CN105188889B - 包含低压控制的渗透驱动隔膜***的发展 - Google Patents
包含低压控制的渗透驱动隔膜***的发展 Download PDFInfo
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Abstract
本发明涉及一种实例水净化***,其包含正向渗透模块、逆向渗透模块、由电动马达提供动力的泵及压力传感器。所述正向渗透模块可接收进料流及汲取流,且可产生中间产物流。所述中间产物流可由泵加压且被提供到所述逆向渗透模块。所述逆向渗透模块可产生产物流并将所述汲取流返回到所述正向渗透模块。所述压力传感器可监测所述中间产物流的压力,且所述压力可用于确定所述电动马达的速度。
Description
交叉参考
本申请案主张2013年3月15日申请的第61/794,537号美国临时申请案的早期申请日期的优先权,所述申请案的全文出于任何目的以引用的方式并入本文中。
技术领域
本文中描述的实例涉及分离***、元件及方法,其可用于正向渗透(FO)或逆向渗透(RO)或通常任何分离过程。
政府赞助
本发明是根据美国国防部授予的第W911NF-09-C-0079号合约在美国政府的支持下实现。美国政府对本发明拥有特定权利。
背景技术
渗透驱动隔膜过程能够通过用两种溶液之间的化学能量梯度驱动水流动跨过隔膜来以节能方式处理高度污染的溶液。渗透预处理过程利用相对于进料溶液具有高渗透势或渗透压的汲取溶液以提供使水输送跨过隔膜的驱动力。随着相对纯净的水流过隔膜,其稀释汲取溶液。
在渗透驱动隔膜水净化***中,随后必须再浓缩汲取溶液,或以某种方式回收溶质以用于重复利用。典型***采用脱盐设备(例如逆向渗透、蒸馏或其它析盐技术)或用于汲取溶质回收的其它方法(例如热交换盐)。通常,此类***被作为两个单独的子***进行控制:渗透***及再浓缩***,在所述两个子***之间具有缓冲容积并具有两个单独的抽排***。单独的抽排***调整每一流的流速及压力。
渗透***中的总生产率是由跨渗透隔膜的水流量规定,所述流量大部分是由汲取溶液渗透压与进料溶液渗透压的差来确定。在传统的***中,汲取溶液浓度是通过用喷射泵及汲取溶液缓冲贮槽将溶质添加到汲取溶液而控制。
在所有情况中,汲取溶液渗透势必须高于要处理的进料。在一些情况中,高的进料水浓度可使得汲取溶液浓度必需高于在依较低能量脱盐技术(例如逆向渗透(RO))进行再浓缩时通常可处理的浓度。
常规的RO***中通常使用的能量回收泵还可以不同方式操作以用于压力延缓渗透(PRO)***。在PRO***中,高渗透势汲取溶液被低渗透势进料溶液稀释。由于对汲取溶液加压,渗透驱动力被部分抵消,但是水通量仍然在汲取溶液的方向上。通过能量产生装置(例如涡轮机)解除汲取溶液中的过量水。
发明内容
本文中揭示了用于净化的设备及方法的实例。例如,一种设备可包含:正向渗透模块,其经配置以接收进料流及汲取流,且产生废弃进料流及中间流;压力传感器,其可测量所述正向渗透模块的汲取侧上的第一压力;及隔膜模块,其可接收所述中间流并产生产物流。所述设备可进一步包含液压泵,其可使所述中间流循环并将所述中间流加压到第二压力。所述设备可进一步包含能量回收装置,其可将所述汲取流从所述第二压力降低到所述第一压力;计量泵,其可将浓缩的汲取溶液提供到所述汲取流;及流量计,其可测量所述产物流的流速。
一种实例方法可包含将进料流提供到正向渗透模块;将汲取流提供到所述正向渗透模块;使所述进料流浓缩且使所述汲取流循环通过所述正向渗透模块,这可产生中间流;监测所述正向渗透模块的汲取侧上的压力;将所述中间流抽排到另一过滤器模块;及用另一过滤器模块过滤所述中间流,这可产生所述汲取流及产物流。所述方法可进一步包含监测所述产物流的流速并以可至少部分基于所述产物流的所述流速的计量速率将溶质提供到所述汲取流。
附图说明
图1是根据本发明的实施例的净化***。
图2是根据本发明的另一实施例的净化***。
图3是根据本发明的实施例的能量回收装置。
具体实施方式
下文陈述特定细节以提供对本发明的实施例的足够理解。然而,所属领域的技术人员将明白,可在无此类特定细节中的各种细节的情况下实施本发明的实施例。在某些情况下,并未详细展示熟悉的化学结构、化学成分、分子、材料、制造组件、控制***、电子组件、时序协议及软件操作以避免不必要地混淆本发明的所描述实施例。
根据本发明的实施例的净化***100被说明为图1中的方框图。为了避免不必要地混淆本发明的实施例,考虑稳定状态的***。
净化***包含正向渗透(FO)模块4中的FO隔膜元件的阵列,所述FO模块4可包含串联、并联或以其某个组合组成管道的一或多个FO隔膜元件。FO模块4可具有四个端口-用于接收进料流3的一个端口、用于接收汲取流17的一个端口、用于产生废弃进料流5的一个端口及用于产生中间流6的一个端口。净化***100进一步包含另一隔膜模块13,其可为逆向渗透(RO)模块。隔膜模块13可包含串联、并联或以其某个组合组成管道的一或多个RO隔膜元件。隔膜模块13可包含三个端口-用于接收加压中间流12的一个端口、用于产生产物流15的一个端口及用于产生汲取流16的一个端口。
进料流1可由进料泵2加压,形成低压进料流3。通常,可使用需要净化的任何进料流,包含但不限于海水或废水。流3可沿管道进入FO模块4中,其中所述流的流速可随着纯净水以某个FO透过流速跨FO隔膜转移到汲取流17而下降。进料溶质可保持在进料流中且按流3的流速减去FO透过流速的速率在废弃进料流5(例如,废流)中排出***。
汲取流17可具有高于进料溶液流3的压力的某个渗透压及接近大气压的静水压力,且可沿管道进入FO模块4的阵列中,其中所述流可随着纯净水以某个FO透过流速从进料流3转移跨过FO隔膜而增加。汲取流退出元件,形成中间流6(例如,中间产物流),其中所述中间流6可由泵9(例如,由电动马达8提供动力的液压泵)加压到大于汲入流17的渗透压的静水压力,从而形成经加压中间产物流12。
流12随后可沿管道进入到隔膜模块13中的隔膜元件的阵列中,在一些实例中所述隔膜模块13可为RO模块,其中所述流的流速可随着纯净水以某个RO透过流速转移跨过RO模块而下降。此RO透过以某个RO透过流速形成产物流15,所述产物流15是***的产物水。RO模块13还可产生浓缩汲取,其退出RO模块13,从而形成具有等于流17的流速的加压汲取流16。流16经过液压马达10(也称作能量回收装置)降压,从而形成汲取流17,其可处于接近大气压的某个压力下,从而重复利用汲取溶液。在一些实例中,可使用多个能量回收装置。
随着***运行,汲取溶质可跨FO模块4及隔膜模块13缓慢地分别损失到废流5及产物流15中。包括浓缩汲取溶液18的计量溶液可由计量泵19缓慢地或定期地抽排到汲取回路中,这可允许***保持在稳定状态。汲取溶液的溶质可为氯化钠,但是也可使用其它溶质。
由于汲取溶液的体积是固定的(忽略浓缩汲取流18的输入),为使所述***在数分钟内保持稳定状态,平均FO透过流速及RO透过流速可彼此相等。在常规***中,汲取溶液缓冲贮槽(未描绘)被添加到中间产物流6,从而允许可变的汲取溶液体积。此汲取溶液缓冲贮槽允许FO透过流速及RO透过流速随时间相对于彼此浮动,从而提供简单的控制方案。可在不修改任一透过流速的情况下添加计量溶液。
常规***的汲取溶液缓冲贮槽允许净化***的更简单控制,但是具有若干缺点。注意,常规***的缺点及本文中描述的实例的优点是通过实例方式提供以促进理解。应理解,并非所有实例均可具有所有或甚至任何所描述优点,且并非所有实例均可解决所有或甚至任何所描述常规***缺点。常规缓冲贮槽***的一个缺点可为,缓冲贮槽显著地增加净化***的重量及容积。例如,如图1中说明的典型***可具有近似20加仑的容积,且缓冲贮槽可具有近似100加仑的容积。部分归因于大的容积,常规***的响应时间不能快速适应进料状况或所需透过速率的变化。缓冲贮槽的使用还增加了生物生长的风险。缓冲贮槽中的缓慢流动或不流动增加细菌或其它生物物质生长的可能性。此生物生长可污染***的剩余部分,且可能需要额外过滤器或净化元件来移除生物生长。
本文中描述的实例包含使用压力控制***,所述压力控制***可允许实现净化***而无需缓冲贮槽或降低对缓冲贮槽的需要。通过移除汲取溶液缓冲贮槽或降低汲取溶液缓冲贮槽的容积,汲取溶液体积可变为固定常数或更接近固定常数,从而使FO模块4、RO模块13、泵及管道组件的容积的小变化不起作用。所得FO透过流速及RO透过流速可变成彼此液力锁定(例如,相等或成某种其它固定关系)。
压力控制***的实例可具有优于常规技术发展水平的FO/RO***的以下优点:可由移除汲取溶液缓冲贮槽及降低汲取体积导致大小及重量降低。可由减小汲取溶液体积导致***响应时间降低,从而允许汲取溶液浓度更迅速地变化以适应进料状况或所需透过速率的变化。可由使整个汲取溶液体积保持在相对较高速度的管道内导致生物生长的风险降低。由于不使汲取溶液暴露于大气压力,FO汲取溶液压力的精确控制可成为可能。其还可允许精确地控制进料压力与汲取压力之间的压力差,从而产生较高通量并降低结垢的倾向。可由于汲取溶液从未暴露于大气压而使汲取溶液压力守恒导致液压效率增加。此类可能优点还可使生产及操作***的成本降低。
通常,使用压力控制的水净化***的实例包含FO模块与后续隔膜模块(例如,RO模块)之间的泵,所述泵将从FO模块提供的中间流加压成提供到隔膜模块的加压中间流。加压量(例如,泵的流速)与FO模块的汲取侧(例如,汲取回路的低压侧上的任意处)上的包含汲取流及中间流的压力有关。因此,压力传感器可经提供以测量FO模块的输出处提供的中间流的压力,或提供到FO模块的汲取流的压力或FO模块的元件之间的汲取侧上的压力或其组合。通过根据FO模块的汲取侧压力改变泵的流速,可改变到后续隔膜模块(例如,RO模块)的输入流的压力,这可改变通过所述后续隔膜模块的透过流速。以此方式,由隔膜模块提供的产物流的流速可维持与正向渗透模块的汲取侧上的压力成比例(例如,在一些实例中等于正向渗透模块的汲取侧上的压力)。因此,通过FO模块及后续隔膜模块的透过流速在一些实例中可保持相等。
再次参考图1中说明的***。为了本发明的此实例实施例,考虑压力控制***,其具有由电动马达8驱动的单个固定排量高压液压泵9且包含集成固定排量液压马达10使得RO产物流速是电动马达8速度的直接函数。此泵的实例是Spectra Watermakers,Inc.(光谱制水公司)的SP5Pearson Pump及Danfoss SWPE。具有单独能量装置的高压泵也可连同此类装置中的任一者的阵列一起应用。在其它实例中,可使用其它泵,包含使用除了电动马达之外的其它机构设置流速的泵。
所述***可包含压力传感器,或换能器7可经定位以测量流6的压力,或替代地或此外,可位于流17(未示出)上,或替代地或此外,位于介于FO模块4的汲取侧上的元件之间的位置处。流量计14此外在一些实例中可经定位以测量RO产物流15上的流速。在其它实例中,流量计14可用以某种其它方式计算流量的逻辑来代替。当电动马达8为恒定速度时,FO透过流速及RO透过流速两者均可液力锁定到特定值。流6、12、16及17中的汲取溶液的液压可由跨相应模块4及13的特定透过流速及渗透驱动力确定。
流12及16中的RO压力可达到克服汲取溶液的渗透压并产生显著的RO透过流速所需的任何压力。流17及6中的FO压力可达到延缓或辅助跨FO隔膜阵列4的渗透压差以产生特定FO透过流速所需的任何压力。归因于进料及汲取渗透压、流速、温度、pH的变化及/或隔膜性能性质的变化,FO透过流速可需要例如通过增加进料液压使其高于汲取液压的辅助;或例如通过增加汲取液压使其高于进料液压的延缓。
在稳定状态期间,***控制方案可用来自压力换能器7的反馈控制电动马达8的速度。所述***可包含泵控制器(例如,微控制器、处理器、电路或其组合),其可使用比例积分微分(PID)控制算法或其它方法动态地设置泵9的流速以维持压力换能器7处的所需压力。此压力可预定或实时地计算以实现进料液压与汲取液压之间的给定压力差。如果压力开始超过所需压力,那么其可为所述***应延缓FO透过流速的指示符,且控制算法可增加电动马达8的速度,因此增加FO透过流速(跨隔膜或流6减去流17的流速水)及RO透过流速15。此可缓和压力换能器7处的压力,因此移除FO透过流速的延缓。如果压力换能器7的压力开始下降到所需压力之下,那么其可为所述***应辅助FO透过流速的指示符,且控制算法可降低电动马达8的速度,因此降低FO透过流速及RO透过流速。此可将压力恢复到所需压力,从而移除FO透过流速的辅助。在一些实例中,控制算法可能能够将压力换能器7处的低压控制点控制在一些实例中的0.1psi内、在一些实例中的0.2psi内、在一些实例中的0.3psi内、在一些实例中的0.4psi内、在一些实例中的0.5psi内、在一些实例中的0.6psi内、在一些实例中的0.7psi内、在一些实例中的0.8psi内、在一些实例中的0.9psi内、在一些实例中的1.0psi内-在其它实例中可使用更大或更小公差。
当***处于稳定状态中时,溶质可从汲取溶液跨FO模块4及RO模块13缓慢地损失。此可造成可由流量计14监测的RO透过流速的逐渐降低。为了维持恒定的RO透过流速,由泵19从流18添加浓缩汲取溶液。泵19可为由浓度控制器(未示出)控制的计量泵。浓度控制器可使用一或多个处理器、电路等等(例如,微控制器)实施。浓度控制器可进一步耦合到测量产物流的流速的流量计。浓度控制器可基于产物流的流速控制计量泵19的速度。例如,浓度控制器可比较产物流的流速与所需流速,且可控制计量泵19以添加溶质来维持所需流速。添加溶质可增加压力换能器7处的压力,因此增加马达8的速度且增加透过流速,从而适应计量溶液的流入。类似地,浓度控制器可控制计量泵19以关闭(或减速),以减小溶质添加的速率来维持所需流速。当泵19关闭时,压力可下降到设置点之下且可降低马达8的速度并降低透过流速。因此,使用渗透流量计14作为反馈,计量流速及占空比可控制***的透过流速。计量点可在汲取***、流17、6、12、16中的任意处。位于如图1中说明的低压侧上的优点可为通过减少可能需要的高压组件的数目来降低成本。
表1含有图1中说明的***中的不同点的实例流速、静水压力及溶质浓度。表1中给定的值是示范性的且不应被解释为将本发明的实施例限于给定值。流速、静水压力及溶质溶度的其它值是可能的。
表1:水净化***100的示范性值
图1中的元件编号 | 流量(gpm) | 静水压力(psi) | 浓度(ppm) | |
进料 | 3 | 6.25 | 5.0 | 32,000 |
进料废弃 | 5 | 5.00 | 0.0 | 42,000 |
FO汲取废弃(设置点7) | 6 | 6.25 | 0.5(设置点7) | 44,900 |
RO汲取进料 | 12 | 6.25 | 700.0 | 44,900 |
***透过(控制点14) | 15 | 1.25(设置点14) | 0.0 | 350 |
RO汲取废弃 | 16 | 5.00 | 685.0 | 56,125 |
FO汲取进料 | 17 | 5.00 | 3.0 | 56,125 |
本文中还描述了无源连接的汲取溶质贮槽的实例。运用无源连接的汲取溶质贮槽,汲取溶液回路的压力的变化将溶质汲取到回路中或将溶质从回路中推出。控制的简化具有降低成本、重量及大小以及改善稳定性、性能及可靠性的优点。图2中说明根据本发明的实施例的实例无源连接的汲取溶质贮槽***200的方框图。正向渗透模块215或渗透预处理***可接收进料流240及汲取流235。FO模块215产生中间产物流250,其可由泵220加压到逆向渗透模块225或再浓缩***。RO模块可产生产物流230并将汲取流235返回到FO模块215。汲取溶质贮槽205可通过流210无源地连接到***。
无源汲取溶质贮槽***可通过平衡生产率与汲取溶液渗透势而操作。如果***的所需生产率大于***当前的生产率,那么再浓缩***可被加速,从而产生额外的水。随着产生此额外的水,通过渗透预处理***的产量增加却可能不相符,因为跨渗透隔膜的渗透压差可能仍然相同。由于质量平衡的差异,汲取溶液回路的体积可下降。浓缩汲取溶质接着可从汲取溶质贮槽汲取到汲取溶液回路中,从而增加汲取溶液的浓度,且因此增加通过渗透预处理的水产量。可发生此额外的流量直到通过渗透预处理***的流量等于通过再浓缩***的流量且***稳定为止。如果***的所需生产率小于***当前的生产率,那么再浓缩***可减速。由于再浓缩以较低速度运行,可产生更少的水。随着产生更少的水,通过渗透预处理***的产量降低可能不相符,因为跨渗透隔膜的渗透压差可能仍然相同。由于质量平衡的差异,汲取溶液回路的体积可增加。汲取溶质接着可从汲取溶液推到汲取溶质贮槽,从而有效地减小汲取溶液的浓度,且因此可降低通过渗透预处理的水产量。可发生从汲取溶液回路的此种溶质移除直到通过渗透预处理***的流量等于通过再浓缩***的流量且***稳定为止。被***排出的过量汲取溶质可被废弃或保持在汲取溶质贮槽中,并在需要增加汲取溶质的后续时间使用。
在例如可需要供应水来加压所述流并从高压水返回产生有用能量的压力延缓渗透(PRO)的过程中,可修改常规的能量回收泵以逆向操作,其中泵的高容积侧为隔膜废弃侧,而非如常规过程中正常进行的那样的供应侧。PRO泵将两种单独组件组合为单个组件。泵的低容积侧可汲入低液压的盐水(例如浓缩的氯化钠水溶液或海水),活塞可对所述流加压,且将盐水抽排到PRO隔膜元件。在PRO隔膜元件中,盐水被稀释,且体积增加。此可迫使盐水流出到泵的高容积侧,其中活塞的高容积侧上的高压力用于对低容积入口加压,以及在泵轴件上产生额外力。在从高压高体积流回收能量之后,低压高体积稀释盐水从泵排放。PRO泵的优点可为更紧凑设计、重量下降、液压及电气效率及简单性增加。
本文中还描述了能量回收泵的实例。根据本发明的实施例的能量回收泵300被说明为图3中的方框图。固定回收正排量能量回收泵可用于从PRO***产生动力。到***的盐水进料305可被馈进到泵310的低容积入口。泵可对此流入汲取流加压,且将加压流345抽排到PRO隔膜容器325。PRO隔膜容器还可接收低渗透压流330。在一些实例中,低渗透压流330可为淡水、河水或废水。来自PRO隔膜容器325的高压汲取流返回335被馈进到泵320的高容积入口,且然后以低压作为废水315从***排出。泵轴件340用于驱动发电设备(未示出)。
根据前文将明白,虽然本文中是为了说明目的描述了本发明的特定实施例,但是在不脱离本发明的精神及范围的情况下可作出各种修改。
Claims (20)
1.一种分离设备,其包括:
正向渗透模块,其经配置以接收进料流及汲取流,所述正向渗透模块经进一步配置以产生废弃进料流及中间流;
压力传感器,其经配置以测量所述正向渗透模块的汲取侧上的所述中间流、提供到所述正向渗透模块的汲取流或所述正向渗透模块的一或多个元件之间的汲取侧上的汲取流的一者或多者的第一压力;
液压泵,其经配置以使所述中间流循环从而提供具有第二压力的加压中间流;
隔膜模块,其经配置以接收所述加压中间流,所述隔膜模块经进一步配置以产生浓缩汲取流和产物流,其中所述产物流具有至少部分基于所述第一压力的流速;以及
泵控制器,其耦合到所述压力传感器及所述液压泵,其中所述泵控制器经配置以比较所述第一压力与所需压力,且经进一步配置以当所述第一压力高于所述所需压力时增加所述产物流的流速且当所述第一压力低于所述所需压力时降低所述产物流的流速。
2.根据权利要求1所述的设备,其进一步包括:
能量回收装置,所述能量回收装置经配置以将所述浓缩汲取流的压力降低到所述汲取流的压力;
计量泵,其经配置以将浓缩汲取溶液提供到所述汲取流;以及
流量计,其耦合到所述计量泵、经配置以测量所述产物流的所述流速,其中所述计量泵部分由所述流量计控制使得由所述计量泵提供的浓缩汲取溶液的量至少部分基于所述产物流的所述流速。
3.根据权利要求1所述的设备,其中所述中间流、所述汲取流、所述加压中间流和所述浓缩汲取流的体积是固定的。
4.根据权利要求1所述的设备,其中通过所述正向渗透模块的透过流速经配置成等于通过所述隔膜模块的透过流速。
5.根据权利要求1所述的设备,其中所述泵控制器经配置以将所述第一压力维持在与所述所需压力相差在1psi内。
6.根据权利要求1所述的设备,其中所述泵控制器包含经配置以执行比例积分控制算法的处理器。
7.根据权利要求2所述的设备,其进一步包括耦合到所述流量计及所述计量泵的浓度控制器,其中所述浓度控制器经配置以至少部分基于所述产物流的所述流速控制所述计量泵的速度。
8.根据权利要求7所述的设备,其中所述浓度控制器经配置以比较所述产物流的流速与所需流速,且经进一步配置以使用所述计量泵添加溶质以维持所述所需流速。
9.根据权利要求1所述的设备,其中所述泵是固定容积排量泵。
10.根据权利要求2所述的设备,其中所述能量回收装置是固定排量回收装置。
11.根据权利要求10所述的设备,其进一步包括多个能量回收装置。
12.根据权利要求1所述的设备,其进一步包括经配置以将所述进料流抽排到所述正向渗透模块的进料泵。
13.一种分离方法,其包括:
将进料流提供到正向渗透模块;
将汲取流提供到所述正向渗透模块;
使所述进料流浓缩且使所述汲取流循环通过所述正向渗透模块以产生中间流;
监测所述正向渗透模块的汲取侧上的所述中间流、提供到所述正向渗透模块的汲取流或所述正向渗透模块的一或多个元件之间的汲取侧中的汲取流的一者或多者的第一压力;
响应于所述第一压力,选择性地加压所述中间流以提供具有第二压力的加压中间流从而有效地产生所选择的产物流流速;
将所述加压中间流抽排到另一过滤器模块;
用所述另一过滤器模块过滤所述加压中间流以依至少部分基于所述第一压力的所选择的流速产生所述汲取流及产物流。
14.根据权利要求13所述的方法,其中所述另一过滤器模块包括逆向渗透模块。
15.根据权利要求13所述的方法,其进一步包括:
监测所述产物流的流速;
以至少部分基于所述产物流的所述流速的计量速率将溶质提供到所述汲取流。
16.根据权利要求13所述的方法,其中由进料泵将所述进料流提供到所述正向渗透过滤器。
17.根据权利要求13所述的方法,其进一步包括:
将所述第一压力提供到处理器;
使用所述处理器执行比例积分控制算法;以及
基于所述比例积分控制算法修改所述产物流的所述流速。
18.根据权利要求17所述的方法,其中当所述中间流的压力高于所需压力时增加所述产物流的所述流速,且当所述中间流的压力低于所述所需压力时降低抽排速率。
19.根据权利要求13所述的方法,其进一步包括:
将所述中间流、所述汲取流和所述加压中间流提供到固定容积回路。
20.根据权利要求15所述的方法,其中当所述产物流的流速低于所需速率时增加所述计量速率,且当所述产物流的流速高于所述所需速率时降低或停止所述计量速率。
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