Methods of protein fractionation using high performance tangential flow filtration

• US 20050197496A1
• Filed: 02/04/2005
• Published: 09/08/2005
• Est. Priority Date: 03/04/2004
• Status: Abandoned Application

• Current Assignee: GTC Biotherapeutics, Inc.
• Original Assignee: GTC Biotherapeutics, Inc.
• Inventors: Perreault, Mark
• Application Number:
  US11/051,216
• Publication Number:
  US 20050197496A1
• Time in Patent Office: Days
• US Class Current: 530/412
• CPC Class Codes: B01D 2315/10 Cross-flow filtration
• CPC Class Codes: B01D 2315/16 Diafiltration
• CPC Class Codes: B01D 61/145 Ultrafiltration
• CPC Class Codes: B01D 61/147 Microfiltration
• CPC Class Codes: B01D 61/16 Feed pretreatment
• CPC Class Codes: B01D 61/58 Multistep processes
• CPC Class Codes: B01D 71/024 Oxides
• CPC Class Codes: C07K 1/34 by filtration, ultrafiltration or reverse osmosis
• CPC Class Codes: C07K 1/36 by a combination of two or more processes of different types

Abstract

Processes and apparati are provided for separating molecules of interest from a mixture containing them which comprises subjecting the mixture to an improved method of high performance tangential flow filtration (HPTFF). The HPTFF of the invention was used to clarify, and process various feedstreams for the removal of a molecule of interest based on both the size and charge of the molecule of interest. According to a preferred embodiment, a transgenic milk feedstream is stabilized and particulate matter such as fat, casein miscelles and bacteria are removed. The method of HPTFF used in the current invention utilizes optimized process parameters that include temperature, trans-membrane pressure, molecular charge, molecular size, cross-flow velocity, and milk concentration. Cleaning and storage procedures were also developed to ensure long membrane life. An aseptic filtration step was also developed to remove any bacteria remaining in a clarified transgenic milk feedstream.

Claims

1. A method for separating a protein of interest from a feedstream, comprising:

(a) filtering said feedstream by a high performance tangential-flow filtration process that separates said molecular species of interest from said feedstream on the basis of pore size and charge of said protein of interest, while maintaining flux at a level ranging from about 5 to 100% of transition point flux in the pressure-dependent region of the flux versus TMP curve, wherein transmembrane pressure is held substantially constant along the membrane at a level no greater than the transmembrane pressure at the transition point of the filtration, whereby said protein of interest is selectively separated from said feedstream such that said protein of interest retains its biological activity;

(b) filtering said feedstream by an ultrafiltration process; and

,

wherein said filtration is occurring above the transition point flux of said protein of interest;

wherein said molecular species has a molecular weight of between 1 and 1000 kDa.

2. The method of claim 1, further comprising fractionating said feedstream.

3. The method of claim 1, further comprising clarifying said feedstream.

4. The method of claim 1, further comprising diafiltering said feedstream.

5. The method of claim 1, further comprising increasing transmembrane pressure and decreasing flux for the first half of the filtration.

6. The method of claim 5, further comprising decreasing transmembrane pressure for the second half of the process.

7. The process of claim 1 wherein said feedstream is concentrated before filtration.

8. The process of claim 1 wherein said protein of interest is less than ten times larger or smaller in molecular weight than a second protein of interest in said feedstream.

9. The process of claim 1 wherein the protein of interest is more than ten times larger or smaller in molecular weight than a second protein of interest of the mixture but have the same charge or isoelectric point.

10. The method of claim 1, further comprising concentrating said feedstream.

11. The method of claim 1, wherein all filtration stages are ultrafiltrations.

12. The method of claim 1, wherein said feedstream is milk

13. The method of claim 1, wherein said feedstream is a cell lysate solution.

14. The method of claim 1, wherein said protein is a biopharmaceutical.

15. The method of claim 12, wherein the condition of said milk is selected from one of the following states:

a) raw;

b) diluted;

c) treated with a buffer solution;

d) chemically treated; and

e) partially evaporated.

16. The method of claim 2, wherein said fractionation step utilizes ceramic filtration membranes.

17. The method of claim 3, wherein said clarification step utilizes ceramic filtration membranes.

18. The method of claim 2, wherein said fractionation step utilizes polymeric filtration membranes with a defined isoelectric profile.

19. The method of claim 3, wherein said clarification step utilizes polymeric filtration membranes.

20. The method of claim 2, wherein said fractionation step utilizes cellulose filtration membranes.

21. The method of claim 3, wherein said clarification step utilizes cellulose filtration membranes.

22. The method of claim 2, further comprising optimizing systematic parameters.

23. The method of claim 22, wherein said systematic parameters include temperature, feedstream flow velocity, transmembrane pressure, feedstream concentration and diafiltration volume.

24. The method of claim 3, further comprising optimizing systematic parameters.

25. The method of claim 24, wherein said systematic parameters include temperature, feedstream flow velocity, transmembrane pressure, feedstream concentration and diafiltration volume.

26. The method of claim 1 wherein said molecular species of interest are biological entities selected from the group consisting of proteins, immunoglobulins, polypeptides, peptides, glycoproteins, RNA and DNA.

27. The method of claim 23, wherein the optimal temperature range is from 15°

C. to 50°

C.

28. The method of claim 23, wherein the optimal temperature range is from 20°

C. to 35°

C.

29. The method of claim 23, wherein the optimal temperature range is from 25°

C. to 29°

C.

30. The method of claim 25, wherein the optimal temperature range is from 15°

C. to 50°

C.

31. The method of claim 25, wherein the optimal temperature range is from 20°

C. to 35°

C.

32. The method of claim 25, wherein the optimal temperature range is from 25°

C. to 29°

C.

33. The method of claim 23, wherein the feedstream flow velocity is from 10 cm/sec to 100 cm/sec.

34. The method of claim 23, wherein the feedstream flow velocity is from 20 cm/sec to 60 cm/sec.

35. The method of claim 23, wherein the feedstream flow velocity is from 25 cm/sec to 45 cm/sec.

36. The method of claim 25, wherein the feedstream flow velocity is from 10 cm/sec to 100 cm/sec.

37. The method of claim 25, wherein the feedstream flow velocity is from 20 cm/sec to 60 cm/sec.

38. The method of claim 25, wherein the feedstream flow velocity is from 25 cm/sec to 45 cm/sec.

39. The method of claim 23, wherein the transmembrane pressure ranges from 2 psi to 40 psi.

40. The method of claim 23, wherein the transmembrane pressure ranges from 5 psi to 30 psi.

41. The method of claim 23, wherein the transmembrane pressure ranges from 10 psi to 20 psi.

42. The method of claim 25, wherein the transmembrane pressure ranges from 2 psi to 40 psi.

43. The method of claim 25, wherein the transmembrane pressure ranges from 5 psi to 30 psi.

44. The method of claim 25, wherein the transmembrane pressure ranges from 10 psi to 20 psi.

45. The method of claim 23, wherein the feedstream concentration is from 0.25×

to 4×

natural milk.

46. The method of claim 23, wherein the feedstream concentration is from 0.5×

to 3×

natural milk.

47. The method of claim 23, wherein the feedstream concentration is from 1.0×

to 2×

natural milk.

48. The method of claim 25, wherein the feedstream concentration is from 0.25×

to 4×

natural milk.

49. The method of claim 25, wherein the feedstream concentration is from 0.5×

to 3×

natural milk.

50. The method of claim 25, wherein the feedstream concentration is from 1.0×

to 2×

natural milk.

51. The method of claim 23, wherein the diafiltration volume range is from 1×

to 20×

the volume of concentrated MF retentate.

52. The method of claim 23, wherein the diafiltration volume range is from 3×

to 15×

the volume of concentrated MF retentate.

53. The method of claim 23, wherein the diafiltration volume range is from 5×

to 10×

the volume of concentrated MF retentate.

54. The method of claim 25, wherein the diafiltration volume range is from 1×

to 20×

the volume of concentrated MF retentate.

55. The method of claim 25, wherein the diafiltration volume range is from 3×

to 15×

the volume of concentrated MF retentate.

56. The method of claim 25, wherein the diafiltration volume range is from 5×

to 10×

X the volume of concentrated MF retentate.

57. The method of claim 2, wherein ultrafiltration membranes are used for all filtering steps.

58. The method of claim 7, wherein ultrafiltration membranes are used for all filtering steps.

59. The method of claim 12, wherein said milk is treated with a solution selected from the group consisting of:

a) water;

b) a buffered aqueous salt solution;

c) chelating agent;

d) acid solution; and

e) alkali solution.

60. The method of claim 4, wherein said diafiltration utilizes ultrafiltration permeate.

61. The method of claim 4, wherein said diafiltration utilizes water.

62. The method of claim 4, wherein said diafiltration utilizes a buffered salt solution.

63. The method of claim 1, wherein the membranes used are cleaned with solutions of a temperature greater than 20°

C.

64. The method of claim 1, wherein the membranes used are cleaned with solutions ranging in temperature from 20°

C. to 70°

C.

65. The method of claim 1, wherein the membranes used are cleaned with solutions ranging in temperature from 40°

C. to 60°

C.

66. The method of claim 1, wherein the membranes used are cleaned with an acid solution.

67. The method of claim 1, wherein the membranes used are cleaned with an alkali solution.

68. The method of claim 1, wherein the membranes used are cleaned with a hypochlorite solution.

69. The method of claim 66, 67 or 68, further comprising a water rinse following the use of the selected solution.

70. The method of claim 1, wherein the membranes used are sanitized prior to use with a hydroxide solution.

71. The method of claim 1, wherein the membranes used are sanitized prior to use with an alcohol solution.

72. The method of claim 1, wherein the membranes used are sanitized prior to use with a hypochlorite solution.

73. The method of claim 1, wherein the membranes used are cleaned for a period of from 20 minutes to 45 minutes.

74. The method of claim 1, further comprising filtering the filtrate from the filtration in a second tangential-flow filtration stage through a membrane having a smaller pore size than the membrane used in the first filtration stage, and recycling the filtrate of this second filtration stages back to the first filtration stage, whereby the process is repeated.

76. The methods of claim 1 or 75 wherein said protein of interest is recombinant human alphafetoprotein.

77. The methods of claim 1 or 75 wherein said protein of interest is recombinant human albumin.

78. The methods of claim 1 or 75 wherein said protein of interest is sourced from the milk of a transgenic mammal.

75. A method for separating a protein of interest from a feedstream, comprising:

(a) filtering said feedstream by a high performance tangential-flow filtration process that separates said molecular species of interest from said feedstream on the basis of pore size and charge of said protein of interest, while maintaining flux at a level ranging from about 5 to 100% of transition point flux in the pressure-dependent region of the flux versus TMP curve, wherein transmembrane pressure is held substantially constant along the membrane at a level no greater than the transmembrane pressure at the transition point of the filtration, whereby said protein of interest is selectively separated from said feedstream such that said protein of interest retains its biological activity;

(b) filtering said feedstream by a microfiltration process; and

,

(c) increasing transmembrane pressure and decreasing flux for the first half of the filtration;

(d) decreasing therafter increasing or maintaining flux as the filtration progresses.

wherein said filtration is occurring above the transition point flux of said protein of interest;

wherein said molecular species has a molecular weight of between 1 and 1000 kDa.