Optimal high recovery, energy efficient dual fully integrated nanofiltration seawater reverse osmosis desalination process and equipment

• US 20060157409A1
• Filed: 01/14/2005
• Published: 07/20/2006
• Est. Priority Date: 01/14/2005
• Status: Abandoned Application

• Current Assignee: Saline Water Conversion Corporation
• Original Assignee: Saline Water Conversion Corporation
• Inventors: Hassan, Ata M.
• Application Number:
  US11/035,277
• Publication Number:
  US 20060157409A1
• Time in Patent Office: Days
• US Class Current: 210/637
• CPC Class Codes: B01D 2311/04 Specific process operations in the feed stream; Feed pretreatment
• CPC Class Codes: B01D 2311/25 Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
• CPC Class Codes: B01D 61/026 comprising multiple reverse osmosis steps
• CPC Class Codes: B01D 61/0271 comprising multiple nanofiltration steps
• CPC Class Codes: B01D 61/04 Feed pretreatment
• CPC Class Codes: C02F 1/44 by dialysis, osmosis or reverse osmosis general membrane separation processes B01D61/00, membrane modules B01D63/00, electrodialysis C02F1/4693, combination of membrane modules and bioreactors C02F3/1268
• CPC Class Codes: C02F 1/441 by reverse osmosis
• CPC Class Codes: C02F 1/442 by nanofiltration
• CPC Class Codes: C02F 2103/08 Seawater, e.g. for desalination
• CPC Class Codes: C02F 2301/08 Multistage treatments, e.g. repetition of the same process step under different conditions
• CPC Class Codes: C02F 2303/10 Energy recovery
• CPC Class Codes: C02F 5/00 Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents softening using ion-exchange C02F1/42
• CPC Class Codes: C02F 9/00 Multistage treatment of water, waste water or sewage
• CPC Class Codes: Y02A 20/131 Reverse-osmosis
• CPC Class Codes: Y02W 10/30 Wastewater or sewage treatment systems using renewable energies

Abstract

An optimal two stage NF₂ membrane pretreatment unit is synergistically combined with a following two stage SWRO₂ desalination unit, where each of the two stage NF₂ and SWRO₂ has an energy recovery device (ERD) turbocharger (TC) in between the stages to form a dual hybrid of NF₂-SWRO₂ (FIG. 1); alternatively the two stage NF₂ unit is synergistically combined with one stage ERD equipped SWRO, unit operated at up to 85 bar (FIG. 2a, b); or the two stage NF₂ unit combined with one stage ERD equipped SWRO₁ unit, with part of its reject recycled constituting part of the feed to the NF units (FIG. 3a,b). The process of this invention raises significantly the product water recovery ratio, producing SWRO hybrids that exceed all prior arts in efficiency, including water yield, product recovery ratio, dramatically reduces both the energy consumption and water production unit cost.

Claims

1-21. -21. (canceled)

22. An optimal seawater desalination process in which saline water, containing a high concentration of hardness scale forming ionic species, microorganisms, particulate matter and a high concentration of total dissolved solids, TDS, is passed under pressure through a two stage nanofiltration membrane, NF2, units to produce a first water product, NF permeate, and NF reject, wherein the said first water product having reduced content of said ionic species and from which is removed microorganisms, particulate matter and scale forming hardness ions, and thereafter passing said first water product through a seawater reverse osmosis, SWRO, membrane unit to produce from it a second water product, SWRO permeate, of potable quality and a third water product of SWRO unit reject, of increased salinity but of reduced scale forming hardness ions.

23. An optimal seawater desalination process as in claim 22, wherein said saline water comprises seawater, or a blend of seawater with part of third water product of SWRO unit reject.

24. An optimal seawater desalination process as in claim 23, wherein said seawater or blend has a total dissolved solids, TDS, content on the order of 1.0 to 5.2%.

25. An optimal seawater desalination process as in claim 23, wherein said seawater or blend has a cation content on the order of 1.2%-1.7%, an anion content on the order of 2.2%-2.8%, a pH on the order of 7.9-8.2, comparable to a total dissolved solids content on the order of 1.0%-5.2%.

26. An optimal seawater desalination process as in claim 25, wherein said cation content includes 700-2200 ppm of calcium and magnesium cations.

27. An optimal seawater desalination process as in claim 22, in which the two stage NF2 units comprise:

a one first stage NF unit consisting of one high pressure pump followed by an assembly of the first set of NF membrane modules arranged in parallel, wherein this first stage NF unit is linked through an energy recovery device, ERD, turbocharger, TC, unit to a second stage NF unit consisting of the ERT TC unit followed by a second set of NF membrane modules, also arranged in parallel, wherein the two stages form a completely, fully integrated NF2 units.

28. An optimal seawater desalination process as in claim 27, wherein an NF module comprises one pressure vessel, PV, fitted with four of NF elements arranged in series when using spiral wound, SW, NF membrane elements and one or more when using hollow fine fiber, HFF, NF membrane elements.

29. An optimal seawater desalination process as in claim 27, wherein the number of modules in the first NF stage unit and, therefore, the number of PVs and NF elements, are twice their number in the second NF stage unit.

30. An optimal seawater desalination process as in claim 27, wherein the second NF stage unit is arranged in series to the first stage NF unit.

31. An optimal seawater desalination process as in claim 27, wherein the combined product from the first and second NF stage units constitutes the first NF water product, while the combined reject from the various first stage NF membrane modules constitutes, in a brine staging process, the feed to the second stage NF unit, whose reject constitutes the final NF reject to be discharged.

32. An optimal seawater desalination process as in claim 27, wherein each NF membrane module in both the first and the second stage NF modules is characterized by having high rejection of SO₄^═

on the order of about 95% or better, and HCO₃⁻

ions on the order of 70% or better, moderate to high rejection of Ca⁺⁺, Mg⁺⁺ on the order of about 70% to 80% or better, respectively, and good TDS ions rejection on the order of 30-40% or better, but has a relatively good product, NF permeate, flow rate on the order of 6 m³/h or better of first water product from an 8 m³/h of seawater feed, for a 75% water product recovery ratio or better.

33. An optimal seawater desalination process as in claim 32, wherein the HCO₃⁻

ion content is further reduced to nearly nil by acid dosing of the first water product prior to its entry to the seawater reverse osmosis units.

34. An optimal seawater desalination process as in claim 27, wherein the turbocharger is capable of receiving high pressure feed, reject of first stage NF unit, which it boosts the said feed pressure to the second NF stage from about 24±

10 bar to about 32±

10 bar or higher.

35. An optimal seawater desalination process as in claim 27, wherein said two stage nanofiltration NF2 units are operated at a temperature on the order of 15-40°

C., while their total product water recovery ratio on the order of 75%, rising to about 80% when dosing antiscalant in the seawater feed.

36. An optimal seawater desalination process as in claim 22, wherein the saline water is passed to the two stage NF2 unit with or without dosing of the proper antiscalant.

37. An optimal seawater desalination process as in claim 22, wherein said seawater reverse osmosis, SWRO, membrane units comprise:

(a) two stage SWRO membrane, SWRO2, units, or

(b) one stage SWRO membrane unit, SWRO1, with or without recycling of part of the third water product, SWRO1 unit reject, to form with seawater a blend of saline water, which constitutes the feed to the NF2 units.

38. An optimal seawater desalination process as in claim 37, in which the two stage SWRO2 units comprise:

a one first stage SWRO unit consisting of one high pressure pump followed by an assembly of the first set of SWRO membrane modules arranged in parallel, wherein this first stage SWRO unit is linked and is completely, fully integrated with a second stage SWRO unit consisting of an ERD TC unit followed by the second set of SWRO membrane modules, also arranged in parallel.

39. An optimal seawater desalination process as in claim 38, wherein a SWRO module comprises one high pressure vessel, PV, fitted with four of spiral wound, SW, SWRO membrane elements arranged in series and one or more when using hollow fine fiber, HFF, SWRO membrane elements, also arranged in series.

40. An optimal seawater desalination process as in claim 38, wherein the number of modules in the first SWRO stage unit and therefore, the number of PVs and SWRO membrane elements are twice their number in the second SWRO stage unit.

41. An optimal seawater desalination process as in claim 38, wherein the second SWRO stage unit is arranged in series to the first stage SWRO unit.

42. An optimal seawater desalination process as in claim 38, wherein the combined product from the first and second SWRO stage units constitutes the second SWRO water product, while the combined reject from the various first stage SWRO membrane modules constitutes, in a brine staging process, the feed to the second stage SWRO unit, whose reject constitutes the third water product, SWRO unit reject, having increased salinity but drastically reduced scale forming hardness ions, especially SO₄^═

and HCO₃⁻

ions.

43. An optimal seawater desalination process as in claim 38, wherein the turbocharger is capable of receiving high pressure feed, reject of first stage SWRO unit, which it boosts the said feed pressure to the second SWRO stage from about 55±

10 bar to about 75±

10 bar or higher, wherein the modules in first and second stages SWRO can tolerate pressure on the order of 55±

10 bar to about 75±

10 bar, respectively.

44. An optimal seawater desalination process as in claim 38, wherein the said SWRO2 units are operated at a temperature on the order of 15-40°

C. and at product water recovery ratio on the order of 71% and 56%, respectively, with and without and with recycling of part of the SWRO2 reject to form with seawater a blend, which constitutes the feed to the NF2 units.

45. An optimal seawater desalination process as in claim 37, wherein the SWRO unit comprises one stage SWRO membrane, SWRO1, equipped with energy recovery device, ERD.

46. An optimal seawater desalination process as in claim 45, wherein the energy recovery device consists of ERD turbocharger, TC.

47. An optimal seawater desalination process as in claim 45, wherein the SWRO1 unit consists of a high pressure pump followed by a set of SWRO membrane modules arranged in parallel.

48. An optimal seawater desalination process as in claim 47, wherein each of the SWRO membrane modules consists of one high pressure vessel fitted with 6 SWRO spiral wound membrane elements arranged in series or fitted with one or two of SWRO hollow fine fiber membrane elements arranged in series.

49. An optimal seawater desalination process as in claim 45, wherein the SWRO unit, SWRO1, produces from the feed consisting of NF2 permeate a second water product of potable quality and a third water product of SWRO reject of increased salinity and low hardness content.

50. An optimal seawater desalination process as in claim 47, wherein the SWRO pump is operated on first water product feed at pressure 55±

10 bar.

51. An optimal seawater desalination process as in claim 46, wherein the ERT turbocharger is capable of receiving high pressure feed from the pump at 55±

10 bar and boosts it by the energy it recovers from SWRO1 reject to 75±

10 bar, wherein the SWRO1 modules can tolerate pressure on the order of 75±

10 bar or better.

52. An optimal seawater desalination process as in claim 47, wherein the SWRO 1 unit is operated at temperature on the order of 14-40°

C. and product water recovery ratio of 56% to 70%, respectively, with and without recycling of part of SWRO1 reject to form with seawater a blend, which constitutes the feed to the NF2 units.

53. An optimal seawater desalination process as in claim 45, wherein the ERD unit is a pressure exchanger, PX, one.

54. An optimal seawater desalination process as in claim 53, wherein the SWRO1 unit consists of a high pressure pump, an ERT PX unit linked and completely integrated with the following SWRO unit membrane modules arranged in parallel.

55. An optimal seawater desalination process as in claim 53, wherein each of the SWRO membrane modules, which are arranged in parallel, consists of one high pressure vessel fitted with 6 SWRO spiral wound membrane elements or fitted with one or two of SWRO hollow fine fiber membrane elements.

56. An optimal seawater desalination process as in claim 53, wherein the pressure booster pump split the NF2 permeate feed to SWRO1 into two streams:

first stream is passed at P=3±

1 bar to high pressure pump, while second stream is passed under same pressure of 3±

1 bar to the ERT PX unit.

57. An optimal seawater desalination process as in claim 56, wherein the said first stream equals in quantity to the product of SWRO1, while the said second stream quantity is on the order of the third water product, SWRO1 reject.

58. An optimal seawater desalination process as in claim 54, wherein the high pressure pump delivers the said first feed stream at pressure of 75±

10 bar to SWRO 1 unit after blending it prior to entry to SWRO1 unit with the said second stream delivered by the ERT PX unit and its following HP booster pump at the exact pressure value of the first steam of 75±

10 bar, wherein the SWRO1 modules can tolerate pressure on the order of 75±

10 bar or better.

59. An optimal seawater desalination process as in claim 55, wherein the ERD PX receives the SWRO1 reject and transfer the recovered energy from it to the second stream NF2 permeate feed to raise its pressure to about 73±

10 bar.

60. An optimal seawater desalination process as in claim 56, wherein the NF2 permeate blend, combining both the two said streams in one common feed, is passed at P=75±

10 bar to the SWRO1 unit to produce a second water product of potable quality and a third water product, SWRO1 reject, with high content of TDS ions and drastically reduced scale forming hardness ions.

61. An optimal seawater desalination process as in claim 53, wherein the SWRO unit is operated at temperature on the order of 14-40°

C. and product water recovery ratio on the order of 56% and 71%, respectively, with and without recycling of part of the SWRO1 reject to form with seawater a blend, which constitutes the feed to the NF2 units.