WO2009029653A1 - Procédé pour éliminer la silice lors de la récupération de pétrole lourd - Google Patents

Procédé pour éliminer la silice lors de la récupération de pétrole lourd Download PDF

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Publication number
WO2009029653A1
WO2009029653A1 PCT/US2008/074442 US2008074442W WO2009029653A1 WO 2009029653 A1 WO2009029653 A1 WO 2009029653A1 US 2008074442 W US2008074442 W US 2008074442W WO 2009029653 A1 WO2009029653 A1 WO 2009029653A1
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WO
WIPO (PCT)
Prior art keywords
stream
brine
concentrated
produced water
evaporator
Prior art date
Application number
PCT/US2008/074442
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English (en)
Inventor
Keith R Minnich
Dan Peterson
Original Assignee
Hpd, Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hpd, Llc filed Critical Hpd, Llc
Priority to RU2010111793/03A priority Critical patent/RU2479713C2/ru
Priority to CN200880113363.9A priority patent/CN101835954B/zh
Priority to BRPI0815845-2A priority patent/BRPI0815845B1/pt
Priority to CA2640421A priority patent/CA2640421C/fr
Publication of WO2009029653A1 publication Critical patent/WO2009029653A1/fr

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Classifications

    • E—FIXED CONSTRUCTIONS
    • E21—EARTH DRILLING; MINING
    • E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
    • E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH DRILLING; MINING
    • E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/34—Arrangements for separating materials produced by the well

Definitions

  • the present invention relates to a process for recovering heavy oil, and more particularly, to an oil recovery process that utilizes a mechanical vapor compression evaporation system to treat produced water.
  • Enhanced Oil Recovery processes employ thermal methods to improve the recovery of heavy oils from sub-surface reservoirs.
  • the injection of steam into heavy oil bearing formations is a widely practiced enhanced oil recovery method.
  • several tons of steam are required for each ton of oil recovered.
  • Steam heats the oil in the reservoir, which reduces the viscosity of the oil and allows the oil to flow to a collection well.
  • Steam condenses and mixes with the oil, the condensed steam being called produced water.
  • the mixture of oil and produced water that 5950-054
  • Oil is separated from the produced water by conventional processes employed in conventional oil recovery operations.
  • Treating the produced water to prepare feed water for steam generation is challenging. It is known to chemically treat the produced water and subject the produced water to an evaporation process to form distillate for steam generation feed water. In particular, it is known to use an evaporator and mechanical vapor compressor to produce the distillate.
  • the produced water typically contains significant amounts of silica-based compounds. These silica-based compounds will tend to foul evaporator and other process surfaces by scaling or deposition of silica on the surfaces. These scales reduce the conductivity of heat transfer elements in 5950-054
  • the equipment and thus reduce the efficiency of evaporation and steam generation.
  • the pH of the feed to the evaporator is conventionally raised to maintain the solubility of silica.
  • the higher pH promotes the precipitation of hardness components, calcium and magnesium. This creates the potential for hardness scaling of the evaporator heat transfer surfaces if not controlled.
  • the scaling threat from hardness can be reduced by chemical addition in the form of a dispersant.
  • the dispersant suspends the particles so that they do not stick and foul evaporator surfaces. At this time, it does not appear that it has been determined how much hardness can be controlled using a dispersant since few existing heavy oil recovery operating systems have very low hardness in the produced water. However, it is anticipated that in future heavy oil recovery processes that the produced water will include higher brackish water makeup and that the concentration of hardness in the produced water 5950-054
  • the present invention relates to a process for cleaning and purifying produced water generated in recovering heavy oil from oil-bearing formations.
  • the process includes evaporation of the produced water and forming a sorption slurry to prevent silica scaling of the evaporator surfaces.
  • the sorption slurry may be formed by adding compounds, which react to form sorption suspended solids, or by sorption suspended solids, to the produced water.
  • the suspended solids form a slurry of 5950-054
  • Evaporator distillate forms a purified water suitable for steam generation which produces steam for injection into the oil-bearing formation.
  • Evaporator distillate forms a purified water suitable for steam generation which produces steam for injection into the oil-bearing formation.
  • an oil/water mixture is recovered from an oil well. Thereafter, oil is separated from the oil/water mixture to produce an oil product and produced water having a contaminant such as dissolved silica, hardness, or residual oil.
  • a metal compound such as magnesium oxide or magnesium chloride, or any of a variety of metal oxide compounds, or alum is mixed with the produced water. When magnesium oxide or magnesium chloride is mixed with the produced water, magnesium hydroxide is formed.
  • the method includes co- precipitating the magnesium hydroxide and silica. Thereafter, the produced water having the precipitated silica is directed to an evaporator which produces steam and a concentrated brine.
  • the method or process further includes condensing the steam to form a distillate and directing the distillate to a steam generator and heating the distillate in the steam generator to produce steam. Thereafter, the steam is injected into an injection well, giving rise to the formation of the oil/water mixture.
  • an oil/water mixture is recovered from an oil well. Thereafter, oil is separated from the oil/water mixture to produce an oil product and produced water having a contaminant such as dissolved silica, hardness, or residual oil.
  • a compound such as an oxide or complex oxide of Ti, Al, or Si is mixed with the produced water. These surface properties of these compounds are such that most of the silica is removed from solution. Thereafter, the produced water having the only a small amount of soluble silica is directed to an evaporator which produces steam and a concentrated brine.
  • the method or process further includes condensing the steam to form a distillate and directing the distillate to a steam 5950-054
  • Figure 1 is a schematic representation of the basic processes for a heavy oil recovery process according to the present invention.
  • Figure 2 is a schematic illustration of a heavy oil recovery process utilizing a crystallization reactor for removing contaminants such as silica from a produced water stream prior to the produced water stream reaching one or more evaporators.
  • Figure 3 is a schematic illustrating a process similar to that shown in Figure 2 but wherein only one membrane is associated with the evaporators.
  • Figure 4 is a schematic illustration of a heavy oil recovery process including a crystallization process for treating a portion of the concentrated brine being circulated about an evaporator.
  • FIG. 5 is a schematic illustration of a heavy oil recovery process similar to that illustrated in Figure 4 but wherein there is provided a membrane, such as a ceramic membrane, downstream from the crystallization reactor or zone.
  • a membrane such as a ceramic membrane
  • the present invention entails a heavy oil recovery process wherein produced water is purified using a sorption slurry with an evaporation process. 5950-054
  • Distillate from the evaporation process forms feed water for use in generating steam for injecting into heavy-oil bearing underground formations.
  • the sorption slurry prevents scaling of the evaporator heat transfer surfaces by silica compounds and in some embodiments by silica and hardness compounds in the produced water thus maintaining evaporator efficiency.
  • Heavy oil recovery utilizes the heat released from condensing steam to release oil from oil-bearing deposits.
  • the resulting oil-water mixture is collected and pumped to the surface where the oil is separated from the mixture leaving what is called produced water.
  • the produced water is re-used to generate steam to feed back into the oil-bearing formation.
  • the present invention is directed, then, at methods of treating the produced water using a sorption slurry and evaporation to form steam generation feed water, thus re-cycling a major portion of the water used in the process of heavy oil recovery.
  • Produced water includes dissolved inorganic ions, dissolved organic compounds, suspended inorganic and organic solids, and dissolved gases.
  • the total suspended solids in produced water can vary. Typically the suspended solids in produced water is less than about 100 ppm, and in some cases the suspended solids in produced water range from about 100 ppm to about 150 ppm.
  • produced water from heavy oil recovery processes includes dissolved organic and inorganic solids in varying proportions.
  • the dissolved solids, including hardness and in particular silica-based compounds, in the produced water have the potential to foul the evaporation equipment by scaling the heat transfer surfaces. Additional treatment is therefore desirable after oil-water separation to remove silica-based compounds from the produced water before evaporation. 5950-054
  • silica will be used to refer generally to silica-based compounds.
  • the evaporation process may be accomplished using any of a variety of evaporators, including but not limited to mechanical vapor recompression evaporators, multiple effect evaporators, and falling film evaporators.
  • the heat transfer surfaces of the evaporator can be a plate-type or tubular-type and can be horizontal or vertical, with evaporation occurring on either side of these surfaces.
  • Various pre-treatment processes are generally employed to assure the efficiency and effectiveness of the evaporation process.
  • the invention includes a sorption slurry to prevent silica scaling in the equipment.
  • Produced water is directed from an oil-water separation step to a pre-heating step followed by de-aeration, sorption compound addition, evaporation and steam generation. Preheating and de-aeration are not required but are optional. Steam from the steam generation step is directed to the oil-bearing formation where the steam condenses releasing heat to free oil from the formation. A resulting oil-water mixture is then collected and pumped to the oil-water separation step, completing the water cycle of the heavy oil recovery process.
  • oil-water separation, pre-heating, de-aeration, and steam generation may each be accomplished by methods known to those of ordinary skill in the art.
  • Oil-water separation may, for example, be accomplished by using gravity separation.
  • Pre-heating the produced water enhances the efficiency of 5950-054
  • dissolved CO 2 removal in subsequent de-aeration may be accomplished by using a heat exchanger to recover heat from one or more waste streams or from a distillate stream. Removal of dissolved CO 2 prior to evaporation is sometimes employed to avoid accumulation of CO 2 in the shell of the evaporator. Such CO 2 accumulation can blanket off a portion of the evaporator heat exchange area and adversely affect evaporation capacity. De-aeration can serve to remove oxygen to reduce corrosion in the evaporator. Steam generation may be accomplished by the use of boilers or various forms of steam generators.
  • the present invention prevents or reduces hardness and silica-based scaling of the evaporator heat transfer surfaces. Scaling is prevented by adding chemicals which comprise fine suspended solids to form a sorption slurry in the recirculating brine of the evaporation process. The suspended solids form crystals, and the crystals provide preferential sorption sites for silica. Silica sorbs to the sorption slurry and is thus pulled out of solution onto the crystals rather than precipitating on the heat transfer surfaces of the evaporator. Scaling of the evaporator surfaces is thus reduced or prevented, thereby preserving the efficiency of the evaporation process.
  • the evaporation step converts at least 90% of the produced water to a produced vapor which condenses to form a distillate.
  • the distillate forms the feed water for steam generation equipment. That portion of the produced water that is not vaporized is known as concentrate or brine.
  • the sorption slurry forms a part of the concentrate or brine.
  • the concentrate or brine is recirculated in the evaporator. Substantially all of the solids in the evaporator feed water remain with the concentrate.
  • a bleed or evaporator blowdown stream from the recirculation loop wastes a portion of recirculating concentrate or brine to maintain a selected brine 5950-054
  • the evaporator blowdown stream can be converted into a solid in a zero liquid discharge system (ZLD) or disposed in an injection well.
  • ZLD zero liquid discharge system
  • the compound may be added to the produced water before entering the evaporator or to the recirculating brine loop in the evaporator.
  • the material added to the evaporator may be an oxide such as magnesium oxide, calcium oxide, calcium hydroxide, or other metal oxides such as aluminum oxide or iron oxide.
  • the material added to form the sorption slurry can be a metal compound such as magnesium chloride.
  • the material added to form the sorption slurry can be alum.
  • the material can be a compound such as an oxide or complex oxide of Ti, Al, or Si, which have particular surface properties.
  • the addition of the material results in a sorption slurry in the recirculating brine loop of the evaporator.
  • the sorption slurry comprises preferential sorption sites such that silica in the produced water preferentially sorbs or co-precipitates with the crystals rather than forming scale deposits on the evaporator heat transfer surfaces.
  • magnesium oxide is added to maintain a weight ratio of between about 0.5:1 and 3:1 of magnesium to silica in the produced water or brine.
  • the ratio of magnesium (Mg) to silica (SiO 2 ) is about 1.0.
  • magnesium oxide reacts with the water to form magnesium hydroxide crystals. Magnesium oxide will raise the pH of the produced water.
  • the magnesium hydroxide crystal sizes range typically from about 0.5 to about 10 ⁇ .
  • the pH of the concentrate or brine should be at least 9.2 and preferably in the range of 10.2-11.2. The elevated pH due to having added magnesium oxide reduces the solubility of 5950-054
  • the material is also added to maintain a weight ratio of between about 0.5:1 and 3:1 of calcium to silica in the produced water.
  • the calcium oxide or calcium hydroxide reacts with the produced water to form a slurry of calcium carbonate crystals.
  • the sizes of the calcium carbonate crystals range from about 5 to about 20 microns.
  • the pH of the concentrate or brine should be at least 9.5 and preferably in the range of 10.2-11.2.
  • a chemical such as soda ash or sodium hydroxide or some mixture of the chemicals is added to adjust the pH to promote precipitation of calcium carbonate crystals. Typically, about 90% of the silica is sorbed and co- precipitated with the calcium carbonate crystals.
  • the material is also added to maintain a weight ratio of between about 0.5:1 and 5:1 of metal to silica in the produced water.
  • the surface properties of the compounds are such that silica is removed from solution.
  • the sizes of the suspended solids range from about 5 to about 100 microns.
  • the pH of the concentrate or brine should be at least 9.5 and preferably in the range of 10.2-11.2.
  • a chemical such as soda ash or sodium hydroxide or some mixture of the chemicals 5950-054
  • FIG. 2 illustrates a method of treating produced water where the method utilizes the sorption slurry process described above in combination with a pair of evaporators and a pair of membranes.
  • evaporators 110, 112 there is provided two evaporators 110, 112 generally interposed between the crystallization reactor and boiler or steam generator.
  • Each evaporator 110, 1 12 includes a brine recirculation line 114, 1 16. Further, the evaporators 110, 1 12 include distillate outlet lines 1 18, 120.
  • the evaporators 1 10, 1 12 in conventional fashion produce steam which is condensed to form distillate which in turn is directed from the evaporators 110, 1 12 via outlet lines 118 and 120.
  • Distillate outlet lines 1 18 and 120 are communicatively connected to a steam generator feed line 40 which in turn directs the distillate produced by the evaporators 110, 112 to the steam generator.
  • Ceramic membrane 130 is interposed between evaporators 110 and 1 12 while ceramic membrane 132 is disposed downstream from evaporator 112.
  • a brine feed line 122 extends from brine circulation line 1 14 to ceramic membrane 130.
  • Brine feed line 124 extends from brine recirculation line 116 to ceramic membrane 132.
  • a return line 140 directs a reject stream from one or both of the ceramic membranes 5950-054
  • a portion of the concentrated brine being recirculated in lines 1 14 and 1 16 is directed to membranes 130 and 132.
  • Membranes 130 and 132 each produce a reject stream and a permeate stream.
  • the permeate stream of ceramic membrane 130 is directed to evaporator 112 while the permeate stream of ceramic membrane 132 is wasted or directed to other points in the process for further purification.
  • Return line 140 is split into segments 140A and 140B. Segment 140A returns the reject stream to the evaporator 110. That is, segment 140A returns the reject to the evaporator 110 or to a point upstream of the evaporator and downstream from the crystallization zone or reactor.
  • Segment 140B returns the reject to the crystallization zone or reactor.
  • the return can be directed to the crystallization zone or to a point upstream of the crystallization zone and preferably downstream from the oil/water separation unit.
  • the solids concentration in the return line 140 can be monitored and once the solids concentration in the return line reaches a threshold, portions of the reject stream can be directed into a waste stream 28 which leads to a dewatering process.
  • the dewatering process as shown in Figure 2 produces a concentrated waste stream 60 and a less concentrated stream 29 that is recycled to a point in the process upstream from the crystallization zone. In some cases, it may be preferable to only recycle the reject stream from the first ceramic membrane 130.
  • the reject stream 142 from ceramic membrane 132 can be wasted or directed to other points or areas in the process.
  • a metal compound such as magnesium oxide or magnesium chloride is mixed with the produced water in the crystallization reactor.
  • this results in the formation of magnesium hydroxide which co-precipitates with silica in the produced water. That is, the silica is sorbed to the magnesium hydroxide crystals that are precipitated in the crystallization reactor.
  • the precipitated silica eventually ends up in the brine recirculating in brine recirculation line 1 14.
  • Substantial portions of the precipitated silica are removed by the first ceramic membrane 130. Residual soluble silica in the permeate from membrane 130 will eventually end up in the brine being circulated in line 116. Brine from line 116 is filtered by the second ceramic membrane 132 and hence, the reject stream of the second membrane may also include precipitated silica as well as other suspended solids.
  • the reject stream from the ceramic membrane 130 is recycled via lines 140 and 140A to evaporator 1 10 or to a point upstream of the evaporator 1 10.
  • some of the reject stream can be recycled to the crystallization reactor or to a point upstream of the crystallization reactor via line 140B.
  • the membranes 130, 132 function as separation devices.
  • the membranes are ceramic membranes.
  • these separation devices could be in the form of other types of membranes or even other types of filters or separating devices such as a hydrocyclone.
  • the retention time in the crystallization reactor can vary. In one embodiment, the retention time is approximately ten to approximately forty minutes and during this time, the produced water and the crystallization reagent or reagents are mixed thoroughly. Also, in these process embodiments, the pH of the produced water can vary but under typical conditions, could vary between a pH of about 9.2 to a pH of about 10.5, and in one preferable process the pH of the produced water could vary from about 9.7 to about 10.0. In cases where the crystallization reagent is magnesium oxide or magnesium chloride, for example, the ratio of magnesium to SiO 2 is about 0.5 to 3.0 and preferably about 1.0 as ppm Mg to ppm SiO 2 .
  • the quantity of reject recirculated in the processes shown in Figures 2 and 3 can vary. In one exemplary process, approximately 60% of the reject can be recirculated to upstream points. It is postulated that a preferable recirculation rate will be approximately 20% to 40%. 5950-054
  • FIG 4 another sorption slurry process is shown therein.
  • This sorption slurry process is utilized in conjunction with an evaporator.
  • the crystallization reactor is disposed downstream of the evaporator 202 and in particular is located in a side stream 210 that connects to a brine recirculation line 206. That is, as viewed in Figure 4, produced water resulting from oil/water separation is directed through line 204 to the evaporator 202.
  • Evaporator 202 produces steam which is condensed and directed as a distillate through line 208 to a steam generator.
  • evaporator 202 produces a concentrated brine that is continuously recirculated through the evaporator in recirculation line 206.
  • Side stream 210 connects to recirculation line 206 and functions to direct a portion of the brine being circulated in line 206 to the crystallization reactor.
  • a crystalizing reagent such as magnesium oxide or magnesium chloride along with a caustic such as sodium hydroxide is added and mixed with the brine.
  • various reagents can be mixed with the concentrated brine to precipitate various contaminants such as silica from the concentrated brine.
  • various compounds such as magnesium oxide, magnesium chloride, calcium oxide, aluminum oxide, ferric oxide and other precipitants can be added to cause contaminants to precipitate.
  • magnesium hydroxide is formed and co-precipitates with silica, substantially reducing the concentration of dissolved silica in the brine.
  • the brine including precipitated silica is directed from the crystallization reactor through side stream 210. Some of the brine with the precipitated silica can be wasted via line 218.
  • Process variables discussed above such as retention time, pH, etc., can vary from process to process. Generally, 5950-054
  • this sorption slurry process is similar to the process shown in Figure 4 except that membrane 214 is provided in the side stream 210 downstream from the crystallization reactor.
  • the concentrated brine with precipitated silica is directed to a membrane 214 such as a ceramic membrane.
  • Membrane 214 produces a reject stream that is directed from the membrane via line 216.
  • Reject in line 216 can be selectively wasted through line 216C or can be returned to either or both segments 216A or 216B.
  • the reject stream 216 is concentrated with suspended solids and all of the reject stream or a portion thereof can be returned to the inlet side of the membrane 214. All or a portion of the same reject can be returned to the crystallization reactor so as to increase the concentration of suspended solids in the crystallization reactor.
  • a pilot scale test was performed on a produced water sample. The objective of the test was to determine scaling tendency. Dosages of magnesium oxide and sodium hydroxide were mixed with the produced water to simulate the sorption slurry process. The test was performed at a recovery of approximately 97%, meaning that the mass per unit of time of the distillate produced by the single evaporator used was approximately 97% of the mass per unit time of the produced water feed to the evaporator 202.
  • the pilot testing was performed using a single tube falling film evaporator comprising a vapor body, a falling film heat exchanger, brine recirculation pump with variable speed drive, surface condenser for process vapors, steam and process condensate receivers, feed tank, and a feed pump with a variable speed drive. 5950-054
  • the feed used for the pilot test was a produced water sample.
  • An analysis of the produced water sample is provided in Table 1 below. Table 1.
  • the pilot evaporator was pre-slurried with both magnesium oxide and sodium hydroxide. The resulting slurry contained 1.3 percent magnesium as Mg(OH) 2 . A portion of this mixture was used to charge the pilot evaporator. [0045] The pilot test was conducted over a time period of about 340 hours and during that time the heat transfer coefficient for the falling film heat exchange varied 5950-054
  • directing or “direct” used herein to describe a material or flow being directed to a part of a process encompasses both direct and indirect.
  • directing at least a portion of the brine stream to the second evaporator means that the brine stream is directed either directly or indirectly to the second evaporator.

Abstract

L'invention concerne un procédé pour récupérer du pétrole, lequel procédé comprend la récupération d'un mélange pétrole/eau à partir d'un puits de pétrole. Ensuite, le procédé comprend la séparation du pétrole du mélange pétrole/eau pour produire un produit pétrolier et de l'eau produite ayant de la silice dissoute dans celle-ci. L'eau produite est adressée à un évaporateur et produit de la vapeur et une saumure concentrée. Le procédé consiste à mélanger un agent de précipitation ou un réactif de cristallisation avec l'eau produite ou la saumure concentrée et à amener la silice de l'eau produite ou de la saumure concentrée à précipiter. La vapeur produite par l'évaporateur est amenée à se condenser pour former un distillat qui est adressé au générateur de vapeur. Au niveau du générateur de vapeur, le distillat est chauffé pour produire de la vapeur qui est injectée dans un puits d'injection, provoquant la création du mélange pétrole/eau.
PCT/US2008/074442 2007-08-27 2008-08-27 Procédé pour éliminer la silice lors de la récupération de pétrole lourd WO2009029653A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
RU2010111793/03A RU2479713C2 (ru) 2007-08-27 2008-08-27 Способ удаления оксида кремния при извлечении тяжелой нефти (варианты)
CN200880113363.9A CN101835954B (zh) 2007-08-27 2008-08-27 用于在重油回收中移除硅石的工艺
BRPI0815845-2A BRPI0815845B1 (pt) 2007-08-27 2008-08-27 Método para recuperar petróleo a partir de um poço de petróleo.
CA2640421A CA2640421C (fr) 2008-08-27 2008-10-06 Procede d'elimination de la silice dans la recuperation du petrole lourd

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US96818007P 2007-08-27 2007-08-27
US60/968,180 2007-08-27

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WO2009029653A1 true WO2009029653A1 (fr) 2009-03-05

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CN (1) CN101835954B (fr)
BR (1) BRPI0815845B1 (fr)
RU (1) RU2479713C2 (fr)
WO (1) WO2009029653A1 (fr)

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WO2011083421A1 (fr) 2010-01-06 2011-07-14 Total S.A. Procede de traitement d'eau et de production de vapeur et installation de production de vapeur
WO2013142764A3 (fr) * 2012-03-22 2014-07-24 E. I. Du Pont De Nemours And Company Traitement d'eau produite en récupération d'huile
GB2510159A (en) * 2013-01-27 2014-07-30 Ide Technologies Ltd Evaporator array for a water treatment system
WO2016025195A1 (fr) * 2014-08-13 2016-02-18 Veolia Water Technologies, Inc. Procédé et dispositif pour le refroidissement instantané d'eau produite et le chauffage d'eau d'alimentation de générateur de vapeur
WO2017180548A1 (fr) * 2016-04-14 2017-10-19 Veolia Water Technologies, Inc. Procédé de traitement d'eau produite avec de l'oxyde de magnésium
US10221670B2 (en) 2012-09-13 2019-03-05 Bl Technologies, Inc. Treatment of produced water with seeded evaporator

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CA2860277C (fr) * 2014-06-02 2016-10-25 Veolia Water Solutions & Technologies North America, Inc. Procede de recuperation d'hydrocarbure incluant l'adoucissement amelioree de l'eau produite
CN107032515A (zh) * 2016-02-04 2017-08-11 通用电气公司 用于从产出水流制备蒸汽的方法和装置及包含其的回收油的工艺和系统

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WO2017180548A1 (fr) * 2016-04-14 2017-10-19 Veolia Water Technologies, Inc. Procédé de traitement d'eau produite avec de l'oxyde de magnésium
CN108883950A (zh) * 2016-04-14 2018-11-23 威立雅水处理技术公司 用氧化镁处理采出水的方法
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CN101835954A (zh) 2010-09-15
BRPI0815845A8 (pt) 2015-12-29
BRPI0815845A2 (pt) 2015-02-24
RU2010111793A (ru) 2011-10-10
BRPI0815845B1 (pt) 2018-06-12
RU2479713C2 (ru) 2013-04-20
CN101835954B (zh) 2013-07-31

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