A process for conditioning of wastewater treatment brines for deep well injection during recovery of heavy hydrocarbon oils in situ. High pressure steam is used to mobilize oil, which is recovered in a mixture of oil and produced water. The produced water is pre-treated by removing residual oil. The
A process for conditioning of wastewater treatment brines for deep well injection during recovery of heavy hydrocarbon oils in situ. High pressure steam is used to mobilize oil, which is recovered in a mixture of oil and produced water. The produced water is pre-treated by removing residual oil. The remaining water is acidified and steam stripped to remove non-hydroxide alkalinity and non-condensable gases, and is then fed to a crystallizing evaporator, where it is evaporated from a circulating brine slurry to produce (1) a distillate stream having a trace amount of residual solutes, and (2) evaporator blowdown stream containing, as dissolved or suspended solids, substantially all of the solutes from the produced water feed. The distillate stream is used as boiler feedwater, either directly or after polishing. The evaporator blowdown is conditioned to remove substantially all suspended solids and to produce a clear brine solution for deep well injection.
대표청구항▼
The invention claimed is: 1. A process to recover heavy hydrocarbon oil by in situ dissolution of at least a portion of a first geological formation containing quantities of heavy hydrocarbon oil, comprising: injecting steam into the first geological formation to heat the heavy hydrocarbon oils in
The invention claimed is: 1. A process to recover heavy hydrocarbon oil by in situ dissolution of at least a portion of a first geological formation containing quantities of heavy hydrocarbon oil, comprising: injecting steam into the first geological formation to heat the heavy hydrocarbon oils in the first geological formation and to mobilize least a portion of said heavy hydrocarbon oils in the first geological formation, to produce a mixture of oil and produced water, wherein said produced water comprises condensate from said steam; separating oil from said mixture of oil and produced water to provide (i) an oil product, and (ii) a produced water composition comprising water and oil; de-oiling said produced water composition to at least partially provide an evaporator feedwater stream, said evaporator feedwater stream comprising water, dissolved gases, and dissolved solutes, said dissolved solutes comprising calcium, sulfate, and silica; providing a crystallizing evaporator having a plurality of heat transfer elements, a liquid containing sump reservoir, and a recirculating pump to recycle liquid from said liquid containing sump reservoir into a heat transfer relationship with said plurality of heat transfer elements; seeding said liquid containing sump reservoir with a selected quantity of calcium sulfate seed crystals, and forming a circulating brine comprising a slurry of water and calcium sulfate seed crystals, wherein said slurry is maintained at a preselected concentration for preferential precipitation of said calcium, said sulfate, and said silica in said evaporator feedwater stream to said calcium sulfate seed crystals rather than to said heat transfer surfaces of said crystallizing evaporator; feeding the evaporator feedwater stream to the crystallizing evaporator, and producing (i) a distillate stream, and (ii) a concentrated blowdown brine slurry stream comprising water, dissolved solids, said dissolved solids comprising silica, and suspended solids, said suspended solids comprising calcium sulfate and silica; feeding said distillate stream to a boiler, and producing steam for injection into said first geological formation; removing said suspended solids from said concentrated blowdown brine slurry stream to produce a substantially suspended solids free clear brine liquor. 2. The process as set forth in claim 1, further comprising injecting said substantially solids free clear brine liquor into a second geological formation, thereby providing disposal of said substantially solids free clear brine liquor. 3. The process as set forth in claim 1, further comprising diluting said substantially suspended solids free clear brine liquor with an aqueous diluent to produce a clear brine solution, said clear brine solution comprising water and dissolved solids, said dissolved solids comprising silica at a level of at about 10% or more below the level of silica in said substantially solids free clear brine liquor; and injecting said clear brine solution into a second geological formation, thereby providing disposal of said clear brine solution. 4. The process as set forth in claim 1, further comprising diluting said substantially suspended solids free clear brine liquor with an aqueous diluent to produce a clear brine solution, said clear brine solution comprising water and dissolved solids, said dissolved solids comprising silica at a level of at about 20% or more below the level of silica in said substantially solids free clear brine liquor; and injecting said clear brine solution into a second geological formation, thereby providing disposal of said clear brine solution. 5. The process as set forth in claim 1, further comprising diluting said substantially suspended solids free clear brine liquor with an aqueous diluent to produce a clear brine solution, said clear brine solution comprising water and dissolved solids, said dissolved solids comprising silica at a level of at about 25% or more below the level of silica in said substantially solids free clear brine liquor; and injecting said clear brine solution into a second geological formation, thereby providing disposal of said clear brine solution. 6. The process as set forth in claim 1, further comprising diluting said substantially suspended solids free clear brine liquor with an aqueous diluent to produce a clear brine solution, said clear brine solution comprising water and dissolved solids, said dissolved solids comprising silica at a level of at about 30% or more below the level of silica in said substantially solids free clear brine liquor; and injecting said clear brine solution into a second geological formation, thereby providing disposal of said clear brine solution. 7. A process to recover heavy hydrocarbon oil by in situ dissolution of at least a portion of a first geological formation containing quantities of heavy hydrocarbon oil, comprising: injecting steam into the first geological formation to heat the heavy hydrocarbon oils in the first geological formation and to mobilize least a portion of said heavy hydrocarbon oils in the first geological formation, to produce a mixture of oil and produced water, wherein said produced water comprises condensate from said steam; separating oil from said mixture of oil and produced water to provide (i) an oil product, and (ii) a produced water composition comprising water and oil; de-oiling said produced water composition to at least partially provide an evaporator feedwater stream, said evaporator feedwater stream comprising water, dissolved gases, and dissolved solutes, said dissolved solutes comprising calcium, sulfate, and silica; providing a crystallizing evaporator having a plurality of heat transfer elements, a liquid containing sump reservoir, and a recirculating pump to recycle liquid from said liquid containing sump reservoir into a heat transfer relationship with said plurality of heat transfer elements; seeding said liquid containing sump reservoir with a selected quantity of calcium sulfate seed crystals, and forming a circulating brine comprising a slurry of water and calcium sulfate seed crystals, wherein said slurry is maintained at a preselected concentration for preferential precipitation of said calcium, said sulfate, and said silica in said evaporator feedwater stream to said calcium sulfate seed crystals rather than to said heat transfer surfaces of said crystallizing evaporator; feeding the evaporator feedwater stream to the crystallizing evaporator, and producing (i) a distillate stream, and (ii) a concentrated blowdown brine slurry stream comprising water, dissolved solids, said dissolved solids comprising one or more scale forming species, and suspended solids, said suspended solids comprising calcium sulfate and silica; feeding said distillate stream to a boiler, and producing steam for injection into said first geological formation; removing said suspended solids from said concentrated blowdown brine slurry stream to produce a substantially suspended solids free clear brine liquor; diluting said substantially suspended solids free clear brine liquor with an aqueous diluent to produce a clear brine solution, said clear brine solution comprising water and dissolved solids, said dissolved solids comprising scale forming species at a level of at about 10% or more below the level of said one or more scale forming species in said substantially solids free clear brine liquor; and injecting said clear brine solution into a second geological formation, thereby providing disposal of said clear brine solution. 8. The process as set forth in claim 7, wherein said one or more scale forming species comprises silica. 9. The process as set forth in claim 7, wherein said one or more scale forming species comprises calcium. 10. The process as set forth in claim 7, wherein said one or more scale forming species comprises barium. 11. The process as set forth in claim 7, wherein said one or more scale forming species comprises strontium. 12. The process as set forth in claim 7, wherein said one or more scale forming species comprises sulfate. 13. The process as set forth in claim 7, wherein said dissolved solids comprising one or more scale forming species are present in said clear brine solution at a level of at about 20% or more below the level of said scale forming species in said substantially solids free clear brine liquor. 14. The process as set forth in claim 7, wherein said dissolved solids comprising one or more scale forming species are present in said clear brine solution at a level of at about 25% or more below the level of said scale forming species in said substantially solids free clear brine liquor. 15. The process as set forth in claim 7, wherein said dissolved solids comprising one or more scale forming species are present in said clear brine solution at a level of at about 30% or more below the level of said scale forming species in said substantially solids free clear brine liquor. 16. A process for treatment of waste brines produced during steam generation operations associated with the recovery of heavy hydrocarbon oil by in situ dissolution of at least a portion of a first geological formation containing quantities of heavy hydrocarbon oil, said process comprising: injecting steam into the first geological formation to heat the heavy hydrocarbon oils in the first geological formation and to mobilize least a portion of said hydrocarbon oils in the first geological formation, to produce a mixture of oil and produced water, wherein said produced water comprises condensate from said steam; separating oil from said mixture of oil and produced water to provide (i) an oil product, and (ii) a produced water composition comprising water and oil; de-oiling said produced water composition to at least partially provide an evaporator feedwater stream, said evaporator feedwater stream comprising water, dissolved gases, and dissolved solutes, said dissolved solutes comprising calcium, sulfate, and silica; providing a crystallizing vapor recompression evaporator having a plurality of heat transfer elements, a liquid containing sump reservoir, and a recirculating pump to recycle liquid from said liquid containing sump reservoir into a heat transfer relationship with said plurality of heat transfer elements; seeding said liquid containing sump reservoir with a selected quantity of calcium sulfate seed crystals, and forming a circulating brine comprising a slurry of water and calcium sulfate seed crystals, wherein said slurry is maintained at a preselected concentration for preferential precipitation of said calcium, said sulfate, and said silica to said calcium sulfate seed crystals rather than to said heat transfer surfaces of said crystallizing evaporator; acidifying said evaporator feedwater stream, to convert non-hydroxide alkalinity to carbon dioxide; steam stripping said acidified evaporator feedwater stream, and removing said non-condensable gases and said carbon dioxide; feeding the acidified and steam stripped evaporator feedwater stream to the crystallizing evaporator, and producing (i) a distillate stream, and (ii) a concentrated blowdown brine slurry stream comprising water, dissolved solids, and suspended solids, said suspended solids comprising calcium sulfate and silica; feeding at least some of said distillate stream to a boiler, and producing high pressure steam for injection into said first geologic formation; removing said suspended solids from said concentrated blowdown brine slurry stream to produce a substantially suspended solids free clear brine liquor; diluting said substantially suspended solids free clear brine liquor with at least a portion of said distillate stream to produce a clear brine solution, said clear brine solution comprising water and dissolved solids, said dissolved solids comprising silica at a level of below the level of silica in said clear brine solution; injecting said clear brine solution into a second geological formation, thereby providing disposal of said clear brine solution. 17. The process as set forth in claim 3, or in claim 7, or in claim 16, wherein said substantially suspended solids free clear brine liquor comprises about 200 parts per million or more of silica, as SiO2 and wherein said clear brine solution comprises about 180 ppm or less of silica. 18. The process as set forth in claim 4, or in claim 7, or in claim 16, wherein said substantially suspended solids free clear brine liquor comprises about 200 parts per million or more of silica, as SiO2 and wherein said clear brine solution comprises about 160 ppm or less of silica. 19. The process as set forth in claim 5, or in claim 7, or in claim 16, wherein said substantially suspended solids free clear brine liquor comprises about 200 parts per million or more of silica, as SiO2 and wherein said clear brine solution comprises about 150 ppm or less of silica. 20. The process as set forth in claim 6, or in claim 7, or in claim 16, wherein said substantially suspended solids free clear brine liquor comprises about 200 parts per million or more of silica, as SiO2 and wherein said clear brine solution comprises about 140 ppm or less of silica. 21. The process as set forth in claim 1, or claim 7, or claim 16, wherein removal of said suspended solids from said concentrated blowdown brine slurry stream to produce said substantially suspended solids free clear brine liquor comprises centrifuging said concentrated blowdown brine slurry stream. 22. The process as set forth in claim 1, or claim 7, or claim 16, wherein removal of said suspended solids from said concentrated blowdown brine slurry stream to produce said substantially suspended solids free clear brine liquor comprises filtering said concentrated blowdown brine slurry stream in a filter press. 23. The process as set forth in claim 22, wherein said filter comprises a pressure filter. 24. The process as set forth in claim 1, or claim 7, or claim 16, wherein removal of said suspended solids from said concentrated blowdown brine slurry stream to produce said substantially suspended solids free clear brine liquor comprises processing said concentrated blowdown brine slurry in a clarifier, to settle solids from said concentrated blowdown brine slurry stream. 25. The process as set forth in claim 1, or claim 7, or claim 16, wherein removal of said suspended solids from said concentrated blowdown brine slurry stream to produce said substantially suspended solids free clear brine liquor comprises processing said concentrated blowdown brine slurry in one or more hydrocyclones, to settle solids from said concentrated blowdown brine slurry stream. 26. The process as set forth in claim 1, or claim 7, or claim 16, wherein said evaporator is a falling-film evaporator. 27. The process as set forth in claim 1, or claim 7, or claim 16, wherein said evaporator is a forced-circulation evaporator. 28. The process as set forth in claim 26, wherein said heat transfer elements are tubular elements having an interior surface and an exterior surface. 29. The process as set forth in claim 28, wherein said evaporator feedwater stream is concentrated at the interior surface of said tubular heat transfer elements. 30. The process as set forth in claim 1, or claim 7, or claim 16, wherein said evaporator comprises a mechanical vapor recompression evaporator. 31. The process as set forth in claim 1, or claim 7, or claim 16, further comprising removing oil from said evaporator feedwater stream to a selected oil concentration before injecting said evaporator feedwater stream into said evaporator. 32. The process as set forth in claim 31, wherein the selected concentration of oil in said evaporator feedwater stream comprises less than about twenty parts per million. 33. The process as set forth in claim 1, or claim 7, or claim 16, wherein said boiler comprises a packaged boiler. 34. The process as set forth in claim 33, wherein said packaged boiler comprises a water tube boiler. 35. The process as set forth in claim 1, or claim 7, or claim 16, wherein said boiler comprises a once-through steam generator. 36. The process as set forth in claim 35, further comprising, after generating steam in said once through steam generator, separating steam and liquid, to produce a steam stream having substantially 100% steam quality. 37. The process as set forth in claim 36, wherein said 100% steam quality steam stream is injected into said first geological formation. 38. The process as set forth in claim 36, wherein separating said steam and said liquid comprises producing a liquid stream containing dissolved solutes, and wherein said liquid stream is flashed at least once to produce a still further concentrated residual liquid containing dissolved solutes. 39. The process as set forth in claim 38, further comprising adding said residual liquid stream containing dissolved solutes to said evaporator feedwater stream. 40. The process as set forth in claim 1, or claim 7, or claim 16, wherein said distillate stream comprises water and non-volatile solutes, said non-volatile salutes present in the range of from about zero to about 20 parts per million. 41. The process as set forth in claim 1, or claim 7, or claim 16, further comprising acidification of said evaporator feedwater stream, to convert non-hydroxide alkalinity to carbon dioxide. 42. The process as set forth in claim 41, further comprising steam stripping said acidified evaporator feedwater stream, and removing said non-condensable gases and said carbon dioxide. 43. The process as set forth in claim 1, or claim 7, or claim 16, wherein said distillate stream comprises about 95% or more by volume of said evaporator feedwater stream, 44. The process as set forth in claim 43, wherein said concentrated blowdown brine slurry stream comprising about 5% or less by volume of said evaporator feedwater stream. 45. The process as set forth in claim 1, or claim 7, or claim 16, wherein producing steam in a boiler comprises generating a steam stream at about 100% quality and at about 1000 pounds per square inch pressure or more from said distillate stream, and wherein said steam stream comprises at least about 70% by weight of said distillate stream. 46. The process as set forth in claim 45, wherein said steam stream comprises at least 95% by weight of said distillate stream. 47. The process as set forth in claim 45, wherein said steam stream comprises at least 98% by weight of said distillate stream. 48. The process as set forth in claim 7, or in claim 16, wherein said aqueous diluent comprises a portion of said distillate stream from said crystallizing evaporator. 49. The process as set forth in claim 7, or in claim 16, wherein said aqueous diluent comprises service water. 50. The process as set forth in claim 7, or in claim 16, wherein diluting said substantially suspended solids free clear brine liquor with at least a portion of said distillate stream to produce a clear brine solution comprises mixing a portion of said distillate stream with said substantially suspended solids free clear brine liquor at a ratio of about 50% by volume of portions from said distillate stream and of said substantially suspended solids free clear brine liquor.
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