CN108883950A - 用氧化镁处理采出水的方法 - Google Patents
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 89
- 229910001868 water Inorganic materials 0.000 title claims abstract description 89
- 238000000034 method Methods 0.000 title claims abstract description 44
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title description 18
- 239000000395 magnesium oxide Substances 0.000 title description 9
- 238000012545 processing Methods 0.000 title description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 120
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 60
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims abstract description 40
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 33
- 239000000347 magnesium hydroxide Substances 0.000 claims abstract description 32
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims abstract description 32
- 239000012141 concentrate Substances 0.000 claims abstract description 28
- 238000004821 distillation Methods 0.000 claims abstract description 9
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 7
- 239000006200 vaporizer Substances 0.000 claims abstract description 6
- 230000001376 precipitating effect Effects 0.000 claims description 11
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 9
- 239000011777 magnesium Substances 0.000 claims description 9
- 229910052749 magnesium Inorganic materials 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 7
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- 238000000926 separation method Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 5
- 239000013078 crystal Substances 0.000 claims description 3
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- 241000790917 Dioxys <bee> Species 0.000 claims description 2
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- 239000003129 oil well Substances 0.000 claims 1
- 150000001875 compounds Chemical class 0.000 abstract description 4
- 238000002425 crystallisation Methods 0.000 description 24
- 230000008025 crystallization Effects 0.000 description 24
- 239000003921 oil Substances 0.000 description 16
- 235000012254 magnesium hydroxide Nutrition 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 239000002244 precipitate Substances 0.000 description 6
- 238000010796 Steam-assisted gravity drainage Methods 0.000 description 5
- 238000000605 extraction Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 3
- 150000002681 magnesium compounds Chemical group 0.000 description 3
- 238000000975 co-precipitation Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical group [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
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- 238000007872 degassing Methods 0.000 description 1
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- 239000002270 dispersing agent Substances 0.000 description 1
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- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 230000009969 flowable effect Effects 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
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- 238000002347 injection Methods 0.000 description 1
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- 231100000719 pollutant Toxicity 0.000 description 1
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- 230000008016 vaporization Effects 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/60—Silicon compounds
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK 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
- E21B43/35—Arrangements for separating materials produced by the well specially adapted for separating solids
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F2001/5218—Crystallization
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- C02F2101/10—Inorganic compounds
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
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Abstract
本发明涉及一种使用一个或多个蒸发器来处理含有二氧化硅的采出水的方法。为了解决二氧化硅结垢,将结晶试剂与蒸发器上游的采出水混合。设计结晶试剂以沉淀二氧化硅吸附性化合物,诸如氢氧化镁。将具有被吸附的二氧化硅的给水引导至蒸发器,该蒸发器产生蒸馏物和含有被吸附的二氧化硅的浓缩物。将至少一部分具有二氧化硅吸附性化合物的浓缩物引导至分离器,该分离器使二氧化硅吸附性化合物与浓缩物分离,并且再循环返回至与采出水混合的地方。
Description
发明领域
本发明涉及从含油地层回收油,更具体地,本发明涉及一种处理采出水(producedwater)的方法,用以在到达倾向于二氧化硅结垢的下游设备之前,从采出水除去二氧化硅。
背景技术
强化采油(Enhanced oil recovery, EOR)方法采用热能来促进从含油地质学地层回收油,特别是重油。用于回收重油的一种具体方法称为蒸汽辅助重力泄油(steam-assisted gravity drainage, SAGD)。在SAGD方法中,将蒸汽注入含油地层中,以供应热能,以使重油流动。通常,对于通过该方法回收的每一吨油,需要几吨的蒸汽。注射的蒸汽加热束缚在地层中的油,该加热降低了油的粘度。来自蒸汽的热来自显热(随着蒸汽冷却)和潜热(随着蒸汽冷凝成水)。油的降低的粘度使得油能够与水混合,产生油-水混合物,该油-水混合物可流动至收集区域,并且最终被泵送至地面。通过从油-水混合物实质除去油而回收油,留下所谓的采出水。
采出水必须经过处理。蒸发技术为处理来自SAGD方法的采出水的被接受的一种方法。该热方法产生高品质蒸馏物作为给水用于蒸汽发生,并且允许灵活采用传统的直流蒸汽发生器(once-through steam generator)或汽包式锅炉(drum-type boiler)。当然,处理采出水以形成相对纯的给水用于蒸汽发生具有挑战性。处理采出水最具挑战性的部分之一是延迟或防止在蒸发器中二氧化硅结垢。多种方法已解决结垢。第一代蒸发方法使用大量的化学品,诸如苛性碱、scalant、分散剂(disperant)等,以保持二氧化硅可溶。使用这些化学品是昂贵的,并且不总是提供无垢操作,进而需要另外的化学品或机械清洁。例如,高pH方法使氢氧化钠与采出水混合,以提高采出水的pH至足以保持二氧化硅可溶。这是昂贵的,因为需要连续和大量的氢氧化钠。此外,该溶液不能保证无垢操作。此外,使用结晶方法来吸附二氧化硅是已知的。这些方法也是昂贵的。这是因为需要连续供应新的结晶试剂。
因此,需要采出水或给水处理方法,其利用化学处理来除去二氧化硅,但是比起在现有技术中已实现的,更加成本有效。
发明内容
本发明涉及一种使用一个或多个蒸发器来处理给水流的方法,其中所述给水包括二氧化硅。为了解决二氧化硅结垢,将结晶试剂与蒸发器上游的给水混合。设计结晶试剂以沉淀二氧化硅吸附性化合物。也就是,结晶试剂引起二氧化硅和吸附二氧化硅的沉淀剂共沉淀。将具有被吸附的二氧化硅的给水引导至产生蒸馏物和浓缩物的蒸发器,其中所述浓缩物包括被吸附的二氧化硅。将具有结晶的沉淀剂的至少一部分浓缩物引导至分离器,诸如旋液分离器。分离器使沉淀剂与浓缩物分离,并且再循环返回至将已分离的沉淀剂与给水混合的地方。该方法引起沉淀剂结晶,并且形成的结晶再循环,形成晶种材料以吸附二氧化硅。
在一个实施方案中,本发明涉及一种用于处理包括二氧化硅的采出水的蒸发器方法。此处再一次,为了解决二氧化硅结垢,将结晶试剂与采出水混合,这导致形成结晶和被吸附在结晶上的二氧化硅共沉淀。将结晶和被吸附的二氧化硅引导至蒸发器,并且在蒸发器浓缩物中结束。所述方法需要将所述浓缩物从蒸发器引导至分离器,该分离器使结晶与浓缩物分离,并且使已分离的结晶再循环返回,以与进入的采出水混合。这降低了结晶试剂的消耗,并且能够使所得到的结晶被再利用,以从采出水吸附二氧化硅,从而实质降低解决二氧化硅结垢所承受的化学成本。
在一个具体实施方案中,结晶试剂为氧化镁,其在位于蒸发器上游的除气器中与采出水混合。当与采出水混合时,氧化镁得到氢氧化镁,氢氧化镁沉淀以形成氢氧化镁结晶。二氧化硅与氢氧化镁共沉淀,并且吸附至氢氧化镁结晶。具有被吸附的二氧化硅的这些氢氧化镁结晶在蒸发器的浓缩物中结束。将蒸发器中的浓缩物引导至分离器,诸如旋液分离器,旋液分离器使氢氧化镁沉淀剂或结晶与浓缩物分离,并且再循环返回至除气器,在这里它们与进入的采出水混合。
根据仅用于说明本发明的以下描述和附图的研究,本发明的其他目的和优点将变得显而易见和明显。
附图说明
图1为显示使用蒸发器处理给水或采出水的系统和方法的示意性说明。
具体实施方式
进一步参考附图,其中显示用于处理给水流的系统和方法。如后面将讨论的,给水可为采出水流或其他废水流,其通常包括悬浮的固体、硬度、碱度、油和各种其他溶解的固体,包括二氧化硅。如在图1中显示的,在该具体的实施方案中,将给水通过管线12引导至预加热器14中。在预加热器中加热给水。可提供各种热源用于加热给水。例如,可将通过蒸发器20产生的蒸馏物引导通过预加热器14,用于加热给水的目的,该蒸发器20形成本发明系统的一部分。将给水从预加热器14引导至除气器16,并且向下通过除气器16。采用常规的方式,除气器16从给水12除去不能冷凝的气体。虽然未在图1中具体显示,但是在除气器16中可采用各种手段,以从给水有效汽提不能冷凝的气体,诸如CO2。在图1中显示的系统和方法包括通向除气器16的试剂注射管线17。如以下将讨论的,试剂注射管线27的功能是将结晶试剂注入除气器中,以与给水混合。在本文讨论的实施方案和方法中,结晶试剂的功能是吸附和共沉淀二氧化硅,以防止在下游设备(尤其是蒸发器的传热管)中二氧化硅结垢或使之最小化。将给水从除气器16引导至主要由数字20指示的蒸发器中。可使用各种类型的蒸发器,包括例如降膜蒸发器、强制循环蒸发器、多效蒸发器和机械蒸汽压缩(MVC)蒸发器。在图1中显示的实例中,蒸发器20为MVC蒸发器。注意到将在蒸发器主体内产生的蒸汽引导通过蒸汽洗涤器20A,随后压缩器20B压缩蒸汽,并且将蒸汽引导返回至蒸发器,在这里经压缩的蒸汽接触用于汽化给水或者通过蒸发器20产生的循环浓缩盐水的传热管。关于这一点,蒸发器20包括浓缩物再循环管线20C和泵20D,用于再循环给水或所得到的浓缩盐水通过蒸发器20。如本领域技术人员认识到的,蒸发器20产生蒸汽,其冷凝以形成蒸馏物,该蒸馏物可用于各种目的。在一个实施方案中,将蒸馏物引导通过预加热器14,如以上讨论的,并且从预加热器14,蒸馏物可用作通向直流蒸汽发生器、汽包锅炉或其他蒸汽发生设备的给水。
在图1中显示的系统和方法包括引导至分离器24的浓缩物排放管线22,在该实施方案中,分离器24包括旋液分离器。如以后将讨论的,分离器或旋液分离器24用于使沉淀剂或结晶与浓缩物分离,并且使它们再循环至除气器16。更具体地,该方法的目的是分离沉淀剂或因为结晶试剂与给水混合而得到的结晶。将旋液分离器中的溢流引导离开溢流清除管线26。
现在转向在图1中显示的方法的一个具体应用,给水可包括采出水,其是由从含油地层回收的油-水混合物分离的。采出水通常包括显著量的二氧化硅和其他污染物。二氧化硅可引起下游蒸发器20的传热管的二氧化硅结垢。因此,该方法的目的是在二氧化硅到达蒸发器20之前,从采出水有效除去二氧化硅。通过使结晶试剂与采出水混合,完成这一点,其中结晶试剂用于共沉淀二氧化硅,并且将二氧化硅吸附到从采出水沉淀的结晶上。本发明的另一个特征是有效回收结晶试剂或沉淀的结晶并且再利用,以降低结晶试剂的成本。
在一个实施方案中,形成结晶的试剂为氧化镁。向采出水加入氧化镁导致形成氢氧化镁,氢氧化镁从采出水沉淀,并且形成吸附二氧化硅的结晶。可加入各种形式的镁。在一些方法中,可加入氯化镁形式的镁。在任何情况下,如上所述,镁化合物形成吸附采出水中的二氧化硅的氢氧化镁结晶,有效导致二氧化硅从可溶形式转化为不可溶形式。
虽然镁结晶试剂可在蒸发器20上游的多个位置加入,在本文说明的实施方案中,通过管线17将镁化合物(在此情况下,氧化镁)注入除气器16。通过管线18将采出水从除气器16引导至蒸发器20。因为二氧化硅被吸附到沉淀的氢氧化镁上,所以由此可见,存在于采出水中的二氧化硅不能显著结垢蒸发器20的传热管。认识到,氢氧化镁结晶和在其上被吸附的二氧化硅将变为蒸发器浓缩物的一部分,并且将被连续再循环通过蒸发器20。一部分蒸发器浓缩物将经由管线22从蒸发器引导。由此可见,管线22中的蒸发器浓缩物将包括沉淀的氢氧化镁或氢氧化镁结晶,并且其中一些氢氧化镁或镁结晶将包括被吸附的二氧化硅。
本发明的方法旨在使氢氧化镁沉淀剂或结晶与蒸发器浓缩物分离,并且再循环至除气器16,以与采出水混合。在图1中显示的方法和实施方案中,将管线22中的蒸发器浓缩物引导至分离器,该分离器用于使氢氧化镁沉淀剂或结晶与浓缩物分离。采用旋液分离器来完成分离方法。旋液分离器将产生溢流和潜流。潜流将包括氢氧化镁沉淀剂或结晶,并且它们将通过管线23被引导返回至除气器16,其中氢氧化镁沉淀剂或结晶用作晶种材料,并且再一次用于吸附二氧化硅。这降低了需要经由管线17注入除气器16的新的氧化镁或其他镁化合物的量。旋液分离器24将产生溢流,其可称为清除或污泥,其可通过常规的手段处置或经历进一步处理。
因此,本发明的方法产生从给水和采出水流除去二氧化硅的成本有效的和高效的方式。特别地,通过结合有效手段回收二氧化硅吸附性沉淀剂并使其生长为结晶,该结晶被一再地使用以从给水流或采出水流吸附二氧化硅,这避免了"直流(once through)"试剂的成本缺点。
当然,在不偏离本发明的范围和必要特征的情况下,可以采用本文描述的那些以外的其他具体的方式来进行本发明。因此,当前的实施方案在所有方面解释为说明性而不是限制性的,并且在所附权利要求书的含义和等同范围内的所有变化旨在涵盖于其中。
Claims (5)
1.一种从含油地层回收油的方法,所述方法包括:
从所述含油地层回收油-水混合物;
从所述油-水混合物分离油,以产生油产物和含有其中溶解的二氧化硅的采出水;
引导所述采出水通过除气器,并且从所述采出水除去不能冷凝的气体;
将基于镁的试剂引导到所述除气器中,在所述除气器中使所述基于镁的试剂与所述采出水混合,引起氢氧化镁和二氧化硅从所述采出水共沉淀,并且将所述二氧化硅吸附到所述氢氧化镁上;
在所述除气器中使所述基于镁的试剂与所述采出水混合之后,将具有所述氢氧化镁和被吸附的二氧化硅的所述采出水引导至蒸发器,并蒸发所述采出水,以产生蒸馏物和含有所述氢氧化镁和被吸附的二氧化硅的浓缩物;
将至少一部分所述浓缩物引导至分离器,使至少一部分所述氢氧化镁与所述浓缩物分离;和
将已分离的氢氧化镁引导至所述除气器,在所述除气器中使所述已分离的氢氧化镁与所述采出水混合,其中所述已分离的氢氧化镁用于从所述采出水吸附二氧化硅。
2.权利要求1的方法,其中所述分离器包括旋液分离器,并且其中所述旋液分离器产生包括所述已分离的氢氧化镁的潜流,并且其中将所述潜流引导至除气器中。
3.一种从油井回收油的方法,所述方法包括:
从所述井回收油-水混合物;
从所述油-水混合物分离油,以产生油产物和具有其中溶解的二氧化硅的采出水;
使基于镁的试剂与所述采出水混合,引起氢氧化镁和二氧化硅从所述采出水共沉淀,并且将所述二氧化硅吸附到经沉淀的氢氧化镁上;
将具有所述氢氧化镁和被吸附的二氧化硅的所述采出水引导至蒸发器,并蒸发所述采出水,以产生蒸馏物和具有带有被吸附的二氧化硅的氢氧化镁的浓缩物;和
将至少一部分所述浓缩物引导至分离器,使至少一部分所述氢氧化镁与所述浓缩物分离,通过使已分离的氢氧化镁与所述蒸发器上游的采出水混合,使所述已分离的氢氧化镁再循环,其中所述已分离的氢氧化镁用于从所述采出水吸附二氧化硅。
4.权利要求3的方法,其中将所述采出水引导至位于所述蒸发器上游的除气器中,并且所述方法包括在所述除气器中从所述采出水除去不能冷凝的气体;和
其中所述方法包括在所述除气器中使所述基于镁的试剂以及与所述蒸发器浓缩物分离的氢氧化镁和所述采出水混合。
5.权利要求3的方法,其中与所述蒸发器浓缩物分离的氢氧化镁的所述再循环导致形成氢氧化镁结晶,并且其中所述氢氧化镁结晶形成晶种材料,用于从所述采出水吸附二氧化硅。
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