AU2012220526B2 - Precipitated calcium carbonate pigment, especially for use in inkjet printing paper coatings - Google Patents

Abstract

PRECIPITATED CALCIUM CARBONATE PIGMENT, ESPECIALLY FOR USE IN INKJET PRINTING PAPER Abstract The invention relates to novel and innovative PCC pigments, able to be used in paper coating formulations to manufacture coated "multipurpose" papers, in particular for inkjet applications, whose print qualities would be identical or quite similar to high resolution commercial papers, while maintaining a reduced paper manufacturing and production cost. Said pigments are obtained by a carbonation process using a reduced flow rate of C0 2/air, which leads to porous agglomerates of PCC of a very specific structure and unique properties, followed by an upconcentration step leading to substantially the same agglomerates but with a higher, appropriate, solids content. (67002251 ):KZA

Description

S&F Ref: 824759D1 AUSTRALIA PATENTS ACT 1990 COMPLETE SPECIFICATION FOR A STANDARD PATENT Name and Address Omya Development AG, of Baslerstrasse 42, CH-4665, of Applicant : Oftringen, Switzerland Actual Inventor(s): Michael Pohl Michael Kaessberger Address for Service: Spruson & Ferguson St Martins Tower Level 35 31 Market Street Sydney NSW 2000 (CCN 3710000177) Invention Title: Precipitated calcium carbonate pigment, especially for use in inkjet printing paper coatings The following statement is a full description of this invention, including the best method of performing it known to me/us: 5845c(6706237_1) Precipitated calcium carbonate pigment, especially for use In inkjet printing paper coatings Technical Field of the Invention The present invention relates to novel mineral pigments of the precipitated 5 calcium carbonate species (PCC). More specifically, the invention relates to novel and innovative PCC pigments, able to be used in a paper coating formulations to manufacture coated "multipurpose" papers, in particular for inkjet applications, whose print qualities would be identical or quite similar to high resolution 10 commercial papers, while maintaining a reduced production cost. Multipurpose papers are typical used as paper for a variety of printing types, and include uses as black and white copy, laser printing and fax paper. The invention additionally relates to the production of said novel mineral 15 pigments of the PCC species in slurry form, present in a solids content appropriate for inkjet paper coating on a low cost paper coater, such as the Metered Size Press (MSP). Technical Problems 20 There exists a demand for coated multipurpose papers, and in particular for papers suitable for inkjet applications, which give an improved print quality without a corresponding increase in production cost. Currently available multipurpose office papers are often associated with an unsatisfactory inkjet print quality.

2 One of the main hurdles to achieve an increase in print quality is to increase the optical density of the ink applied to the paper surface, in particular following full colour spectrum dye ink application. Inkjet printers form images by applying a series of ink dots on the paper 5 surface. The dye inks used in inkjet printing are generally anionic and in a low solids formulation that is naturally very mobile. Good print quality is only obtained if the ink dye remains on the paper surface as the Ink solvent penetrates into the paper, leaving a uniform circular dot at the point of application. 10 It is known that a charge difference between adsorbent and adsorbate, respectively the paper surface and the dye molecules, is generally used to prornote dye adsorption. Hence, one solution to increase optical density lies in increasing the number of cationic sites near the paper surface. If the paper surface is 15 coated, the number of cations present near the surface can be increased by adding cationic additives to the coating formulation. However, adding cationic additives in order to obtain a given optical density adds significantly to the final paper cost. Increasing the fraction of cationic additive retained in a thin layer near the 20 paper surface, characterised by the coating holdout, is a second solution to increase optical density. Higher coating holdout can be achieved through the use of a narrower coating particle size distribution, which is a technically difficult and expensive solution. If PCC is present in the coating formulation, the Inherent adsorptive 25 properties of PCC particles towards ink dyes can offer another alternative to reduce the quantity of cationic additives necessary to ensure a given optical density. For an equal quantity of this pigment, decreasing the primary PCC particle size increases the positively-charged pigment surface area available to interact with and bind ink dye. This promotes ink 30 dye adsorption on the PCC particles near the site of ink application, which leads to an increase in optical density.

3 Segregation of large dye molecules on the paper surface is also aided by surface size exclusion and a high pore volume coating, allowing the passage of solvent into the base paper while retaining the dye molecules on the surface. This suggests the need for a porous coating formulation; 5 one theoretical solution is therefore to introduce aggregates/agglomerates, such as possibly aggregated pigments, in the coating formulation, with a carefully controlled pore size distribution and capillarity. However, as the skilled man knows, such a theoretical solution is quite difficult to specifically engineer; in the specifically related domain, USP 5,750,086 10 (discussed herebelow) produces finely divided PCC, along with numerous other patents, but not porous products or aggregates/agglomerates. A second challenge in increasing print quality is to reduce the bleeding phenomenon observed following ink application to the paper surface. Ink dye bleeding of one colour into another adjacent colour occurs as a result 15 of latent ink dye binding to and drying on the paper surface, and is partly due to delayed ink solvent absorption into the base paper, which serves to bring the ink dye in contact with the surface for rapid binding. Bleeding has as a consequence that printed images are distorted and appear less sharp. 20 Sim'larly, feathering also results in blurred images and occurs when deposited ink follows the contours of the paper. As with ink bleeding, it is rectified by rapid ink drying, preferring dye absorption to adsorption when using porous media. As the above implies, there is a need to balance and control ink 25 adsorption onto the pigment surface as opposed to absorption into the void volume of pigment pores, since high absorption leads to decreased bleeding and feathering, but with an accompanying decrease in optical density, whereas high adsorption leads to improved optical density, while increasing bleeding and feathering. 30 A third challenge in obtaining a high print quality is to decrease the print unevenness in the final paper product. Print unevenness is the result of the inhomogeneous penetration of the ink-binding elements (cationic additive or coating pigment) of the coating formulation into the base paper.

4 Coating formulations having a low solids content present an increased risk of solvent entraining the ink-binding elements away from the paper surface during two phenomena: as the formulation solvent passes into the base paper following paper coating and during the later movement of the 5 solvent to the paper surface during drying. Such surface unevenness can be limited by using a slurry presenting a high solids content, which limits the quantity of solvent passing into and out of the base paper. However, such a high solids content is incompatible with some of the above objectives or theoretical solutions. 10 When the coating formulation includes a pigment, use of a high solids pigment slurry is desirable, since it is known that the starch binder and other additives generally added to multipurpose paper coating formulations are in the form of a low solids solution. If the solids content of the coating slurry is not maximised, the dilution upon addition of the binder 15 and other additives will be too significant. The above-listed constraints suggest the need for fixation of dyes on sites distributed homogeneously over the paper surface. It is clearly important that the coating formulation be high in solids, however as is known in the art, upconcentration of aggregate-containing slurries often lead to a loss of 20 important pore volume. As such, the theoretical solutions to the above-listed problems were not recognized as able to solve the defined problems, and said list to the contrary suggests that they must be delicately weighted and that extremely difficult compromises, if not impossible ones, would have to be 25 found; this was nevertheless one of the objectives of this invention, and it is the merit of the invention to have ultimately reached a global solution. A second concern of the man skilled in the art is to achieve this balance employing a cost-efficient solution. Any skilled man will appreciate that such a requisite is always a factor highly complicating the definition of a 30 technical solution, especially in the considered domain. Known multipurpose inkjet papers are characterized by surface sized or slightly pigmented qualities, and generally surface sized or coated on a cost--efficient on-line coater, such as the MSP or Film Press, allowing a high coating application speed and coating a lower coat weight than their off-line-counterparts. Speciality grade inkjet papers are characterized by a superior high 5 resolution print quality relative to multipurpose papers. Such papers are generally coated at a high coat weight with formulations including special high quality binders and additives via more costly coating techniques, employing for example VaribarTM, airknife, curtain or blade off-line coaters. Due to raw material cost, production rate, coating weight and composition, 10 and coater type, the cost of known multipurpose inkjet papers is inferior to the cost of high resolution matt inkjet papers by an order of magnitude which is roughly 6 to 20 times. Hence, the man skilled in the art recognises the benefits of being able to obtain a high quality paper coating using a low cost coating solution. 15 As mentioned above, lowering the cationic additive demand of the coating formulation, relative to current specialty pigments for inkjet, is also desirable for cost savings. Further, it is of interest to reduce the quantity of binder needed, since this component represents an expensive part of the coating composition and 20 its presence on the paper surface decreases the active area available to interact with ink. One option is to use aggregates/agglomerates presenting appropriately small pores, in which case only sufficient binder to adsorb onto the surface of the aggregates/agglomerates need be added, since the binder cannot attain the surface of the primary particles exposed within 25 the pores. However, as indicated above, this proposal is uniquely theoretical. As regards the paper coating process, cost reduction can be attained by promoting a more rapid paper drying step following coating. More rapid drying translates to a higher paper machine speed and increased 30 productivity since the risk of wet coating material deposits on the paper making machine is reduce. More rapid drying is possible through the use of a maximum solids content coating formulation.

6 A high solids coating formulation also reduces the cost associated with transporting said coating formulation from the pigment manufacturer to the paper mill, respectively coating plant. A final concern of the man skilled in the art is to ensure an equal or 5 improved runnability (number of sheets produced without failure) on coating machines. It is known that coaters such as the MSP or the Film Press demonstrate an improved runnability when using an increased coating slurry solids content, while maintaining a low (500 to 1500 mPAs) slurry viscosity. 10 As the skilled man will appreciate, these are additional technical problems to be solved. The skilled man will also recognise that many of said problems call for conflicting or antagonist solutions, which lead to severe. problems if not properly balanced; this was the difficult problem solved by this invention. 15 As mentioned above, the overall technical problem, and technical challenge, is to develop a novel class of PCC pigments structured to be used in a paper coating process to manufacture a paper which is "technically speaking" a coated multipurpose paper, in particular for inkjet applications, but whose print properties would be improved relative to 20 other coated papers of the same grade, while maintaining a low production cost. Last but not least, the solution must of course fit to as many types of printers as possible, if not all, adding another complexity to resolve. Any skilled person will recognize both the commercial need for such an 25 innovative technology, the paramount technical challenge it represents, and the considerable technical, commercial and financial advance it would bring.

7 Prior Art Pigment options for use in multipurpose inkjet paper coatings currently on the market include specialty PCC inkjet pigments, such as those of EP 0 815 174, or expensive fumed or precipitated silica. 5 Besides its considerable cost as a coating material, it is know that silica is generally limited to low solids formulations, whose use considerably reduces the coating line speed, further increasing to overall coating cost. The man skilled in the art is therefore motivated to seek lower cost coating alternatives available in higher solids formulations. 10 According to EP 0 815 174, which relates to coating a PCC, an organophosphonate compound, such as an amine-containing phosphoric acid or ethanol amine bis-(methylenephosphonic acid), is added to a PCC slurry in a quantity corresponding to 0.4 to 0.85 % by weight relative to the weight of PCC. Said slurry is then heat aged over a sufficient time period 15 (1 to 10 hours at a terriperature exceeding 750C, or 2 to 5 hours at 80 to 850 C) to impart a specific surface area exceeding 60 m 2 /g. Alum or other inorganic, aluminium-containing compounds can be co precipitated during the synthesis of PCC. In Example 1 of this patent, addition of aluminium sulphate octadecahydrate is performed just prior to 20 the carbon dioxide introduction. Optionally, up to 10% by weight of hydrated aluminium sulphate can also be introduced. The heat ageing and/or milling of the PCC are regarded as critical in order to reach an appropriate level of ink binding to the PCC. To the contrary, as will be seen below, neither expensive, time-consuming 25 heat ageing nor milling are required in the present invention; indeed, in the present invention, heat ageing even results in an inadmissible loss of PCC surface area. Furthermore, the solids content of the slurry disclosed in the examples was low, near to 20%.

8 EP 1 246 729 is presented as an improvement over the above mentioned patent, and the product of this patent is said to feature a surface area of 60 to 65 m 2 /g, preferably 80 to 90 m 2 /g, and generally no more than 95 to 100 m 2 /g. That surface area is said to be obtained by heat ageing in the 5 presence of an organophosphonate compound, as indicated above. The PCC particles are said to be individually spherical in shape, with a diameter of the order of 0.02 to 0.03 tm. This high specific surface area PCC presenting a narrow particle size is obtained in a low solids (25%) slurry. 10 The alleged innovation in EP 1 246 729 comes from the combination of a finely divided PCC, presenting a surface area exceeding 60 m 2 /g, in a major proportion, and a minor proportion of a gel-type silica, along with a binder. The resulting composition can be blade coated, or less preferably coated 15 using an air knife and Meyer bar. The required presence of expensive silica and the low solids content of the slurry represent major drawbacks. USIP 5,750,086 describes a process for manufacturing ultrafine particles of colloidal calcium carbonate (PCC), in which magnesium sulphate is added 20 to a 3 to 14% by weight aqueous suspension of calcium hydroxide, followed by carbonation with the introduction of zinc sulphate alone or together with sulphuric acid. In the examples, the introduced metal salts solutions or sulphuric acid have a concentration of 10 % by weight. 25 The process is said to lead to chain-structured ultrafine particles of colloidal calcium carbonate having an average diameter of 0.01 pam of smaller, an average length of 0.05 ptm or smaller, and a BET specific surface area of 70 ml/g or greater.

9 The obtained ultrafine particles are said to "show lower affinity of aggregation". Indeed, the applicant primarily targets applications requiring non-aggregated fillers, such as plastic applications wherein the dispersibility of the end product is important. The present invention, by 5 contrast, targets an aggregated product for inkjet paper applications. The specific gas flow rate of 120 litres per minute per kilogram calcium hydroxide as indicated in the USP 5,750,086 examples, however, is quite significantly higher compared to the process conditions of the present invention, as will be seen herebelow. 10 Indeed, it was found according to the present invention and contrary to the teaching of the prior art and common knowledge, that by reducing the specific gas flow rate to below about 30 or below about 20 litres per minute per kilogram calcium hydroxide during precipitation, one obtains. not the discrete pigment described in USP 5,750,086, but rather coarse 15 mechanically stable porous spherical agglomerates/aggregates consisting of said colloidal calcium carbonate. As mentioned above, while it was possible to theorize regarding the potential interest of porous PCC with an appropriate pore size distribution, possibly obtained via an agglomeration process, this remained theoretical 20 until the above surprising innovation. It has also to be noted that there is no indication whatsoever in the prior art or in the common knowledge that altering one parameter among dozens in the PCC preparation process, would lead to porous agglomerates. There is even less indication that those agglomerates would be stable. There is still less indication that the 25 parameter to be modified was precisely said flow rate. The process of USP 5,750,086 was reproduced with the above mentioned, decisive, modification to the gas flow rate and the obtained product properties are shown in Table 2, Example 1. As can be seen in Table 2, the product obtained by altering the teaching of 30 USP 5,750,086 according to the invention is, quite surprisingly, not the discrete pigment described in USP 5,750,086, but rather coarse agglomerates.

10 However, a problem with the slurry produced in Examples 1 is the low solids content which is useful in some applications in the considered industries, but is not suitable for multipurpose paper coating on coaters such as the MSP. This represented an additional problem to be solved, as will be seen herebelow. 5 This surprising result is one of the key starting points of the present invention. Additional Prior Art: Japanese patent 2004-299302 teaches an inkjet record form featuring an "ink acceptance layer", the layer comprising calcium carbonate as a principal pigment, which leads to improved feathering and bleeding. There is no specific indication as to the properties or structure of the calcium io carbonate to be used. This document instead focuses on the use of a dispersant and the cationic charge density of the dispersant. EP 0 761 782, Japanese patent 10-265 725 and Japanese patent 2004-197 055 each describe improved inks for inkjet printing, namely used to improve optical density, bleeding and/or feathering upon printing. None of these patents give a specific indication as to the coating pigment to be used 15 when preparing the paper sheet. US 2003/0227 531 Al discloses a paper coating of a polyvalent metal salt, such as calcium, magnesium or aluminium onto one surface of the base paper, in order to improve feathering and bleeding. Summary of the Invention 20 According to a first aspect of the present invention, there is provided process for providing PCC useful for ink-jet printing applications, - of the type according to which a calcium hydroxide slurry is first prepared by mixing quicklime (CaO) with water in a stirring reactor or tank ("slake"), the calcium hydroxide slurry is then screened, such as on a 100 pm screen, to remove any residual impurities and/or non-reactive 25 unburnt lime, the screened slurry is then directed towards a stainless steel reactor equipped with an agitator; the temperature is adjusted, generally to between 10 and 70*C, and subsequently the slurry is directed towards a carbonation reactor or tank, wherein carbon dioxide-containing gas is bubbled through the slurry, the slurry exits the carbonation tank when appropriate in view of 10a conductivity and pH, generally when the conductivity reaches a minimum and the pH drops below 8, coarse particles are removed on a screen, such as a 45 pm screen, such that the slurry contains only the ultrafine PCC agglomerates of the invention, - wherein the implementation of process steps comprises the following: 5 A First steps, production of the PCC: Al - the carbonation step is performed at a carbonation gas flow rate of below 30 litres per minute at standard temperature and pressure per kilogram calcium hydroxide during precipitation; A2 1 o - the slurry of calcium hydroxide leaving the stainless steel reactor after the separation of the residual impurities and/or non-reactive unburnt lime is treated by a combination of magnesium sulphate and Group 11 and/or Group Ill metal sulphates - most preferably in the presence of an acid - the acid being most preferably sulphuric acid is - until stable, porous agglomerates/aggregates are obtained at a concentration of 5 to 25% solids, preferably 15 to 20% solids ("precursor"); A3 - the slurry of calcium hydroxide is first prepared by mixing quicklime with water in a stirring reactor or tank ("slake") in a weight ratio of CaO: water between 1:3 and 1:20, preferably between 20 1:5 and 1:12, most preferably between 1:7 and 1:10; A4 - the temperature is preferably adjusted to between 15 and 500C, most preferably to between 15 and 30*C, before the slurry is directed towards the carbonation reactor or tank. According to a second aspect of the present invention, there is provided stable, porous 25 aggregates/agglomerates of PCC wherein they have been obtained according to the first aspect. According to a third aspect of the present invention, there is provided stable, porous aggregates/agglomerates of PCC obtained by the process of the first aspect wherein they feature the following properties: -a specific surface area of 30 to 100 m 2 /g, preferably from 50 to 80 m 2 /g, and/or 30 - a mean aggregate diameter of 1 to 5 pm, with an average diameter of 2 pm, and/or -a fraction of fines below 2 pm of less than 20%, preferably less than 15% (as measured on a Helos sympatec), and/or 10b -a primary particle size of the acicular particles of 20 nm to 50 nm with an aspect ratio between 1:2 and 1:10 and/or -a solids content, by weight from 5 to 25%, preferably 15 to 20% at the end of Steps A, and a solids content of 25 to 60%, preferably 35 to 50% solids, in particular 39 to 40% solids at the end s of Steps B. According to a fourth aspect of the present invention, there is provided pigments, wherein they comprise stable, porous PCC aggregates/agglomerates according to second or third aspects. According to a fifth aspect of the present invention, there is provided pigments or PCC slurries wherein they comprise stable, porous PCC aggregates/agglomerates according to the second or io third aspects. According to a sixth aspect of the present invention, there is provided coating formulations for the paper making industry wherein they comprise aggregates/agglomerates of PCC, pigments and/or slurries according to any one of the second to fifth aspects. According to a seventh aspect of the present invention, there is provided applications of the coating 15 formulations according to the sixth aspect to the coating of inkjet paper. According to an eighth aspect of the present invention, there is provided applications of the coating formulations according to the sixth aspect to the coating of "multipurpose" inkjet paper or of specialty, high quality, paper. According to a ninth aspect of the present invention, there is provided inkjet paper, namely 20 "multipurpose" inkjet paper or specialty, high quality, paper, wherein it is coated by at least a coating composition according to sixth aspect. The objectives of the invention can only be fully reached by the combination of the specific process for preparing porous, stable, agglomerates of PCC, using a decisively reduced gas flow rate for the carbonation step, and of the selected upconcentration steps to produce a high solids PCC slurry 25 suitable for inkjet paper coating applications.

11 It is briefly reminded here that PCC is generally obtained in the prior art via the following steps: a calcium hydroxide slurry at about 13% solids is first prepared by slaking; calcium oxide (also referred to as burnt lime or quicklime) is mixed with water in a stirring reactor or tank. Said calcium 5 hydroxide slurry is then screened, such as on a 100 jtm screen, to remove any residual impurities and/or non-reactive unburnt lime, and then directed towards a stainless steel reactor equipped with an agitator. The temperature is adjusted, generally to around 20*C, and subsequently the sluny is directed towards the carbonation reactor or tank where carbon 10 dioxide is bubbled through, optionally with air, precipitating PCC. The PCC sluny leaves the carbonation tank when appropriate in view of an appropriate drop in pH and/or conductivity. The above is known to the skilled man, and the following patents are. incorporated herein by reference: EP 0 768 344, WO 98/52870 15 (PC T/US98/09019) and WO 99/51691 (PCT/US99/07233). Generally speaking, the present invention resides in a series of first steps (Steps A) leading to the production of a low solids PCC slurry, comprising essentially porous, stable, agglomerates/aggregates of PCC particles, possibly followed by the upconcentration of said slurry (Steps B) without 20 loss of said agglomerates/aggregates. Steps A of the invention relate to a process for the preparation of porous, stable agglomerates/aggregates of PCC as a low solids slurry, and the so obtained PCC product, which is a new industrial product. The invention therefore covers a new process for producing a PCC slurry 25 via the carbonation route, characterized in that the carbonation step is conducted with a carbonation gas flow rate reduced to below 30 litres per minute per kilogram calcium hydroxide during precipitation (Steps A). The present invention also covers a new process for producing a PCC slurry via the carbonation route, additionally characterized in that the 30 production of PCC as described in the above paragraph is conducted in the presence of magnesium sulphate, in combination with one or more 12 group II or Ill metal sulphates, said metal sulphate(s) being in particular aluminium based and/or zinc based, preferably aluminium based or zinc based. These steps are based on those described in USP 5,750,086, however with the much lower carbonation gas flow rate as mentioned 5 above. The surprising result is that the pigment obtained is not a non agglomerating, ultrafine particular, discrete product, but rather coarse (1 to 5 pra range) porous and stable agglomerates/aggregates. The produced agglomerates/aggregates are surprisingly so stable that 10 they are substantially maintained in agglomerated/aggregated form during a subsequent "upconcentration" step, and astonishingly the finally produced PCC agglomerates/aggregates impart improved print properties when incorporated in inkjet paper coatings, as compared to the print quality of other market papers of the same grade. 15 In most preferred embodiments, Steps A of the present invention are additionally characterized by the use of the inventive combination of magnesium sulphate and aluminium sulphate, or magnesium sulphate and zinc sulphate. In less preferred embodiments, the process of the invention uses the 20 combination of magnesium sulphate and zinc sulphate, to which is added aluminium sulphate, or the combination of magnesium sulphate and aluminium sulphate, to which is added zinc sulphate. Further, a less preferred embodiment includes the use of magnesium sulphate and one or more sulphates of group 11 and/or IlIl metals. 25 The invention additionally lies in the combination of the PCC production process (Steps A), with subsequent particular upconcentration (devatering/redispersion) steps in the presence of a dispersant (Steps B). It Is entirely innovative to use the combination: PCC production (Steps A) with the upconcentration process (Steps B) for this type of inkjet 30 application.

13 The final product is, quite surprisingly, a PCC in the form of stable agglomerates/aggregates having an average diameter in the Lm range, namely between 1 and 5 ltm, forming a PCC pigment which, when used in a standard coating formulation, leads to a superior print qualities at 5 reduced cost. The invention also covers novel PCC pigments per se, as new industrial products, in the form of stable agglomerates/aggregates in the Lm range, namely between 1 and 5 tm, as obtained at the end of Steps A or at the end of Steps A and B. This is entirely different from the commercial 10 technologies and prior patents. The invention also covers the novel pigment slurries containing said pigments as new industrial products, namely the low solids slurry obtained at the end of Steps A and the high solids slurry obtained at the end of Steps A and B. 15 The invention additionally covers novel coating formulations for coating ink jet paper containing said pigments or pigment slurries The invention also covers coated ink jet papers, coated with such novel coating formulations. 20- Detailed description of the invention The invention relates to: - a process for providing PCC useful for ink-jet printing applications, - of the type according to which a calcium hydroxide slurry is first prepared by mixing quicklime (CaO) with water in a stirring reactor or tank 25 ("slake"). The calcium hydroxide slurry is then screened, such as on a 100 tm screen, to remove any residual impurities and/or non-reactive unburnt lime. The screened slurry is then directed towards a stainless steel reactor 14 equipped with an agitator; the temperature is adjusted, generally to between 10 and 70*C, and subsequently the slurry is directed towards a carbonation reactor or tank, wherein carbon dioxide-containing gas is bubbled through the slurry. The slurry exits the carbonation tank when 5 appropriate in view of conductivity and pH, generally when the conductivity reaches a minimum and the pH drops below 8. Coarse particles are removed on a screen, such as a 45 pm screen, such that the slurry contains only the ultrafine PCC agglomerates of the invention, - characterized by the implementation of process steps comprising a 10 series of first steps, relating to the production of the PCC in which: Al In a PCC production process as described above, the carbonation step is performed at a carbonation gas flow rate of below about 30 litres per minute at standard temperature and pressure per kilogram calcium hydroxide during precipitation. 15 The invention also relates to a process as defined above characterized in that: A2 In a PCC production process as described above under Al, the slurry of calcium hydroxide leaving said stainless steel reactor after said separation of said residual impurities and/or non-reactive unburnt lime is 20 treated by a combination of magnesium sulphate and Group lI and/or Group Ill metal sulphates, most preferably in the presence of an acid, said acid being most preferably sulphuric acid, until stable, porous agglomerates/aggregates are obtained at a concentration of 5 to 25% solids, preferably 15 to 20% solids ("precursor"). 25 The invention also relates to a process as defined above characterized in that: A3 In a PCC production process as described above under Al or A2, the 3lurry of calcium hydroxide is first prepared by mixing quicklime with water in a stirring reactor or tank ("slake") in a weight ratio of CaO:water 15 between 1:3 and 1:20, preferably between 1:5 and 1:12, most preferably between 1:7 and 1:10. The invention also relates to a process as defined above characterized in that: 5 A4 In a PCC production process as described above under Al, A2 or A3, the temperature is preferably adjusted to between 15 and 500C, most preferably to between 15 and 300C, before the slurry is directed towards the carbonation reactor or tank. These steps are schematically shown on attached Fig. 1. On said figure, 10 the references have the following meanings: 1: Water II: Quicklime Ill: Reactor, such as a stirred reactor or tank IV: Screen, such as a 100 Im screen 15 V: Residual Impurities and/or Non-reactive Unburnt Lime VI: Calcium Hydroxide Slurry VII: Reactor, such as a carbonation reactor or tank VIII: Magnesium Sulphate Solution IX: Group Il and/or Group III Metal Sulphate(s) 20 X: Optionally acid, such as sulphuric acid XI: Carbon Dioxide-Containing Gas XII: Screen, such as a 45 pm screen XIII: Coarse Particles 16 XIV: Invention PCC (in a porous, agglomerated form) Slurry Steps A are followed by the upconcentration of the PCC produced during Steps A, in the presence of a cationic, anionic or combination dispersant, under sufficiently gentle or mild conditions for the 5 aggregates/agglomerates not to be substantially destroyed, until a concentration of 25 to 60%, preferably in the range 35 to 50%, most preferably 39 to 40% solids by weight is reached. The amount of dispersant added is controlled so that the PCC agglomerates/aggregates of the precursor are just coated, this quantity corresponding that added 10 prior to a slurry viscosity increase. If the upconcentration leads to a filter cake, such as following upconcentration performed using a pressurized filter, or a centrifuge, or by vacuum filtration, the concentrated material is optionally washed with water and a redispersion is performed until the final material substantially 15 consists of stable, porous agglomerates/aggregates identical with or very similar to those obtained in Steps A. The upconcentration can be performed in a thermal evaporation step with the final material substantially remaining in the form of the stable, porous 20 agglomerates/aggregates obtained in Steps A. The upconcentration of part or all of the precursor may lead to a dry product, and in such a case, the dry product is redispersed until the final material substantially consists of stable, porous agglomerates/aggregates identical with or very similar to those obtained in Steps A. 25 Fig. 2 represents a dewatering process in a centrifuge, with: 1: PCC slurry from Steps A II: Dewatering centrifuge Ill: Filtrate IV: Filter Cake 17 V: Dispersing Unit VI: Solution of a Dispersing Aid (such as a Sodium Salt of Polyacrylic Acid or a Sodium Citrate/Carboxy Methyl Cellulose mixture) VII: Upconcentrated PCC Slurry 5 Fig. 3 represents an alternate dewatering process in a centrifuge, with: 1: PCC slurry from Steps A II: Dewatering centrifuge III: Filtrate IV: Filter Cake 10 V: Dispersing Unit VI: Solution of a Dispersing Aid (such as a Sodium Salt of Polyacrylic Acid or a Sodium Citrate/Carboxy Methyl Cellulose mixture) VII: Upconcentrated PCC Slurry Fig 4 represents a thermal upconcentration step under vacuum, with: 15 1: PCC slurry from Steps A II: Thermal Evaporator Ill: Upconcentrated PCC Slurry Fig 5 represents a thermal upconcentration on a heating plate, with: I: PCC slurry from Steps A 20 11: Heating Plate Ill: Solution of a Dispersing Aid (such as a Cationic Copolymer/Hydroxy Ethyl Cellulose) 18 IV: Upconcentrated PCC Slurry The following are optional and/or preferred features In Steps A, to be taken alone or in combination. The carbonation gas flow rate is preferably selected in the range of 1 to 5 30, preferably 10 to 20, most preferably around 19.7 litres per minute at standard temperature and pressure per kilogram calcium hydroxide during precipitation. Said carbonation gas is C02 or a mixture of C02 and one or more other gases, such as air and/or nitrogen. The slurry of calcium hydroxide is most preferably treated by a 10 combination of magnesium sulphate and aluminium sulphate, or a combination of magnesium sulphate and zinc sulphate. According to less preferred options, zinc sulphate can be added to the combination of magnesium sulphate and aluminium sulphate, or aluminium sulphate can be added to the combination of magnesium 15 sulphate and zinc sulphate. The addition of magnesium sulphate is most preferably performed before carbonation. Magnesium sulphate can be added, in a less preferred option, either before the addition of other sulphates or during that addition. In a second, less preferred option, magnesium sulphate can be added 20 during carbonation along with aluminium and/or zinc sulphate. As a least preferred option of the invention, magnesium sulphate can be added during carbonation or just at the beginning of carbonation. The addition of aluminium sulphate and/or zinc sulphate most preferably takes place over the period of carbonation. 25 The addition of the acid, namely sulphuric acid, most preferably in the form of a 10% by weight solution of sulphuric acid, takes place preferably at the beginning of carbonation. Still more preferably , however, the addition of sulphuric acid takes place simultaneously with the addition of aluminium sulphate or zinc sulphate.

191 Without being bound by any theory, the applicant is of the opinion that in the present invention, the presence, as described below, of sulphuric acid is necessary for achieving proper results. In all the above options, sulphates of Group 11 and/or IlIl can be added in 5 addition to aluminium sulphate and/or zinc sulphate, or as a substitute for aluminium sulphate and/or zinc sulphate. The temperature in the carbonation tank is observed to rise up to between 40 and 800C, preferably up to between 50 and 600C, most preferably up to between 56 and 57*C. 10 Removal of residual impurities and/or non-reactive unburnt lime takes place on a 45 ptm mesh screen when the Brookfield viscosity of the material exiting from the carbonation tank is sufficiently low, namely less than 100 mPas at 100 rpm. 15 The final slurry product substantially consists of stable, porous agglomerates/aggregates. The following are optional and/or preferred features in Steps B, to be taken alone or in combination. By "deagglomeration/deaggregation" it is meant that the 20 agglomerates/aggregates obtained at the end of Steps A by the specific process of the invention are disintegrated, the disintegrated product being ultrafine PCC of the same kind (with the exception of the contained or deposited metal salts) as the one obtained in USP '086. By "gentle or mild conditions" it is meant that the 25 deagglomeration/deaggregation of the agglomerates/aggregates is kept to a minimum, so that said agglomerates/aggregates are not "substantially destroyed". More precisely, this means that it is most preferred that during the upconcentration steps, the increase of surface area is limited to less than 50%, preferably less than 25%, and/or the increase in the fraction of 30 particles below 2 pm is limited to less than 50%, preferably less than 25%, most preferably less than 10%, and/or the decrease of the mean 20 aggregate diameter is limited to less than 50%, preferably less than 20%, most preferably less than 15%, as measured according to the means described below. SEM images before and after upconcentration are substantially identical 5 which means that the existing agglomerates/aggregates (as obtained in Step A "precursor") are not noticeably altered during upconcentration. The upconcentration step can be performed in the form of any thermal or mechanical separation technology for solid/liquid suspensions provided the aggregates/agglomerates obtained in Steps A ("precursor") are 10 sufficiently stable and are not "substantially destroyed" by said technology. During the upconcentration process, a common dispersant is added in the customary proportions, in order to increase the slurry solids content without overly increasing the viscosity of the slurry. Said dispersant may be cationic, anionic or a combination thereof. The amount of dispersant 15 added is controlled so that the PCC agglomerates/aggregates of the precursor are just coated, this quantity corresponding that added prior to a slury viscosity increase. For example, approximately 5 to 9% w/w of a 40% solution of a sodium salt of polyacrylic acid relative to dry calcium carbonate is added to the slurry containing the pigment of the invention, 20 corresponding to approximately 1.5 to 3.5% weight dry polyacrylic acid on dry calcium carbonate. Most preferably the upconcentration is performed in a centrifuge, or a pressurized filter, or vacuum filtration or by thermal upconcentration, in the presence of a cationic, anionic or combination dispersant. The final slurry 25 concentration is about 39 to 40% solids by weight. A degree of destruction of the agglomerates/aggregates was expected. Such pigment aggregates/agglomerates are often held together by relatively weak Van der Waals or electrostatic attractive forces, which are 30 surpassed by the centrifugal and/or shear forces created within the equipment associated, with commercial upconcentration, namely within the centrifuge, fast-rotating decanter or high pressure filter press. The result that no noticeable destruction of aggregates/agglomerates is observed 21 while fully achieving the degree of required upconcentration is therefore entirely not obvious. The present invention covers the stable, porous aggregates/agglomerates of PCC produced at the end of Steps A alone ("precursor"), and the final 5 stable, porous aggregates/agglomerates of PCC, as obtained by' the above processes, at the end of Steps A in combination with Steps B, said PC featuring quite innovative properties which in turn make it of particular value for ink-jet applications. 10 The stable, porous aggregates/agglomerates of PCC obtained at the end of Steps A as well as those obtained after the upconcentration Steps B can be characterized by a selection of the following: a specific surface area of 30 to 100 m 2 /g, preferably 50 to 80 m 2 /g, and/or a mean aggregate diameter of 1 to 5 jim, with an average diameter of 2 Rm, and/or a fraction 15 of fins below 2 lam of less than 20%, preferably of less than 15%, and/or a primary acicular particle size of 20 to 50 nm, with an aspect ratio between 1:2 and 1:10, and/or a solids content, by weight from 5 to 25%, preferably 15 to 20% at the end of Steps A, and a solids content of 25 to 60%, preferably 35 to 50% solids, in particular 39 to 40% solids at the end 20 of Steps B. The Iinal slurry concentration may be partially or wholly obtained by the addition of one or more additional pigments or pigment slurries during Steps B. 25 The invention covers the novel pigments characterized in that they comprise stable, porous PCC aggregates/agglomerates as described herein, and novel pigment or PCC slurries characterized in that they comprise stable, porous PCC aggregates/agglomerates as described herein. 30 The invention also covers novel pigments and PCC slurries characterized in that their solids concentration is, by weight, from 5 to 25%, preferably 15 to 20% solids at the end of Steps A, and from 25 to 60%, preferably 35 to 50%, in particular 39 to 40% solids at the end of Steps B.

22 According to a preferred embodiment, the functional pigment or pigment slurry with a high surface area and integrated cations, is incorporated in the coating formulation in a way known to the skilled man, in order to increase namely the optical density upon printing without an increase in 5 bleeding or feathering: this is one of the major achievements of the invention. The invention therefore also covers novel coating formulations for the paper making industry characterized in that they comprise novel aggregates/agglomerates of PCC, novel pigments and/or novel slurries 10 described herein. The invention also covers coating formulations as described herein characterized in that the PCC slurry which it contains features the following properties: a solids content of 25 to 60%, preferably 35 to 50%, in particular around 39 to 40% weight, and/or a high surface area PCC, 15 nan-ely featuring a specific surface area of 30 to 100 m 2 /g, preferably 50 to 80 m 2 /g. The invention also covers the applications of the coating formulations according to any of claims 19 or 20 relating to the coating of inkjet paper, namely to the coating of "multipurpose" inkjet paper or of specialty, high 20 quality, paper. To sum up, the most preferred invention and best mode as of today relies on the selection of a decisively reduced carbonation gas flow rate during the precipitation of the PCC, the specific combination of cations introduced in the PCC crystal lattice during PCC synthesis, the use of a high solids 25 coating slurry, upconcentrated after the synthesis with dispersant to 25 to 60%, preferably 35 to 50%, in particular around 39 to 40 % solids by weight, in particular for use in paper coatings to be coated on MSP or Film Press, the use a high surface area PCC in the range of 30 to 100 m 2 /g, preferably 50 to 80 m 2 /g, at the end of Steps A and/or at the end of Steps 30 B, most preferably at the end of step B, the use of small diameter PCC primary crystals, agglomerated/aggregated to form a porous PCC agglomerate.

23 As surface area is a function of particle size distribution, this distribution will have to be set accordingly. The resulting functional pigment surface chemistry ensures an increased ink dye fixation and increased pigment surface area resulting in increased 5 optical density, or a lower cationic additive demand in coating formulation for an equal optical density. No increase or even a decrease in bleeding and'or feathering relative to commercial alternatives is observed. The possibility of obtaining a high solids content slurry with the invention pigment leads to better runnability when incorporated in a paper coating 10 formulation and coated on a coater, such as a MSP (less build-up on MSP rolls). The high solids content leads to less drying energy demand and easier and faster drying; a higher paper machine speed is possible without an increase in deposits on the rolls in paper machine after-drying section. The invention leads to a high solids content coating slurry meaning that 15 less energy must be introduced during the drying step, thereby reducing the cost. Further the use of the inventive aggregates/agglomerates limits the quantity of binder needed, thereby limiting cost. Because the invention will favour agglomerates/aggregates, the 20 applications will be limited to matt inkjet paper applications. The invention agglomerates/aggregates are too coarse to obtain a glossy finish. Various processes of the invention will be better understood through the following description and the following non-limiting examples. 25 EXAMPLES: Examples of preparations of the innovative inkjet pigment and pigment data for the corresponding products: 24 Examples 1, 5 and 7 were prepared according to Steps A of the invention. Examples 2, 3, 4, 6, 8 and 9 were upconcentrations of one of Examples 1, 5 arid 7, upconcentrated according to the invention (Steps B). Example 1: 5 Process of the Invention, Steps A with magnesium sulphate and zinc sulphate: 150 kg of quicklime were added to 1300 litres of tap water in a stirred reactor. Before lime addition the water temperature was adjusted to 400C. The quicklime was slaked for 25 minutes under continuous stirring and the 10 resulting slurry of calcium hydroxide ("milk of lime") at 13.1% w/w solids was then screened on a 100 pm screen. The calcium carbonate precipitation was conducted to a 1000 litre baffled cylindrical stainless steel reactor equipped with an gasing agitator having a gas dispersion unit, a stainless steel carbonation tube to direct a carbon 15 dioxide/air gas stream to the impeller, and probes for monitoring the pH and conductivity of the suspension. 700 litres of the calcium hydroxide suspension obtained in the slaking step as stated above were added to the carbonating reactor and the temperature of the reaction mixture was adjusted to the desired starting 20 temperature of 200C. Prior to carbonation, 30 kg of 10% w/w aqueous solution of magnesium sulphate (MgSO 4 .7H 2 0) was added to the milk of lime. The agitator was then adjusted to 1480 rpm, and the slurry was cartonated by passing a gas mixture of 26 volume percent carbon dioxide 25 in air at 118 Nm 3 /h, corresponding to 19.7 litres per minute at standard temperature and pressure per kilogram of calcium hydroxide, through the sluny. During carbonation, 100 kg of 10% w/w aqueous solution of zinc sulphate (ZnSO 4 .7H 2 0) and 30 kg of 10% w/w aqueous solution of sulphuric acid were added to the reaction mixture in a continuous manner 30 over the total carbonation time.

25 Completion of carbonation was reached after 1 hour, 55 minutes reaction time and indicated by a drop in conductivity to a minimum accompanied by a drop in pH to a constant value below 8.0. During carbonation, the slurry temperature was allowed to rise due to the 5 exothermic nature of the reaction to a final slurry temperature of 57*Q. The residual impurities and/or non-reactive unburnt lime were then removed by passing the aqueous slurry through a 45 pm screen. The product of the above carbonation was an aqueous suspension of 15.6% w/w solids content of ultrafine primary calcium carbonate particles 10 bound together to form stable porous spherical aggregates. The single crystals as constituents of the aggregates featured a particle diameter of 20 to 50 nm and an aspect ratio between 1:2 and 1:10 according to SEM pictures. The porous aggregates formed from these single crystals showed diameters between 1 to 5 pm, with an average 15 diameter of 2 pm, also according to SEM pictures. Pigment data of the product obtained in the process described above are listed as Example 1 in Table 2. The table results for Example 1 confirm the high aggregate/agglomerate surface area and appropriate aggregate/agglomerate dimensions, but an 20 insufficient solids content for subsequent coating applications. Indeed, the results of a coating trial with a low solids formulation run according to the general coating conditions described hereafter, demonstrate that for an equal solids addition per paper surface area, coating with a lower solids formulation leads to a decrease in optical density (Table 1). 25 It is therefore necessary to upconcentrate without a noticeable loss or degradation of aggregates.

26 Table 1: Effect of total slurry solids content on 100% black optical density Total slurry Metal sulphate Metal Sulphate 100% Black solids content in the total slurry type optical density (% wt) solids (% wt) 13.7 10 ZnSO 4 *7H 2 0 2.44 36.7 10 ZnSO 4 *7H 2 0 2.72 Example 2: 5 Process of the invention, upconcentration (Steps B) of the product of Example 1 2210 g of the precipitated calcium carbonate slurry obtained according to process Steps A as described in Example 1 were cooled to 250C and dewatered in Steps B using a pressurized filter. 10 OnE obtains a filter cake of about 43% w/w solids. The filtrate was collected and used for redispersion of the filter cake. 50 g of filtrate obtained in dewatering step as described above was added in a 1 litre dispersing unit equipped with an impeller and mixed with 16 g of a 40% w/w solution of a sodium salt of polyacrylic acid as dispersant. 15 Into this mixture, the filtercake having 57% w/w residual moisture content, as obtained in dewatering step described above, was added stepwise into the dispersing unit under continuous mixing. After each addition of filter cake and subsequent homogenization, the slurry Brookfield viscosity at 100 rpm was determined. The addition of filter 20 cake was stopped when the Brookfield viscosity reached a defined maximum limit of approximately 1000 mPas.

27 At this point 680 g of filter cake had been added. The product of the upconcentration process described above was an aqueous suspension with 39.9% w/w solids content ultrafine primary calcium carbonate particles bound together to form stable porous 5 spherical aggregates of I to 5 pm. The crystalline structure of the product was determined by SEM pictures. Pigment data of the product obtained in the process described above are listed as Example 2 in Table 2. From these data it can be seen that the obtained pigment features a high 10 BET specific surface area value, which shows that one has obtained the high surface needed to interact and bind the ink, along with appropriate aggregate/agglomerate dimensions (1 to 2 pm according to SEM) and yellowing index. The final product additionally features a sufficient solids content for 15 subsequent ink jet paper coating applications. Example 3: Process of the Invention, upconcentration (Steps B) of the product of Example 1 20 2211) g of the precipitated calcium carbonate slurry obtained according to the process described in Example 1 were cooled to 250C and dewatered using a pressurized filter. The filtrate was collected and used for later redispersion of filter cake. 30 g of filtrate obtained in dewatering step as described above was added 25 to a 1 litre dispersing unit equipped with an impeller and mixed with 6.4 g of a 35% w/w solution of Sodium Citrate and 100 g of a 6% w/w solution of sodium salt of Carboxy Methyl Cellulose (CMC) as dispersant.

28 Into this mixture, filtercake having residual moisture of 57% w/w obtained in dewatering step described above was added stepwise to the dispersing unit under continuous mixing. After each addition of filter cake and subsequent homogenization, the slurry Brookfield viscosity at 100 rpm 5 was determined. The addition of filter cake was stopped when the Brookfield viscosity reached a defined maximum limit of approximately 10CO mPas. At this moment 590 g of filter cake had been added. The product of the upconcentration process described above was an 10 aqueous suspension with 36.1% w/w solids content of ultrafine primary calcium carbonate particles bound together to form stable porous spherical aggregates. The crystalline structure of the product was determined by SEM pictures. Pigment data of the product obtained in the process described above are 15 listed as Example 3 in Table 2. The results call for the same comments as in Example 2. Example 4: Process of the Invention, PCC production (Step A, option 20 magnesium sulphate and zinc sulphate) and upconcentration (Steps BL. 150 kg of quicklime were added to 1300 litres of tap water in a stirred reactor. Before lime addition, the water temperature was adjusted to 400 C. 25 The quicklime was slaked for 25 minutes under continuous stirring and the resulting slurry of calcium hydroxide ("milk of lime") at 12.8% w/w solids was then screened on a 100 pm screen.

29 The calcium carbonate precipitation was conducted to a 1000 litre baffled cylindrical stainless steel reactor equipped with an gasing agitator having a gas dispersion unit, a stainless steel carbonation tube to direct a carbon dioxide/air gas stream to the impeller, and probes for monitoring the pH 5 and conductivity of the suspension. 700 litres of the calcium hydroxide suspension obtained in the slaking step as stated above were added to the carbonating reactor and the temoerature of the reaction mixture was adjusted to the desired starting temperature of 20*C. 10 Before the start of carbonation, 30 kg of 10% w/w aqueous solution of magnesium sulphate (MgSO 4 .7H 2 0) was added to the milk of lime. The agitator was then adjusted to 1480 rpm, and the slurry was carbonated by passing a gas mixture of 26 volume percent carbon dioxide in air at 118 Nm 3 I/h, corresponding to 19.7 litres per minute at standard 15 temperature and pressure per kilogram of calcium hydroxide, through the slurry. During carbonation 100 kg of 10% w/w aqueous solution of zinc sulphate (ZnSO 4 .7H 2 0) and 30 kg of 10% w/w aqueous solution of sulphuric acid were added continuously over total carbonation time to the reaction 20 mixture. Completion of carbonation was reached after 1 hour, 50 minutes reaction time and indicated by a drop in conductivity to a minimum accompanied by a d:op in pH to a constant value below 8.0. During carbonation slurry temperature was allowed to rise resulting in a 25 finely slurry temperature of 580C due to the heat generated during the exothermic reaction. Upconcentration step: The slurry was then screened on a 45pm screen before being fed to a dewatering centrifuge (operating at 4440 rpm) at a rate of 350 1/h. To the 30 upc;oncentrated filtercake discharged by the dewatering centrifuge 4.75% 30 w/w of a 40% w/w solution of a sodium salt of polyacrylic acid as dispersing aid was added in a continuous manner. The mixture was then redispersed in a mixing unit and the upconcentrated product was recovered as an aqueous slurry of the pigment. 5 Product of the carbonation and upconcentration steps as stated above was an aqueous suspension of 39% w/w solids content of ultrafine primary calcium carbonate particles bound together to form stable porous spherical aggregates. The single crystals as constituents of the aggregates had acicular particle shape with a diameter of 20 to 50 nm and 10 aspect ratios between 1:2 and 1:10. The porous aggregates formed from these single crystals showed diameters between 1 and 5 pm, with an average diameter of 2 pm. The crystalline structure of the product was determined by SEM pictures. Pigment data of the product obtained in the process described above are 15 listed as Example 4 in Table 2. The results call for the same comments as Examples 2 and 3. Example 5: Process of the invention, Steps A, option magnesium sulphate and 20 aluirninium sulphate: 115 kg of quicklime were added to 1000 litres of tap water in a stirred reactor. Before lime addition the water temperature was adjusted to 40 C. The quicklime was slaked for 25 minutes under continuous stirring and the resulting slurry of calcium hydroxide ("milk of lime") at 12.7% w/w solids 25 was then screened on a 100 pm screen. The calcium carbonate precipitate was conducted in a 1000 litre baffled cylindrical stainless steel reactor equipped with an gasing agitator having a gas dispersion unit, a stainless steel carbonation tube to direct a carbon 31 dioxide/air gas stream to the impeller, and probes for monitoring the pH and conductivity of the suspension. 700 litres of the calcium hydroxide suspension obtained in the slaking step as stated above were added to the carbonating reactor and the 5 temperature of the reaction mixture was adjusted to the desired starting temperature of 20 C. Before the start of carbonation, 30 kg of 10% w/w aqueous solution of magnesium sulphate (MgSO 4 .7H 2 0) was added to the milk of lime. The agitator was then adjusted to 1480 rpm, and the slurry was 10 carbonated by passing a gas mixture of 26 volume percent carbon dioxide in air at 118 Nm 3 /h, corresponding to 19.7 litres per minute at standard temperature and pressure per kilogram of calcium hydroxide, through the slurry. During carbonation, 100 kg of 10% w/w aqueous solution of aluminium 15 sulphate (A1 2

(SO

4

)

3 .18H 2 0) and 30 kg of 10% w/w aqueous solution of sulphuric acid were added continuously to the reaction mixture over the total carbonation time. Completion of carbonation was reached after 1 hour, 48 minutes reaction time and indicated by a drop in conductivity to a minimum accompanied by 20 a drop in pH to a constant value below 8.0. During carbonation, the slurry temperature was allowed to rise resulting in a final slurry temperature of 61 0C due to the heat generated during the exothermic reaction. The slurry was then screened on a 45 pm screen and the product 25 recovered as an aqueous slurry of the pigment. The product of the carbonation step described above was an aqueous suspension with 14.3% w/w solids content of ultrafine primary calcium carbonate particles bound together to form stable porous spherical aggregates.

32 The single crystals as constituents of the aggregates featured acicular particle shapes with a diameter of 20 to 50 nm and aspect ratios between 1:2 and 1:10. The porous aggregates formed from these single crystals showed 5 diameters between 1 to 5 pm, with an average diameter of 2 pm. The crystalline structure of the product was determined by SEM pictures. Pigment data of the product obtained in the process described above are listed as Example 5 in Table 2. 10 Example 6: Process of the invention, upconcentration (Steps B) of the product of Exairnple 5 10 litres of the precipitated calcium carbonate slurry obtained according to process described in Example 5 were screened on a 45 pm screen prior to 15 being fed to a thermal evaporator. The evaporator consisted of a cylindrical stainless steel vessel equipped with an agitator and a double mantle heating unit operating with 1200C hot synthetic oil as heating media. Prior to evaporation 8.5% w/w of a 40% w/w solution of a sodium salt of 20 polyacrylic acid as dispersing aid was added to the precipitated calcium carbonate slurry and mixed in. Thermal upconcentration was achieved through evaporation in said lab evaporator under atmospheric pressure at slurry temperatures ranging from 90 to 950C. 25 The evaporation was stopped when the Brookfield viscosity reached defined maximum limit of approximately 1000 mPas. The product of the upconcentration process described above was an aqueous suspension with 35.5% w/w solids content of ultrafine primary 33 calcium carbonate particles, bound together to form stable porous spherical aggregates. The crystalline structure of the product was determined by SEM pictures. Pigment data of the product obtained in the process described above are 5 listed as Example 6 in Table 2. Example 7: Process of the invention, Steps A (option magnesium sulphate and zinc: sulphate): 10 115 kg of quicklime were added to 1000 litres of tap water in a stirred reactor. Before lime addition the water temperature was adjusted to 400C. The quicklime was slaked for 25 minutes under continuous stirring and the resLIlting slurry of calcium hydroxide ("milk of lime") at 12.5% w/w solids was then screened on a 100 pm screen. 15 The calcium carbonate precipitate was conducted to a 1000 litre baffled cylindrical stainless steel reactor equipped with an gasing agitator having a gas dispersion unit, a stainless steel carbonation tube to direct a carbon dioxide/air gas stream to the impeller, and probes for monitoring the pH and conductivity of the suspension. 20 700 litres of the calcium hydroxide suspension obtained in the slaking step as stated above were added to the carbonating reactor and the temperature of the reaction mixture was adjusted to the desired starting temperature of 200C. Before the start of carbonation, 30 kg of 10% w/w aqueous solution of 25 magnesium sulphate (MgSO 4 .7H 2 0) was added to the milk of lime. The agitator was then adjusted to 1480 rpm, and the slurry was carbonated by passing a gas mixture of 26 volume percent carbon dioxide in air at 118 Nm 3 /h, corresponding to 19.7 litres per minute at standard 34 temperature and pressure per kilogram of calcium hydroxide, through the slurry. During carbonation, 100 kg of 10% w/w aqueous solution of zinc sulphate (ZnSO 4 .7H 2 0) and 30 kg of 10% w/w aqueous solution of sulphuric acid 5 were added continuously to the reaction mixture over the total carbonation time. Completion of carbonation was reached after 1 hour, 43 minutes reaction time and indicated by a drop in conductivity to a minimum accompanied by a drop in pH to a constant value below 8.0. 10 During carbonation, the slurry temperature was allowed to rise resulting in a final slurry temperature of 620C due to the heat generated during the exothermic reaction. The slurry was then screened on a 45 pm screen and the product recovered as an aqueous slurry of the pigment. 15 The product of the carbonation step described above was an aqueous suspension with 13.7% w/w solids content of ultrafine primary calcium carbonate particles bound together to form stable porous spherical aggregates. The single crystals as constituents of the aggregates featured acicular 20 particle shapes with a diameter of 20 to 50 nm and aspect ratios between 1:2 and 1:10. The porous aggregates formed from these single crystals showed diameters between 1 and 5 pm, with an average diameter of 2 pm. The crystalline structure of the product was determined by SEM pictures. 25 Pigment data of the product obtained in the process described above are listed as Example 7 in Table 2. These results call for the same comments as for Example 1.

35 Example 8: Process of the invention, upconcentration (Steps B) of the product of Example 7 10 litres of the precipitated calcium carbonate slurry obtained according to 5 the process described in Example 7 were screened on a 45 pm screen prior to being fed to a thermal evaporator. The evaporator consisted of a cylindrical stainless steel vessel equipped with an agitator and a double mantle heating unit operating with 1200C hot synthetic oil as heating media. 10 Prior to evaporation 8.5% w/w of a 40% w/w solution of a sodium salt of polyacrylic acid as dispersing aid was added to the precipitated calcium carbonate slurry and mixed in. Thermal upconcentration was achieved through evaporation in said lab evaoorator under atmospheric pressure at slurry temperatures ranging 15 from 90 to 95"C. The evaporation was stopped when the Brookfield viscosity reached a defined maximum limit of approximately 1000 mPas. The product of the upconcentration process described above was an aqueous suspension with 36.7% w/w solids content of ultrafine primary 20 calcium carbonate particles, bound together to form stable porous spherical aggregates. The crystalline structure of the product was determined by SEM pictures. Pigment data of the product obtained in the process described above are listed as Example 8 in Table 2. 25 36 Example 9: Process of the Invention, PCC production (Steps A, option magnesium sulphate and zinc sulphate) and upconcentration (Steps 5 115 kg of quicklime were added to 1000 litres of tap water in a stirred reactor. Before lime addition, the water temperature was adjusted to 40* C. The quicklime was slaked for 25 minutes under continuous stirring and the resulting slurry of calcium hydroxide ("milk of lime") at 13.5% w/w solids 10 was then screened on a 100 pm screen. The calcium carbonate precipitation was conducted to a 1000 litre baffled cylindrical stainless steel reactor equipped with an gasing agitator featuring a gas dispersion unit, a stainless steel carbonation tube to direct a carbon dioxide/air gas stream to the impeller, and probes for monitoring 15 the pH and conductivity of the suspension. 700 litres of the calcium hydroxide suspension obtained in the slaking step as stated above, were added to the carbonating reactor and the temperature of the reaction mixture was adjusted to the desired starting temperature of 200C. 20 Before the start of carbonation, 30 kg of 10% w/w aqueous solution of magnesium sulphate (MgSO 4 .7H20) was added to the milk of lime. The agitator was then adjusted to 1480 rpm, and the slurry was carbonated by passing a gas mixture of 26 volume percent carbon dioxide in air at 118 Nm 3 /h, corresponding to 19.7 litres per minute at standard 25 temperature and pressure per kilogram of calcium hydroxide, through the slurry. During carbonation, 100 kg of 10% w/w aqueous solution of zinc sulphate (ZnSO 4 .7H 2 0) and 30 kg of 10% w/w aqueous solution of sulphuric acid were added continuously to the reaction mixture over the total carbonation time.

37 Completion of carbonation was reached after 1 hour, 44 minutes reaction time and indicated by a drop in conductivity to a minimum accompanied by a drop in pH to a constant value below 8.0. During carbonation, the slurry temperature was allowed to rise resulting in 5 a final slurry temperature of 560C due to heat generated during the exothermic reaction. ThE slurry was then screened on a 45pm screen. Upconcentration step: ThE screened slurry was then fed at a rate of 400 I/h to a dewatering 10 centrifuge operating at 4440 rpm. To the upconcentrated filtercake discharged by the dewatering centrifuge, 6% w/w of a 40% w/w solution of a sodium salt of polyacrylic acid as dispersing aid was added in a continuous manner. The mixture was then redispersed in a mixing unit and the upconcentrated 15 product was recovered as an aqueous slurry of the pigment. The product of the carbonation and upconcentration steps described above was an aqueous suspension with 39.9% w/w solids content of ultrafine primary calcium carbonate particles, bound together to form stable porous spherical aggregates. The single crystals as constituents of 20 the aggregates had acicular particle shape with a diameter of 20 to 50 nm and aspect ratios between 1:2 and 1:10. The porous aggregates formed from these single crystals showed diameters between 1 and 5 pm with an average diameter of 2 pm. The crystalline structure of the product was determined by SEM pictures. 25 Pigment data of the product obtained in the process described above are listed as Example 9 in Table 2. In Table 2, specific surface area (SSA) was measured using a Tristar 3000 Analyzer, particle size distribution (PSD) using a Helos Sympatec, brightness using a Datacolor Elrepho 3000 Jerics, solids content using a 38 Mettler Toledo HB43 Halogen balance, and viscosity using a Brookfield DVII Viscometer, all according to the recommendations of the manufacturer.

39 0) 0 (D (n O E U))O 0) 0 oo C( i Cj CD V) CD NO w=f C'~ C 0) - ce) N) 00 CD LOc W D Nt -Y 0) .2 0 o U) (D N > U) .OClL CL) LIl 0) C, E m) L N: CD UD 04 UD C6 0) -V 0) 4 E LOcoc oi EN Ni 0 Ul. U)U) mm)Y EE c ND 0 0 ca CD 0) N CD a Z -) cis) U) l) W N 0) Ce 0 o :a C Cl E .2 E >C ~C 0 _ (I a; C w ~ C LI- 0) C2) E -a 0) 0 -E E) L- c C Dl Lo CV co co NU) 0 0) o- ) (D , U ~ ~ ) N ~ U C~0 . Ia) co-00 .. V V < .r f I 40 Coating trials A selection of the above products of the invention were introduced in paper coating slurries and coated onto paper. Coating Trials based on Example 4, 6 and 8 slurries 5 Three paper coating slurries were prepared, each using one of three PCC slurries prepared according to the invention, along with standard additives. Emox TSC is an oxidized potato starch from Emsland-Staerke GmbH, Basoplast PR8172 is a binder from BASF, Catiofast CS is a Poly-Dadmac cationic additive from BASF, and Lupamin 6005 is a polyvinyl-formamide 10 from BASF.

41 Table 3: Coating formulation compositions (by parts) Coating Slurry Solids content Coating Coating Coating (% w/w) Slurry 1 Slurry 2 Slurry 3 PCC Slurry of the invention Example 4 39.0 100 Example 6 35.5 100 Example 8 36.7 1 1 100 Additives Emo: TSC (Emsland-Staerke 40 25 GmbH) 35 25 25 Basoplast PR8172 (BASF) 40 10 10 10 Caticfast CS (BASF) 33 10 30 10 10 Lupamin 6005 (BASF) 30 1 1 1 Final Coating Slurry Characteristics Final solids content % 37.5 35.7 36.6 Final slurry pH - 9.0 8.3 8.4 Brookfield viscosity at 200C mPas 1.60 580 460 Twc additional paper coating slurries were prepared, each using one of two PCC flurries prepared according to the invention, along with another 42 selection of standard additives (Mowiol 26-88, Printofix Cartafix VXT01 and Cartabond TS1 from Clariant). Table 4: Coating formulation compositions (by parts) Coating Slurry Solids content Coating Coating (% w/w) Slurry 4 Slurry 5 PCC Slurry of the Invention Example 6 36.7 100 Example 8 35.4 100 Additives Mowiol 26-88 7.6 12 12 Printofix 43.0 5 5 Cartafix VXT01 20.0 3 3 Cartabond TS1 43.0 1.5 1.5 Final Coating Slurry Characteristics Final slurry pH - 8.3 8.0 Final slurry solids content % 27.8 27.8 Final slurry Brookfield viscosity mPas 300 100 at 200C 5 Coating Slurry 1 was then coated simultaneously on both sides of a base paper, which is described in Table 5, using the Jagenberg MSP under the conditions listed in Table 6.

43 Table 5: Characteristics of the base paper coated using Coating Slurry 1 Grammage: 84.1 g/m 2 Filler content (otro): 23.9% Tension length: 4.75 km Surface contact angle OS (1a): 112.2 Surface contact angle OS (10a): 106.6 Yelhow index OS: -25.6% 44 Table 6: Coating Machine Conditions on the Jagenberg MSP using Coating Slurry 1 Coating speed: 560 m/min Coating application weight: 9.8 - 10.8 g/m 2 Coating Moisture content: 5.2 - 5.4 % Coating colour temperature during 28*C coating: Coating heads Left Right Type of coating rod: C25 C25 Coating rod speed: 200 rpm 200 rpm Coating rod pressure: 1.5 bar 1 .5 bar Pumping speed: 60 rpm 60 rpm Pumping pressure: 0.8 bar 1.1 bar Calendering Number of NIPS: 1 Calendering speed: 200 m/min Calendering pressure: 65 kN/m Calendering temperature: 600C Coating Slurries 2, 3, 4 and 5 were coated on one side of a base paper, 5 which is described in Table 7, using the K-Coater under the conditions listed in Table 8.

45 Table 7: Characteristics of the base paper coated In Coating Slurries 2, 3, 4 and 5 Grammage 89.2 g/m 2 Filler content (otro) 12.9% Tension length 5.26 km Surface contact angle OS (1a) 109.3 Surface contact angle OS (1Oa) 106.4 Yellow index OS -18.3% Table 8: Coating Machine Conditions on a K-Coater with a grooved 5 rod for Coating Slurries 2, 3, 4 and 5 Coating application weight 8 g/m 2 _Coating Moisture content 5 % Coating colour temperature during 23*C coating Paper drying conditions Dried in a lab oven at 800C for 4 minutes Ink let printing trials Printing trials on three different inkjet printers, namely the Epson Stylus Photo 950, the HP Deskjet 5550 and the Canon i950, were used to compare the inkjet printability of the papers coated with the pigments of 10 the invention as opposed to market inkjet papers. The printing test cards were designed to assess the optical density, as well as the degree of feathering and bleeding.

46 The HP Bright White and Epson S041214 papers are marketed as a multipurpose inkjet papers. The Zweckform 2585 and Epson S041061 papers are considered to represent high quality matt inkjet papers, offering a higher print quality than standard multipurpose inkjet papers. 5 Optical density was measured using the Gretag D 186 densitometer according to the standard procedures indicated by the manufacturer. For an equal quantity of applied ink, the higher the optical density, the better the coating maintains the dyes on the paper surface. Paper Coated with Coating Slurry 1: 10 The following coating trial (Coating Trial 1) was performed coating Coating Slurry 1, which was based on the PCC slurry of Example 4, on the base paper as described above. Bleeding and feathering on a first type of printing test card were measured using PapEye instrumentation from ONLY Solution GmbH according to 15 the standard procedures given by the manufacturer. The lower the measured value, the better the bleeding and feathering.

47 Table 9: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Papers Printer type Optical density Gretag-Macbeth D186 cyan magent yello Green, Blue, m Red, y Epson stylus black black (c), a (m) w (y), c 100% 100% 100% Bleed Feath _poto 950 100% 80% 100% 100% 10 y 100% c 100% m 100% i ering 300.4 448.5 Zpeckform 2585 2.28 2.04 1.73 1.47 1.23 1.37 1.75 1.39 5 6 304.5 460.7 Epson S041061 2.29 2.02 1.58 1.42 1.11 1.31 1.70 1.36 2 6 348.7 539.4 HF' Bright White 1.92 1.71 1.31 1.26 1.08 1.15 1.43 1.16 1 6 M 350.4 532.8 son S041214 1.58 1.39 0.97 1.02 0.89 0.89 1.11 0.93 0 0 5 The above table shows that the optical density obtained with the product ot the invention is superior to comparable multipurpose market papers, and approaches the quality of a superior inkjet paper. The bleeding obtained with the product of the invention is equal or inferior to other equivalent market papers. The feathering obtained with the product of the 10 invention is inferior to other market papers. The improved optical density, bleeding and feathering attest to an improved balance of absorption/adsorption properties of the paper coating relative to competing market products. Further, the pigment structure did not negatively influence runnability; the 15 runnability was actually improved since less dry built-up on the MSP was observed.

48 Table 10: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Pap ers Printer type Colour density Gretag-Macbeth D186 cyan magent yello Green, Blue, m Red, y HP Deskiet black black (c), a(m) W (y), c 100% 100% 100% Bleed Feath 5550 100% 80% 100% 100% 100% y 100% c 100% m 100% Ing ering Zweokform 310.6 503.2 2581; 2.06 1.91 1.99 1.26 0.93 1.06 1.75 1.31 9 4 312.9 520.7 Epson S041061 1.95 1.81 1.85 1.19 0.92 1.03 1.67 1.28 2 8 319.5 494.8 HP Bright White 2.35 2.05 1.71 1.17 0.94 1.04 1.56 1.32 1 6 331.3 514.5 E son S041214 1.85 1.68 1.39 1.01 0.83 0.89 1.28 1.02 5 9 The optical density results of the invention were superior to comparable 5 market papers and in some cases higher quality inkjet papers as well. A decreased bleeding and similar degree of feathering relative to comparable and one of the higher quality papers was also noted. Again, the pigment structure did not negatively influence runnability; the runnability was improved since little dry built-up on the film press was 10 observed.

49 Table 11: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Papers Printe; type Colour density Gretag-Macbeth D186 cyan magent yello Green, Blue, m Red, y black black (c), a (m) w (y), c 100% 100% 100% Bleed Feath Canon 1950 100% 95% 100% 100% 100% Y 100% c 100% n 100% Ing erlng Zweckform 299.6 470.1 2585 2.21 1.95 1.41 1.84 1.00 0.99 2.16 1.59 6 3 303.9 479.1 Epson 3041061 2.17 1.82 1.22 1.75 0.91 0.96 1.90 1.55 7 4 354.4 549.3 HP Bright White 1.751 1.54 1.171 1.51 0.86 0.93 1.65 1.28 3 9 348.4 527.0 pson 9041214 1.42 1.29 0.991 1.281 0.771 0.771 1.24el 1.07 t 4 j 3 The optical density results of the invention were mostly superior to those 5 of other comparable market papers, and approached the values given by superior quality papers. A decreased bleeding and similar degree of feathering relative to comparable market papers was noted. Papers Coated with Coating Slurries 2 and 3: 10 The following coating trials were performed using aluminium and zinc basEd PCC slurries, each thermally upconcentrated. Coating the base pap-r with Coating Slurries 2 and 3 lead, respectively, to Coating Trial 2 and 3 results below. A second type of test card was used to evaluate optical density, bleeding and feathering. 15 Bleeding and feathering were measured using the Personal IAS@ (Image Analysis System) instrumentation from Quality Engineering Association, 50 Inc., according to the standard procedures given by the manufacturer. The lower the measured value, the better the bleeding and feathering. Tablo 12: Optical Density and Bleeding/Feathering Results of Paper 5 Coated with the Coating Pigment of the Invention, as Opposed to Market Pape s Printer type Optical density' Gretag-Macbeth DI 86 cyan magent yello Green, Blue, m Red, y Epson stylus black black (c), a (m) w (y), c 100% 100% 100% Bleed Feath photo S5O 100% 80% 100% 100% 100% y 100% c 100% n 100% In ring 164.1 Zweckorm 2585 2.38 1.29 2.25 1.64 1.54 1.66 2.04 1.55 4 58.00 166.3 Epson S041061 2.45 1.23 2.09 1.59 1.49 1.54 1.85 1.51 4 67.63 239.2 104.3 jHP ht White 2.09 1.06 1.72 1.42 1.34 1.32 1.61 1.31 0 7 The above table shows that the optical density obtained with the product of the invention is superior to comparable market papers, and sometimes surpassed even higher quality paper values. The bleeding obtained with 10 the product of the invention is inferior to other equivalent market papers. The feathering obtained with the product of the invention is lower than other comparable market papers. The paper brightness was similar to market papers.

51 Table 13: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Papers Printer ty.e Optical density Gretag-Macbeth D186 cyan magent yello Green, Blue, m Red, y HP Deskjet black black (c), a (m) w (y), c 100% 100% 100% Bleed Feath 5550 100% 80% 100% 100% y100% y100% c100% m100% Ing edlng Zweckform 237.7 2585 above 1.16 0.98 1.00 1.46 1.20 1.84 1.38 2 produc M 193.6 Epson S41061 1.92 1.09 0.97 0.97 1.47 not 1.73 1.47 9 marke M M 237.7 it White 2.35 1.24 he 1.01 1v i 1.7 1.33 2 72.59 The above table shows that the optical density obtained with the product 5 of the invention was clearly superior to not only comparable market papers, but sometimes higher quality paper as well. The bleeding obtained with the product of the invention is equal or inferior to other equivalent market papers. The feathering obtained with the product of the invention is lower than or similar to other comparable market papers. The paper 10 brightness was similar to market papers.

52 Table 14: Optical Density and Bleeding/Feathering Results of Paper Coaied with the Coating Pigment of the Invention, as Opposed to Market Pa ers Printer type Optical density Gretag-Macbeth D186 cyan magont yello Green, Blue, m Red, y black black (c), a (m) w (y), c 100% 100% 100% Bleed Feath Canon 1950 100% 80% 100% 100% 100% y 100% c 100% m 100% Ing . ering Zweckform 198.6 2585 2.07 1.20 2.30 1.74 1.71 1.58 2.31 1.85 3 59.64 204.4 Epson S041061 2.06 1.17 2.06 1.80 1.66 1.42 1.82 1.68 5 63.72 245.3 HP Bri ht White 1.72 1.03 1.73 1.58 1.49 1.26 1.58 1.48 2 90.74 The above table shows that the optical density obtained with the product 5 of the invention is superior to comparable market papers, and sometimes surpassed even higher quality paper values. The bleeding obtained with the product of the invention is equal or inferior to other equivalent market papers. The feathering obtained with the product of the invention is lower than other comparable market papers. The paper brightness was similar 10 to market papers. Papers Coated with Coating Slurries 4 and 5: The following coating trials were performed using aluminium and zinc based PCC slurries of Examples 6 and 8, thermally upconcentrated. 15 Coating the base paper with Coating Slurries 4 and 5 lead, respectively, to Coating Trial 4 and 5 results below.

53 Bleeding and feathering were measured using the second printing test card and Personal lAS@ (Image Analysis System) instrumentation from Quality Engineering Association, Inc., according to the standard procedures given by the manufacturer. The lower the measured value, the 5 better the bleeding and feathering. Table 15: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Pape s Printer type Optical denst Gretag-Macbeth D186 cyan magent yello Green, Blue, m Red, y Epson stylus black black (c), a (m) w (y), C 100% 100% 100% Bleed Feath photo ;50 100% 80% 100% 100% 100% y 100% c 100% m 100% Ing ering 164.1 Zwecktorm 2565 2.38 1.29 2.25 1.64 1.54 1.66 2.04 1.55 4 58.00 166.3 Epson S041061 2.45 1.23 2.09 1.59 1.49 1.54 1.85 1.51 4 67.63 239.2 104.3 HP Bri ht White 2.09 1.06 1.72 1.42 1.34 1.32 1.61 1.31 0 7 The above table shows that the optical density obtained with the product 10 of the invention is superior to comparable multipurpose market papers, and approaches the quality of a superior inkjet paper. The bleeding obtained with the product of the invention is equal or inferior to other equivalent market papers. The feathering obtained with the product of the invention is inferior to other market papers. 15 The improved optical density, bleeding and feathering attest to an improved balance of absorption/adsorption properties relative to competing market products.

54 Table 16: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Papers Printer type Optical density Gretag-Macbeth D186 cyan magent yello Green, Blue, m Red, y HP DeskJet black black (c), a (m) w (y), c100% 100% 100% Bleed Feath 5550 100% 80% 100% 100% 100% y 100% o100% n 100% Ing ering Zweckform 237.7 2585 2.08 1.16 0.98 1.00 1.46 1.20 1.84 1.38 2 63.94 193.6 son S041061 1.92 1.09 D.97 0.97 1.47 1.18 1.73 1.47 9 66.95 . 237.7 HPB1ht White 2.35 1.24 1.02 1.01 1.39 1'.17 1.69 1.33 2 72.59 The optical density results.of the invention were superior to comparable 5 market papers as well as higher quality inkjet papers. A decreased bleeding and an increase in feathering relative to comparable papers were also noted.

55 Table 17: Optical Density and Bleeding/Feathering Results of Paper Coated with the Coating Pigment of the Invention, as Opposed to Market Papers Printr type Optical enalty retag-Macbeth D186 cyan magent yello Green, Blue, m Red, y black black (c), a (M) w (y), c 100% 100% 100% Bleed Feath Canon 1950 100% 80% 100% 100% 100% y 100% c100% m100% Ing ering Zweckiorm 198.6 2585 2.07 1.20 2.30 1.74 1.71 1.58 2.31 1.85 3 59.64 204.4 Epson S041061 2.06 1.17 2.06 1.80 1.66 1.42 1.82 1.68 5 63.72 245.3 HPiht White 1.2 1.03 1.73 1.58 1.49 1.26 1.58 1.46 2 90.74 The optical density results of the invention were always superior to those 5 of other comparable market papers, and approached the values given by superior quality papers. A decreased bleeding and similar degree of feathering relative to comparable market papers was noted. The present invention also covers the technical equivalents of the above 10 des-ription, as well as options that would be easily available to the skilled man when reading the present application.

Claims (21)

1. Process for providing PCC useful for ink-jet printing applications, - of the type according to which a calcium hydroxide slurry is first prepared by mixing quicklime (CaO) with water in a stirring reactor or tank ("slake"), the calcium hydroxide slurry is then s screened, such as on a 100 pm screen, to remove any residual impurities and/or non-reactive unburnt lime, the screened slurry is then directed towards a stainless steel reactor equipped with an agitator; the temperature is adjusted, generally to between 10 and 70*C, and subsequently the slurry is directed towards a carbonation reactor or tank, wherein carbon dioxide-containing gas is bubbled through the slurry, the slurry exits the carbonation tank when appropriate in view of 10 conductivity and pH, generally when the conductivity reaches a minimum and the pH drops below 8, coarse particles are removed on a screen, such as a 45 pm screen, such that the slurry contains only the ultrafine PCC agglomerates of the invention, - wherein the implementation of process steps comprises the following: A First steps, production of the PCC: is A1 - the carbonation step is performed at a carbonation gas flow rate of below 30 litres per minute at standard temperature and pressure per kilogram calcium hydroxide during precipitation; A2 - the slurry of calcium hydroxide leaving the stainless steel reactor after the separation of the 20 residual impurities and/or non-reactive unburnt lime is treated by a combination of magnesium sulphate and Group |1 and/or Group Ill metal sulphates - most preferably in the presence of an acid - the acid being most preferably sulphuric acid - until stable, porous agglomerates/aggregates are obtained at a concentration of 5 to 25% 25 solids, preferably 15 to 20% solids ("precursor"); A3 - the slurry of calcium hydroxide is first prepared by mixing quicklime with water in a stirring reactor or tank ("slake") in a weight ratio of CaO: water between 1:3 and 1:20, preferably between 1:5 and 1:12, most preferably between 1:7 and 1:10; 30 A4 - the temperature is preferably adjusted to between 15 and 500C, most preferably to between 15 and 30"C, before the slurry is directed towards the carbonation reactor or tank. 57

2. Process according to claim 1, wherein Steps A are followed by the following steps, Steps B: B upconcentration of the "precursor": dewatering/redispersing steps following the above "Steps A", - upconcentration of the PCC produced during Steps A is performed under sufficiently gentle s or mild conditions for the aggregates/agglomerates not to be substantially destroyed, - with a cationic, anionic or a combination dispersant, - and the amount of dispersant added is controlled so that the PCC agglomerates/aggregates of the precursor are just coated, this quantity corresponding to that added prior to a slurry viscosity increase, 10 - until a concentration of 25 to 60%, preferably in the range 35 to 50%, most preferably 39 to 40% solids by weight is reached.

3. Process according to claim 1 or 2, wherein in Steps A one applies at least one of the following parameters: - the carbonation gas flow rate is selected in the range of 1 to 30, preferably 10 to 20, most 15 preferably around 19.7 litres per minute at standard temperature and pressure per kilogram calcium hydroxide during precipitation, - the carbonation gas is CO 2 or a mixture of C02 and one or more other gases, such as air and/or nitrogen, - the slurry of calcium hydroxide is treated by a combination of magnesium sulphate and 20 aluminium sulphate, - or a combination of magnesium sulphate and zinc sulphate.

4. Process according to any one of claims 1 to 3, wherein in Steps A one applies at least one of the following parameters: - zinc sulphate is added to the combination of magnesium sulphate and aluminium sulphate, 25 - aluminium sulphate is added to the combination of magnesium sulphate and zinc sulphate, - the addition of magnesium sulphate is performed before carbonation, - magnesium sulphate is added, either before the addition of other sulphates or during that addition, - magnesium sulphate is added during carbonation along with aluminium and/or zinc 30 sulphate, - magnesium sulphate is added during carbonation or at the beginning of carbonation, - the addition of aluminium sulphate and/or zinc sulphate takes place during carbonation, 58 - the addition of the acid, namely sulphuric acid, most preferably under the form of a 10% by weight solution of H2SO 4 takes place at the beginning of carbonation, - the addition of H 2 SO 4 takes place simultaneously with the addition of aluminium or zinc sulphate, 5 - in all the above options, sulphates of Group |1 and/or IlIl can be added in addition to aluminium and/or zinc sulphates, or as a substitute for aluminium and/or zinc sulphates, - the temperature in the carbonation tank is observed to rise up to between 40 to 800C, preferably up to between 50 to 60*C, most preferably up to between 56 and 57*C, - removal of residual impurities and/or non-reactive unburnt lime takes place on a 45 pm io mesh screen when the Brookfield viscosity of the material existing the carbonation tank is sufficiently low, namely less than 100 mPas at 100 rpm, - the final slurry product substantially consists of stable, porous agglomerates/aggregates.

5. Process according to any one of claims 2 to 4, wherein in Steps B, - by "gentle or mild conditions" it is meant that the deagglomeration/deaggregation of the 15 agglomerates/aggregates is kept to a minimum so that the agglomerates/aggregates are not "substantially destroyed", that is, during the upconcentration steps: - the increase of surface area is limited to less than 50%, preferably less than 25% , and/or - the increase of the fraction of particles below 2 pm is limited to less than 50%, preferably less than 25%, most preferably less than 10%, and/or 20 - the decrease of the mean aggregate diameter is limited to less than 50%, preferably less than 20%, most preferably less than 15%, as measured using a Helos Sympatec apparatus, - by "deagglomeration/deaggregation" it is meant that the agglomerates/aggregates obtained at the end of Steps A by the specific process of the invention are disintegrated, - the upconcentration step can be performed in the form of any thermal or mechanical 25 separation technology for solid/liquid suspensions provided the aggregates/agglomerates obtained in Steps A ("precursor") are sufficiently stable and are not "substantially destroyed" by the technology.

6. Process according to any one of claims 2 to 5, wherein: - upconcentration is performed in a centrifuge, or a pressurized filter, or vacuum filtration or 30 by thermal upconcentration, in the presence of a cationic, anionic or combination dispersant, - and wherein the final slurry concentration is about 39 to 40% solids by weight. 59

7. Process according to any one of claims 2 to 6, wherein: - the upconcentration leads to a filter cake, such as by upconcentration in a pressurized filter or in a centrifuge or by vacuum filtration, and in such a case: - the concentrated material is optionally washed with water 5 - a redispersion is performed - until the final material substantially consists of stable, porous agglomerates/aggregates identical with or very similar to those obtained in Steps A, of claim 1; - the upconcentration can be performed in a thermal evaporation step with the material substantially remaining under the form of the stable, porous agglomerates/aggregates obtained in 10 Steps A of claim 1.

8. Process according to any one of claims 2 to 7 wherein: - the upconcentration of part or all of the precursor leads to a dry product, and in such a case: - a redispersion is performed is - until the final material substantially consists of stable, porous agglomerates/aggregates identical with or very similar to those obtained in Steps A of claim 1.

9. Process according to any one of claims 1 to 8 wherein approximately 5 to 9% w/w of a 40% solution of a sodium salt of polyacrylic acid relative to dry calcium carbonate is added as a dispersant to the slurry containing the pigment obtained in claim 1 (Steps A) (corresponding to 20 approximately 1.5 to 3.5% weight dry polyacrylic acid on dry calcium carbonate).

10. Process according to any one of claims 2 to 7, wherein the final slurry concentration is partially or wholly obtained by the addition of one or more additional pigments or pigment slurries during Steps B.

11. Process for providing PCC useful for ink-jet printing applications, said process as claimed in 25 claim 1 and substantially as hereinbefore described with reference to any one of the Examples and/or any one of the accompanying drawings.

12. Stable, porous aggregates/agglomerates of PCC wherein they have been obtained according to any one of claims 1 to 11. 60

13. Stable, porous aggregates/agglomerates of PCC obtained by the process of any one of claims 1 to 11 wherein they feature the following properties: - a specific surface area of 30 to 100 m 2 /g, preferably from 50 to 80 m 2 /g, and/or -a mean aggregate diameter of 1 to 5 pm, with an average diameter of 2 pm, and/or 5 - a fraction of fines below 2 pm of less than 20%, preferably less than 15% (as measured on a Helos sympatec), and/or -a primary particle size of the acicular particles of 20 nm to 50 nm with an aspect ratio between 1:2 and 1:10 and/or - a solids content, by weight from 5 to 25%, preferably 15 to 20% at the end of Steps A, and 1o a solids content of 25 to 60%, preferably 35 to 50% solids, in particular 39 to 40% solids at the end of Steps B.

14. Pigments, wherein they comprise stable, porous PCC aggregates/agglomerates according to claim 12 or 13.

15. Pigments, or PCC slurries wherein they comprise stable, porous PCC 15 aggregates/agglomerates according to claim 12 or 13.

16. Pigments or PCC slurries according to claim 15, wherein their solids concentration is, by weight: - when in the form of the "precursor" at the end of Steps A, from 5 to 25%, preferably from 15 to 20% solids 20 - when in the form of the final upconcentrated PCC (Steps B), from 25 to 60% solids, preferably from 35 to 50% solids, in particular from 39 to 40% solids.

17. Coating formulations for the paper making industry wherein they comprise aggregates/agglomerates of PCC, pigments and/or slurries according to any one of claims 12 to 16.

18. Coating formulations according to claim 17 wherein the PCC slurry which it contains features 25 the following properties, - a solids content of 25 to 60%, preferably from 35 to 50%, in particular from 39 to 40% by weight, and/or - a high specific surface area PCC, with a specific surface area of 30 to 100 m 2 /g, preferably from 50 to 80 m 2 /g. 61

19. Applications of the coating formulations according to claims 17 or 18 to the coating of inkjet paper.

20. Applications of the coating formulations according to claim 17 or 18 to the coating of "multipurpose" inkjet paper or of specialty, high quality, paper.

21. Inkjet paper, namely "multipurpose" inkjet paper or specialty, high quality, paper, wherein it is coated by at least a coating composition according to claim 17 or 18. Omya Development AG Patent Attorneys for the Applicant/Nominated Person SPRUSON & FERGUSON