarbons such as petroleum distillate fractions and normal and isoparaffinic solvents with limited aromatic character. Any of the many additives known in the art that may be included in the ink compositions of the invention, so long as such additives do not significantly detract from the benefits of the present invention. Illustrative examples of these include, without limitation, pour point depressants, surfactants, wetting agents, waxes, emulsifying agents, defoamers, antioxidants, UV absorbers, dryers (e.g., for formulations containing vegetable oils), flow agents and other rheology modifiers, gloss enhancers, and anti-setting agents. When included, additives are typically included in amounts of at least about 0.001% of the ink composition, and the additives may be included in amounts of up to about 7% by weight or more of the ink composition.
The invention is illustrated by the following Examples. The Examples are merely illustrative and do not in any way limit the scope of the invention as described and claimed.
A presscake dispersion is formed by stirring a mix of pigment and presscake. This produces a fluid, well-dispersed, presscake. The flush vehicle is produced from a selection of alkyd, typical flushing vehicles and solvents.
The twin-screw extruder had the following configuration: a diameter of 40 mm and a length/diameter ratio of 58. The extruder had fourteen total barrel sections which were set up as follows: pigment feed at the beginning of the first barrel, and a flush vehicle at the third barrel. Water was drained at barrel seven and wash water was added at three points in barrel nine and ten. A vacuum was applied at barrel thirteen and barrel fourteen was provided with a location for adding a mixture of solvents and resin to give a final product mix.
On the above-described equipment, the feed rate was rated by lbs of pigment per hour (lbs/hr). In each example, the feed rate was set at 30-35 lbs/hr for one of the following pigments: Pigment Red 57:1, Pigment Yellow 12, and Pigment Blue 15:3. A flush vehicle of an alkyd, a resin and hydrocarbon solvent was added to the extruder in examples in which Pigment Yellow 12 and Pigment Red 57:1 were introduced into the extruder. During the continuous flushing of Pigment Blue 15:3, a flush vehicle of a resin and a hydrocarbon solvent was added to the extruder. In all of the examples, an additional material formed of resin and hydrocarbon solvent was added to the pigment flush produced by the process of the present invention to adjust the color of the pigment to the desired color.
The invention has been described in detail with reference to preferred embodiments thereof. It should be understood, however, that variations and modifications can be made within the spirit and scope of the invention and of the following claims.
| Number | Date | Country | |
|---|---|---|---|
| Parent | 10102422 | Mar 2002 | US |
| Child | 10956117 | Oct 2004 | US |
