Precipitated calcium carbonate pigment, especially for use in inkjet printing paper coatings
원문보기
IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C01F-001/00
C01F-005/24
C01F-011/18
C22B-026/20
B82Y-030/00
출원번호
US-0887748
(2006-03-29)
등록번호
US-8883098
(2014-11-11)
우선권정보
EP-05075901 (2005-04-11)
국제출원번호
PCT/IB2006/000975
(2006-03-29)
§371/§102 date
20071003
(20071003)
국제공개번호
WO2006/109171
(2006-10-19)
발명자
/ 주소
Kaessberger, Michael
Pohl, Michael
출원인 / 주소
Omya International AG
대리인 / 주소
Amster, Rothstein & Ebenstein LLP
인용정보
피인용 횟수 :
0인용 특허 :
9
초록▼
Novel and innovative PCC pigments, having a reduced production cost, able to be used in a paper coating formulations to manufacture coated high-quality matt papers, in particular for inkjet applications. Process for the preparation of same, using a reduced flow rate of a carbon dioxide-containing ga
Novel and innovative PCC pigments, having a reduced production cost, able to be used in a paper coating formulations to manufacture coated high-quality matt papers, in particular for inkjet applications. Process for the preparation of same, using a reduced flow rate of a carbon dioxide-containing gas in the PCC carbonation step, which produces stable, porous, agglomerates of PCC featuring unique properties and structure, this step being followed by an upconcentration step to increase the solids content.
대표청구항▼
1. A process for preparing precipitated calcium carbonate (PCC) useful for ink jet printing applications comprising the steps of: a) preparing a calcium hydroxide slurry by mixing quicklime (CaO) with water;b) screening the calcium hydroxide slurry obtained in step a) to obtain a screened slurry;c)
1. A process for preparing precipitated calcium carbonate (PCC) useful for ink jet printing applications comprising the steps of: a) preparing a calcium hydroxide slurry by mixing quicklime (CaO) with water;b) screening the calcium hydroxide slurry obtained in step a) to obtain a screened slurry;c) adjusting the temperature of the screened slurry to obtain a temperature adjusted slurry;d) contacting the temperature adjusted slurry with a carbon dioxide-containing gas at a carbonation gas flow rate of below 30 liters per minute at standard temperature and pressure per kilogram calcium hydroxide in the presence of (i) magnesium sulphate and aluminium sulphate, (ii) magnesium sulphate and zinc sulphate, or (iii) magnesium sulphate, aluminium sulphate and zinc sulphate, to obtain agglomerates/aggregates; ande) screening the agglomerates/aggregates obtained in step d) to obtain ultrafine PCC agglomerates having a mean aggregate diameter of 1 to 5 μm, wherein the ultrafine PCC agglomerates comprise ultrafine calcium carbonate particles bound together. 2. The process of claim 1, wherein the calcium hydroxide is prepared in step a) by mixing quicklime with water in a weight ratio of CaO:water between 1:3 and 1:20. 3. The process of claim 2, wherein the weight ratio of CaO:water in step a) is between 1:5 and 1:12. 4. The process of claim 2, wherein the weight ratio of CaO:water in step a) is between 1:7 and 1:10. 5. The process of claim 1, wherein the calcium hydroxide slurry is screened in step b) with a 100 μm screen. 6. The process of claim 1, wherein the temperature of the slurry in step c) is adjusted to between 10 and 70° C. 7. The process of claim 1, wherein the temperature of the slurry in step c) is adjusted to between 15 and 50° C. 8. The process of claim 1, wherein the temperature of the slurry in step c) is adjusted to between 15 and 30° C. 9. The process of claim 1, wherein in step d) magnesium sulphate is introduced before carbonation or at the beginning of carbonation. 10. The process of claim 1, wherein in step d) magnesium sulphate is added before the addition of aluminium and/or zinc sulphate or in combination with the addition of aluminium and/or zinc sulphate. 11. The process of claim 1, wherein in step d) carbonation takes place in the presence of magnesium sulphate and aluminium sulphate. 12. The process of claim 1, wherein in step d) carbonation takes place in the presence of magnesium sulphate, aluminium sulphate and zinc sulphate. 13. The process of claim 1, wherein in step d) carbonation takes place in the presence of magnesium sulphate and zinc sulphate. 14. The process of claim 1, wherein in step d) magnesium sulphate is added during carbonation along with aluminium and/or zinc sulphate. 15. The process of claim 1, wherein in step d) magnesium sulphate is added before carbonation and aluminium sulphate and/or zinc sulphate is added during carbonation. 16. The process of claim 1, wherein in step d) carbonation takes place in the presence of an acid. 17. The process of claim 16, wherein the acid is added before or at the beginning of carbonation. 18. The process of claim 16, wherein the acid is sulphuric acid. 19. The process of claim 18, wherein the sulphuric acid is a 10% by weight solution of sulphuric acid. 20. The process of claim 18, wherein the addition of sulphuric acid takes place simultaneously with the addition of aluminium or zinc sulphate. 21. The process of claim 1, wherein in step d) the temperature of the slurry is observed to rise up to between 40 to 80° C. 22. The process of claim 1, wherein in step d) the temperature of the slurry is observed to rise up to between 50 to 60° C. 23. The process of claim 1, wherein in step d) the temperature of the slurry is observed to rise up to between to 56 and 57° C. 24. The process of claim 1, wherein in step d) the carbonation gas flow rate is in the range of 1 to 30 liters per minute at standard temperature and pressure per kilogram calcium hydroxide. 25. The process of claim 1, wherein in step d) the carbonation gas flow rate is in the range of 10 to 20 liters per minute at standard temperature and pressure per kilogram calcium hydroxide. 26. The process of claim 1, wherein in step d) the carbonation gas flow rate about 19.7 liters per minute at standard temperature and pressure per kilogram calcium hydroxide. 27. The process of claim 1, wherein in step d) the carbonation gas is CO2 or a mixture of CO2 and one or more other gases. 28. The process of claim 27, wherein the one or more other gases is air and/or nitrogen. 29. The process of claim 1, wherein in step d) the carbonation is completed when conductivity reaches a minimum and pH drops below 8. 30. The process of claim 1, wherein in step d) agglomerates/aggregates are obtained at a concentration of 5 to 25% solids. 31. The process of claim 1, wherein in step d) agglomerates/aggregates are obtained at a concentration of 15 to 20% solids. 32. The process of claim 1, wherein in step e) the screening is performed with a 45 μm screen. 33. The process of claim 1, wherein the ultrafine PCC agglomerates obtained in step e) comprise ultrafine calcium carbonate particles bound together to form stable porous spherical aggregates. 34. The process of claim 33, wherein the ultrafine calcium carbonate particles have a primary acicular particle size of 20 to 50 nm, and an aspect ratio of between 1:2 and 1:10. 35. The process of claim 1, wherein the ultrafine PCC agglomerates have an average diameter of 2 μm. 36. The process of claim 1, further comprising subjecting the ultrafine PCC agglomerates obtained in step e) to dewatering and/or redispersing steps to obtain a PCC product. 37. The process of claim 36, wherein the dewatering comprises upconcentrating the ultrafine PCC agglomerates under sufficiently gentle or mild conditions for the aggregates/agglomerates not to be substantially destroyed, wherein said upconcentrating is conducted without the use of a dispersing aid or with a cationic dispersing aid. 38. The process of claim 37, wherein the amount of any added cationic dispersant aid is controlled so that the ultrafine PCC agglomerates are coated. 39. The process of claim 37, wherein the upconcentration is performed in a centrifuge, a pressurized filter, by vacuum filtration or by thermal upconcentration, without dispersant or in the presence of a cationic dispersant. 40. The process of claim 37, wherein the cationic dispersant is a cationic copolymer of [2-(methacryloyloxy)ethyl]trimethyl ammonium chloride and [3-(methacrylamido)propyl]trimethyl ammonium chloride. 41. The process of claim 40, wherein the cationic dispersant is used in combination with hydroxylethyl cellulose. 42. The process of claim 37, wherein the upconcentration results in a concentrated material that is optionally washed with water, followed by redispersion to obtain the PCC product. 43. The process of claim 36, wherein the PCC product has a solids concentration of 15 to 50% solids by weight. 44. The process of claim 36, wherein the PCC product has a solids concentration of 20 to 30% solids by weight. 45. The process of claim 36, wherein the PCC product has a solids concentration of 23 to 26% solids by weight. 46. The process of claim 36, wherein the PCC product comprises agglomerates having a mean aggregate diameter of 1 to 5 μm. 47. The process of claim 36, wherein the PCC product comprises agglomerates having an average diameter of 2 μm. 48. The process of claim 36, wherein the PCC product has a fraction of fines below 2 μm of less than 20%. 49. The process of claim 36, wherein the PCC product has a fraction of fines below 2 μm of less than 15%. 50. The process of claim 36, wherein the PCC product has a specific surface area of 30 to 100 m2/g. 51. The process of claim 36, wherein the PCC product has a specific surface area of 50 to 80 m2/g.
연구과제 타임라인
LOADING...
LOADING...
LOADING...
LOADING...
LOADING...
이 특허에 인용된 특허 (9)
Fairchild George Henry ; Thatcher Richard Louis, Acicular calcite and aragonite calcium carbonate.
Fortier Steven M. ; Jackson William B. ; O'Rorke Peter B. ; Perez Ricardo ; Bryan David P., Method for the production of precipitated calcium carbonate having a selected crystal form, products produced thereby and their uses.
※ AI-Helper는 부적절한 답변을 할 수 있습니다.