초록 ▼

Methane is formed into synthesis gas through a combination of a partial oxidation reaction and a steam reforming reaction. Oxygen for the partial oxidation reaction is obtained by contacting air with an oxygen transport membrane and recovering the oxygen transported through the membrane. To increase

Methane is formed into synthesis gas through a combination of a partial oxidation reaction and a steam reforming reaction. Oxygen for the partial oxidation reaction is obtained by contacting air with an oxygen transport membrane and recovering the oxygen transported through the membrane. To increase the oxygen flux through the membrane, steam is utilized as a sweep gas on the anode side of the membrane. The steam reduces the oxygen partial pressure on the anode side increasing the flux. The efficiency and cost benefit of the process is enhanced by utilizing in-line combustors to heat gases being delivered to the oxygen transport membrane. Membrane integrity is enhanced by conducting the reactions in a reactor that is remote from the oxygen transport membrane.

대표청구항 ▼

Methane is formed into synthesis gas through a combination of a partial oxidation reaction and a steam reforming reaction. Oxygen for the partial oxidation reaction is obtained by contacting air with an oxygen transport membrane and recovering the oxygen transported through the membrane. To increase

Methane is formed into synthesis gas through a combination of a partial oxidation reaction and a steam reforming reaction. Oxygen for the partial oxidation reaction is obtained by contacting air with an oxygen transport membrane and recovering the oxygen transported through the membrane. To increase the oxygen flux through the membrane, steam is utilized as a sweep gas on the anode side of the membrane. The steam reduces the oxygen partial pressure on the anode side increasing the flux. The efficiency and cost benefit of the process is enhanced by utilizing in-line combustors to heat gases being delivered to the oxygen transport membrane. Membrane integrity is enhanced by conducting the reactions in a reactor that is remote from the oxygen transport membrane. 2, wherein said single unit operation comprises a weak acid cation ion-exchange system. 4. The process as set forth in claim 3, wherein said feedwater stream contains contains more hardness than alkalinity, further comprising, before feeding said feedwater to said weak acid cation exchange system, the step of adjusting the ratio of hardness to alkalinity by adding a base to said feedwater, so as to raise the alkalinity of said feedwater. 5. The process as set forth in claim 3, wherein said feedwater stream contains more alkalinity than hardness, further comprising, before feeding said feedwater to said week acid cation exchange system, the step of addition of acid to said feedwater, so as to destroy the excess alkalinity in said feedwater. 6. The process as set forth in claim 1 or claim 2, wherein in step (c), pH is raised to at least about 10. 7. A process for treatment of a feedwater stream in membrane separation equipment, said membrane separation equipment comprising at least one unit having a membrane separator, to produce a low solute containing product stream and a high solute containing reject stream, said process comprising: (a) providing a feedwater stream containing solutes therein, said solutes comprising (i) hardness, (ii) alkalinity, and (iii) at least one molecular species which is sparingly ionized when in neutral or near neutral pH aqueous solution, said at least one molecular species comprising one or more of (1) at least some TOC, or (2) at least some silica, or (3) at least some boron; (b) concentrating said feedwater stream in a first unit of said membrane separation equipment after effectively eliminating the tendency of said feedwater to form scale when said feedwater is concentrated to a preselected concentration factor at a selected pH, by effecting, in any order, two or more of the following: (i) removing hardness from said feedwater stream (ii)removing substantially all non-hydroxide alkalinity from said feedwater stream; (iii) removing dissolved gases, whether initiallly present or created during said hardness or said alkalinity removal step; (c) raising the pH of the product from step (a) to a selected pH of at least about 8.5 by adding a selected base thereto, to urge said at least one molecular species which is sparingly ionized when in neutral or near neutral pH aqueous solution toward increased ionization; (d) passing the product from step (c) above through said membrane separation equipment to produce a reject stream and a product stream, said membrane separation equipment substantially resisting passage of dissolved species therethrough, to concentrate said feedwater to said preselected concentration factor, to produce (i) a high solute containing reject stream, and (ii) a low solute containing permeate product stream, and (iii) wherein TOC in said product stream is less than five percent (5%) of said at least some TOC in said feedwater. 8. The process according to claim 1 or claim 7, wherein said membrane separation equipment comprises a reverse osmosis equipment. 9. The process according to claim 8, wherein said reverse osmosis equipment comprises two reverse osmosis units operated in series with respect to said product stream. 10. The process as set forth in claim 9, further comprising the step of treating said product stream in a continuous electrodeionization unit to produce a purified water stream. 11. The process as set forth in claim 10, further comprising the step of purifying said purified water stream from said continuous electrodeionization unit in an ultraviolet sterilization unit. 12. The process as set forth in claim 11, further comprising the step of purifying the product stream from said ultraviolet sterilization unit in a final sub-micron filter to produce an ultrapure water product. 13. The process as set forth in claim 12, wherein said ultrapure water product meets or exceeds a 18.2 megohm resistivity quality standard. 14. The process as set for th in claim 10, further comprising the step of treating said purified water stream in a mixed bed ion-exchange system. 15. The process according to claim 8, further comprising the step of passing said product stream from said, reverse osmosis equipment through at least a primary mixed bed ion-exchange unit. 16. The process according to claim 15, wherein said said primary mixed bed ion-exchange unit is regenerated for reuse in said process. 17. The process according to claim 15, further comprising (1) the step of providing a secondary mixed bed ion exchang unit downstream of said primary mixed bed ion exchange unit, and (2) the step of controlling said primary mixed bed ion-exchange unit to a preselected leakage rate with respect to one or more of (a) silica (b) boron, or (c) TOC, and thereupon, discarding media resin of said primary mixed bed ion-exchange unit, and substituting therefor the media of said secondary mixed bed ion-exchange unit. 18. The apparatus as set forth in claim 9, further comprising, downstream of the second reverse osmosis membrane unit, at least one mixed bed ion-exchange unit to process the product stream from said second reverse osmosis unit. 19. The process as set forth claim 8, wherein said reverse osmosis equipment comprises a thin-film composite membrane. 20. The process as set forth in claim 8 or in claim 9, wherein after said reverse osmosis equipment, said product stream is further treated in a cation exchange unit. 21. The process according to claim 20, further comprising the step of passing said product stream from said cation exchange unit through at least one anion exhange unit. 22. The process according to claim 1 or claim 2, wherein the step of raising the pH is accomplished by addition of a base in a softener to simultaneously raise pH while precipitating hardness from said feedwater. 23. The process according to claim 22, wherein the step of removing hardness is partially is accomplished by sodium zeolite cation exchange. 24. The process according to claim 1 or claim 7, wherein the step of raising, the pH is accomplished in part by decarbonation of said feedwater stream. 25. The process according to claim 1 or claim 7, wherein said feedwater comprises boiler blowdown. 26. The process of claim 1 or claim 7, wherein said product stream of said process comprises a TOC content of less than about one percent (1%) of the TOC content of said feedwater stream. 27. The process of claim 1 or claim 7, wherein said product stream of said process comprises a TOC content of about zero point four percent (0.4%), or less, of the TOC content of said feedwater stream. 28. The process of claim 1 or claim 7, wherein said product stream of said process comprises a TOC content of about zero point three four percent (0.34%), or less, of the TOC content of said feedwater stream. 29. The process as set forth in claim 1, or in claim 7, the additional step of removing substantially all non-hydroxide alkalinity not associated with hardness. 30. The process as set forth in claim 1 or claim 7, further comprising the step of adding acid before the step of removing dissolved gas, to effect conversion of alkalinity to carbon dioxide. 31. The process according to claim 1 or claim 7, wherein said feedwater comprises cooling tower blowdown. 32. The process according to claim 1 or claim 7, wherein said feedwater comprises ash pond water. 33. The process according to claim 1 or claim 7, wherein said feedwater comprises ash sluicing water. 34. The process according to claim 1 or claim 7, wherein said feedwater comprises effluent from sewage treatment. 35. The process according to claim 1 or claim 7, wherein said feedwater comprises effluent from pulping or papermaking operations. 36. The process according to claim 1 or claim 7, wherein said feedwater comprises effluent from oil refining operations.