High speed manufacturing process for precipitated calcium carbonate employing sequential perssure carbonation

• US 6,251,356 B1
• Filed: 07/21/1999
• Issued: 06/26/2001
• Est. Priority Date: 07/21/1999
• Status: Expired due to Term

• Current Assignee: Pacific Nano Products, Inc.
• Original Assignee: G.R. International, Inc.
• Inventors: Mathur, Vijay K.
• Primary Examiner(s): HENDRICKSON, STUART L
• Application Number:
  US09/358,759
• Time in Patent Office: 706 Days
• Field of Search: 423/430, 423/432
• US Class Current: 423/432
• CPC Class Codes: C01F 11/181 Preparation of calcium carbonate by carbonation of aqueous solutions and characterised by control of the carbonation conditions
• CPC Class Codes: C01P 2004/03 obtained by SEM
• CPC Class Codes: C01P 2004/30 extending in three dimensions
• CPC Class Codes: C01P 2004/39 parallelepiped-like
• CPC Class Codes: C01P 2006/12 Surface area
• CPC Class Codes: C01P 2006/60 Optical properties, e.g. expressed in CIELAB-values
• CPC Class Codes: D21H 17/675 Oxides, hydroxides or carbonates

Abstract

A process for the production of precipitated calcium carbonate. A slurry of calcium hydroxide is agitated in a pressurized reactor, and carbon dioxide is provided under pressure to the reactor to produce precipitated calcium carbonate at a high reaction rate. Carbon dioxide is utilized at a high efficiency. Solubilized calcium ions and carbonate ions react to produce a calcium carbonate precipitate. Control of process conditions such as temperature, slurry concentration, and pressure, enables production of a desired crystal habit (including sclenohedral, rhombohedral, stacked rombohedral, or aragonite crystal structures), crystal size, or crystal aspect ratio. The precipitated calcium carbonate produced by the process under pressure is useful as either a paper filler or as an ingredient in paper coatings, and provides a paper product with improved preselected properties, which properties include opacity, density, and/or brightness.

Claims

1. A method for the production of precipitated calcium carbonate, said method comprising:

(a) providing a source of calcium ions;

(b) mixing said source of calcium ions with a solvent to create a slurry, said slurry comprising (i) an undissolved portion of said source of calcium ions, and (ii) a solution comprising calcium ions;

(c) feeding said slurry to a reactor;

(d) bubbling a gas stream comprising carbon dioxide through said slurry while maintaining said reactor at a pressure above atmospheric pressure, to produce carbonate ions from said carbon dioxide, and then reacting said carbonate ions with said calcium ions to form a calcium carbonate precipitate;

(e) agitating the contents of said reactor,

(f) wherein the acts of creation of said slurry and reaction of said slurry are performed sequentially, and

(g) wherein the time required for the act of reacting said slurry is approximately the same as the time required for act of creating said slurry.

2. The process as set forth in claim 1, wherein said solvent comprises water.

3. The process as set forth in claim 2, wherein said reactor is provided with an instrument to measure pH of said slurry during said step (d), and wherein the step of bubbling a gas comprising carbon dioxide through said reactor is continued until the pH of said slurry ranges from about 6.5 to about 7.5.

4. The process as set forth in claim 3, wherein during operation of said process, one or more process or product variables is selected for control of said process, and wherein each of said one or more said variable is selected from the group consisting of (a) calcium carbonate product surface area, as measured by the Blaine method, (b) carbon dioxide utilization efficiency, (c) production rate of calcium carbonate as measured by the conversion rate of calcium hydroxide slurry, in grams of calcium hydroxide consumed per liter per minute, and (d) crystal habit.

5. The process as set forth in claim 2, wherein said slurry comprises calcium oxide.

6. The process as set forth in claim 2, wherein said slurry comprises calcium hydroxide.

7. The process as set forth in claim 6, wherein said slurry comprises from about 32 grams per liter of calcium hydroxide to about 308 grams per liter of calcium hydroxide, expressed as calcium carbonate.

8. The process as set forth in claim 6, wherein said slurry comprises from about 200 grams per liter of calcium hydroxide to about 250 grams per liter of calcium hydroxide, expressed as calcium carbonate.

9. The process as set forth in claim 2, wherein said reaction step (d) is carried out isothermally at about 50 degrees F., and wherein said precipitated calcium carbonate comprises a rhombohedral PCC crystal habit having an aspect ratio of about 1:

1.5.

10. The process as set forth in claim 9, wherein at the start of said reaction step (d), said slurry comprises about 116 grams per liter of calcium hydroxide.

11. The process as set forth in claim 9, wherein during said reaction step (d), said reactor pressure is maintained at about 70 psig.

12. The process as set forth in claim 2, wherein said reaction step (d) is carried out at about 68 degrees F., and wherein said precipitated calcium carbonate comprises a rhombohedral PCC crystal habit having an aspect ratio of about 1:

1.

13. The process as set forth in claim 12, wherein at the start of said reaction step (d), said slurry comprises about 87 grams per liter of calcium hydroxide.

14. The process as set forth in claim 12, wherein during said reaction step (d), said reactor pressure is maintained at about 20 psig.

15. The process as set forth in claim 2, wherein said reaction step (d) is carried out with a starting slurry temperature of about 73 degrees F., and wherein said precipitated calcium carbonate comprises a stacked rhombohedral PCC crystal habit.

16. The process as set forth in claim 15, wherein at the start of said reaction step (d), said slurry comprises about 32 grams per liter of calcium hydroxide.

17. The process as set forth in claim 15, wherein during said reaction step (d), said reactor pressure is maintained at about 70 psig.

18. The process as set forth in claim 2, wherein said reaction step (d) is carried out with a starting slurry temperature of about 100°

F., and wherein said precipitated calcium carbonate comprises a scalenohedral PCC crystal habit.

19. The process as set forth in claim 18, wherein at the start of said reaction step (d), said slurry comprises about 246 grams per liter of calcium hydroxide.

20. The process as set forth in claim 18, wherein during said reaction step (d), said reactor pressure is maintained at about 30 psig.

21. The process as set forth in claim 2, wherein said reaction step (d) is carried out with a starting slurry temperature of about 120°

F., and wherein said precipitated calcium carbonate comprises an aragonite crystal habit.

22. The process as set forth in claim 21, wherein at the start of said reaction step (d), said slurry comprises about 229 grams per liter of calcium hydroxide.

23. The process as set forth in claim 21, wherein during said reaction step (d), said reactor pressure is maintained at about 70 psig.

24. The process as set forth in claim 2, wherein said step (b), comprises slaking of lime and is carried out in a slaker, and wherein said step (d), comprises carbonation and is carried out in a pressurized reactor, and wherein said slaker and said pressurized reactor are matched, capacity throughput wise, so that said reactor and said slaker are each sequentially utilized for efficient optimization of equipment.

25. The process as set forth in claim 24, wherein said slaker and said pressurized reactor are matched, capacity wise, so that said slaker and said pressurized reactor are engaged in substantially continuous operations.

26. The process as set forth in claim 2, wherein said slurry, at time of feed to said reactor, has a pH in excess of 12.

27. The process as set forth in claim 2, wherein said reactor is provided with an instrument to measure pH of said slurry during said step (d), and wherein the step of bubbling a gas comprising carbon dioxide through said reactor is continued until said slurry pH reaches about 7.0.

28. The process as set forth in claim 1, wherein said source of calcium ion is selected from the group consisting of calcium oxide and calcium hydroxide.

29. The process as set forth in claim 3, wherein said solution comprising calcium ions comprises partially solubilized calcium hydroxide.

30. The process as set forth in claim 1, wherein the step of creating said slurry comprises slaking lime.

31. The process as set forth in claim 1, wherein the step of reacting said slurry comprises carbonation of said soluble calcium ions.

32. The process as set forth in claim 1, wherein during said step (d), solute from said slurry is dissolved to maintain the concentration of calcium ions at or near the solubility limit of said solute in said solvent, until the supply of calcium ions is substantially converted to calcium carbonate.

33. The process as set forth in claim 1, wherein said process further comprises thoroughly mixing said slurry by mechanically agitating said slurry.

34. The process as set forth in claim 1, wherein the pressure in said reactor maintained at a pre-selected level, based on a process or product variable selected for optimization.

35. The process as set forth in claim 1, wherein the partial pressure of carbon dioxide during said step (d) is maintained in excess of 0.2 atmospheres.

36. The process as set forth in claim 1, wherein the partial pressure of carbon dioxide during said step (d) is maintained between 0.2 atmospheres and 1.0 atmospheres.

37. The process as set forth in claim 1, wherein the partial pressure of carbon dioxide during said step (d) is maintained at approximately 0.4 atmospheres.

38. The process as set forth in claim 1, wherein the pressure in said reactor during reaction of said slurry is maintained at least above 5 psig.

39. The process as set forth in claim 1, wherein the pressure in said reactor during reaction of said slurry is maintained between about 5 psig and about 70 psig.

40. The process as set forth in claim 1, wherein the pressure in said reactor during reaction of said slurry is maintained at above atmospheric pressure but not more than about 30 psig.

41. The process as set forth in claim 1, wherein the pressure in said reactor during reaction of said slurry is maintained at about 30 psig.

42. The process as set forth in claim 1, wherein said gas stream comprises from about 5 percent carbon dioxide by volume to about 100 percent carbon dioxide by volume.

43. The process as set forth in claim 1, wherein said gas stream comprises from about 10 percent to about 25 percent carbon dioxide by volume.

44. The process as set forth in claim 1, wherein said gas stream comprises about 20 percent carbon dioxide by volume.

45. The process as set forth in claim 1, wherein said gas stream comprises 10 percent or less carbon dioxide by volume.

46. The process as set forth in claim 1, wherein said gas stream comprises between 5 percent and 10 percent carbon dioxide by volume.

47. The process as set forth in claim 1, wherein said reactor further comprises an agitator, and wherein said process further comprises the step of thoroughly mixing said slurry and said gas stream during said reaction step (d).

48. The process as set forth in claim 47, wherein the step of thoroughly mixing said slurry and said gas stream is performed with a mechanical agitator.

49. The process as set forth in claim 47, wherein the step of thoroughly mixing said slurry and said gas stream is performed with a mechanical agitator operating at a rotational speed between 500 revolutions per minute and 1500 revolutions per minute.

50. The process as set forth in claim 47, wherein the step of thoroughly mixing said slurry and said gas stream is performed with a mechanical agitator having a tip speed of between 260 feet per minute and 764 feet per minute.

51. The process as set forth in claim 1, wherein reaction of said slurry is carried out at the rate of formation of calcium carbonate in excess of 0.50 grams per liter per minute.

52. The process as set forth in claim 1, wherein said reaction of said slurry is carried out at the rate of formation of calcium carbonate of from about 0.5 to about 10 grams per liter per minute.

53. The process as set forth in claim 1, wherein said reaction of said slurry is carried out at the rate of formation of calcium carbonate of from about 5 to about 6 grams per liter per minute.

54. The process as set forth in claim 1, wherein said reaction of said slurry is carried out at the rate of formation of calcium carbonate in excess of about 10 grams per liter per minute.

55. The process as set forth in claim 1, wherein said gas stream containing carbon dioxide is provided to said reactor at the rate of from about 0.4 to about 4.0 liters per minute, based on said gas stream at atmospheric pressure, based on a 20% by volume carbon dioxide concentration in said gas stream.

56. The process as set forth in claim 1, wherein said gas stream containing carbon dioxide is provided to said reactor at the rate of about 2 liters per minute, based on said gas stream at atmospheric pressure, based on a 20% by volume carbon dioxide concentration in said gas stream.

57. The process as set forth in claim 1, wherein the step (d) is carried out at a temperature of from about 50°

F. to about 120°

F.

58. The process as set forth in claim 1, wherein the step (d) is carried out at a temperature of from about 75°

F. to about 105°

F.

59. The process as set forth in claim 1, wherein the step (d) is carried out at a temperature of about 100°

F.

60. The process as set forth in claim 1, wherein said precipitated calcium carbonate has an average specific surface area, as measured by the Blaine method, from between about 15,000 cm²/gram, to about 60,000 cm 2/gram.

61. The process as set forth in claim 1, wherein said precipitated calcium carbonate has an average specific surface area, as measured by the Blaine method, less than about 15,000 cm²/gram.

62. The process as set forth in claim 1, wherein said precipitated calcium carbonate has an average specific surface area, as measured by the Blaine method, more than about 60,000 cm²/gram.

63. The process as set forth in claim 1, wherein said gas stream comprises carbon dioxide in a flue gas from combustion of a hydrocarbon fuel.

64. The process as set forth in claim 1, wherein said gas stream comprises carbon dioxide in a gas from the thermal decomposition of lime mud.

65. The process as set forth in claim 1, wherein said carbon dioxide in said gas stream is utilized at an efficiency of at least 90 percent.

66. The process as set forth in claim 65, wherein said carbon dioxide in said gas stream is utilized at an efficiency of at least 95 percent.

67. The process as set forth in claim 1, wherein said carbon dioxide in said gas stream is utilized at an efficiency of at least 99 percent.

68. The process as set forth in claim 1, further comprising between said step of creating said slurry and said step of charging said reactor with said slurry, the step of cooling said slurry.

69. The process as set forth in claim 1, further comprising the step of providing a PCC storage tank, and wherein a carbon dioxide gas stream is bubbled through said PCC storage tank.

70. The process as set forth in claim 1, further characterized in that said reactor is sized less than 200 gallons capacity per ton per day of PCC output.

71. The process as set forth in claim 70, further characterized in that said reactor is sized less than 100 gallons capacity per ton per day of PCC output.

72. The process as set forth in claim 70, further characterized in that said reactor is sized less than 50 gallons capacity per ton per day of PCC output.