| 20130037479 | HOLLOW FIBER FORWARD OSMOSIS MEMBRANE - It is an object of the present invention to provide a hollow fiber forward osmosis membrane, which can enhance forward osmotic pressure energy acquired by permeation, and thus improve power generation efficiency in the forward osmotic pressure power generation, when dilution water such as freshwater permeates into seawater through the osmosis membrane. The relationship between optimal conditions for an inner diameter d and a length L of the hollow fiber osmosis membrane to be used for forward osmotic pressure power generation whereby dilution water such as fresh water is caused to permeate into non-concentrate seawater through the hollow fiber osmosis membrane to increase a flow rate on the side of the seawater using forward osmotic pressure energy thus generated, and power is generated using the increased flow rate, is expressed as equation (1) in the range of d=50 to 200 μm, L=0.5 to 2 m and J=1.7×10 | 02-14-2013 |
| 20150083656 | PROCESS OF SUPPLYING WATER OF CONTROLLED SALINITY - A process of producing an injection water stream of controlled salinity and controlled sulfate anion content that is suitable for injection into an oil bearing formation of an oil reservoir, the process comprising the steps of: (a) feeding a source water having a total dissolved solids content in the range of 20,000 to 45,000 ppm and a sulfate anion concentration in the range of 1,000 to 4,000 ppm, preferably, 1,500 ppm to 4,000 ppm to a desalination plant that comprises a plurality of reverse osmosis (RO) membrane units and a plurality of nanofiltration (NF) membrane units wherein the source water is pressurised to a pressure in the range of 350 to 1250 psi absolute, and dividing the source water to provide a feed water for the RO membrane units (hereinafter “RO feed water”) and a feed water for the NF membrane units (hereinafter “NF feed water”); (b) if necessary, increasing the pressure of the RO feed water to a value in the range of 900 to 1250 psi absolute before introducing the RO feed water to the RO membrane units and withdrawing an RO permeate and an RO retentate from the RO membrane units wherein the RO membrane units are operated in either a single-pass, single-stage mode or in a single-pass, two-stage mode and wherein the recovery of RO permeate is in the range of 35 to 75% by volume, preferably, 35 to 60% by volume based on the volume of the RO feed water that is fed to the RO membrane units such that the RO permeate has a total dissolved solids contents of less than 250 ppm, and a sulfate anion concentration of less than 3 ppm; (c) if necessary, reducing the pressure of the NF feed water to a value in the range of 350 to 450 psi absolute before introducing the NF feed water to the NF membrane units and withdrawing an NF permeate and an NF retentate from the NF membrane units wherein the NF membrane units are operated in a single-pass, single-stage mode and wherein the NF membrane units are operated with a recovery of NF permeate in the range of 35 to 60% by volume based on the volume of the NF feed water that is fed to the NF membrane units such that the NF permeate has a total dissolved solids content in the range of 15,000 to 40,000 ppm, preferably, 15,000 to 35,000 ppm, and a sulfate anion concentration of less than 40 ppm, preferably less than 30 ppm; and (d) mixing at least a portion of the RO permeate and at least a portion of the NF permeate in a ratio in the range of 2:1 to 40:1, preferably, 4:1 to 27:1, in particular, 10:1 to 25:1 to provide an injection water having a total dissolved solids content in the range of 500 to 5,000 ppm, and a sulfate anion concentration of less than 7.5 ppm, preferably, less than 5 ppm, more preferably less than 3 ppm. | 03-26-2015 |
