CN101998876B - 从空气中提取co2的方法和装置 - Google Patents

从空气中提取co2的方法和装置 Download PDF

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CN101998876B
CN101998876B CN200780036850.5A CN200780036850A CN101998876B CN 101998876 B CN101998876 B CN 101998876B CN 200780036850 A CN200780036850 A CN 200780036850A CN 101998876 B CN101998876 B CN 101998876B
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carbon dioxide
algae
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air
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CN101998876A (zh
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艾伦·B·赖特
克劳斯·S·拉克纳
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Carbon Sink Inc
Kilimanjaro energy Co.
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Abstract

本发明公开一种从空气中提取CO2并将提取的CO2传送至受控环境的方法和装置，包括在暴露于空气流的基质中形成的阴离子交换材料；本发明考虑利用常规提取方法或通过利用揭露的提取方法之一，如湿度波动或电渗透从空气中提取CO2。本发明还提供将CO2传送到温室，在温室中CO2水平的增高将改善生长条件。此外，CO2还可用于藻类培养。

Description

从空气中提取CO2的方法和装置
发明领域
本发明一方面涉及从空气中除去选定的气体。本发明尤其用于从空气中提取和隔离二氧化碳(CO2)，并联系这些用途来加以说明，然而其它用途也在考虑范围内。 
背景技术
有令人信服的证据表明大气中二氧化碳水平的急剧增加和全球表面温度的相应增加之间具有很强的相关性。这种影响通常被称为全球变暖。CO2排放的各种来源中有大量小而分布广泛的排放体，从源头上减轻它们是不切实际的。另外，大规模的排放体如碳氢燃料发电厂没有受到充分保护来防止排出的CO2进入大气。这些主要来源和其它的结合起来导致大气二氧化碳浓度的急剧增加率的发生。直到所有排放体在其源头被纠正为止，其它技术都需要来捕获尽管相对较低但增长着的背景水平的大气CO2。人们正在努力提高现有的排放减少技术以及开发新型技术，用于直接捕获周围环境的CO2。这些努力需用方法学来管理由此产生的CO2的浓缩废物流，以防止它被重新引入大气。 
CO2的产生发生在各种工业应用中，如电力发电厂从煤中产生，以及碳氢化合物的使用中，碳氢化合物通常为燃烧设备如发动机燃烧的燃料的主要成分。从这些燃烧装置排出的废气包含CO2气体，目前只被简单地释放到大气中。然而，随着对温室气体的关注增加，来自所有来源的CO2排放将必须缩减。对于移动源来说，最佳选择很可能是直接从空气中而不是从汽车或飞机的移动燃烧装置收集二氧化碳。从空气中除去CO2的优点在于它不再需要将CO2储存在移动装置上。 
从周围空气中提取二氧化碳(CO2)使人们有可能利用碳基燃料并在事后处理相关的温室气体排放。由于二氧化碳按百万分之一的数量计既无毒也 无害，但仅通过在大气中积累就造成环境问题，所以从空气中除去CO2有可能可以弥补不同时间其它地方同样大小的排放量。 
然而，大多数现有技术方法结果是从空气中捕获CO2，其效率差，因为这些过程加热或冷却空气，或大量改变空气压力。因此CO2净损失可忽略不计，因为该清洁过程将CO2作为给该过程提供动力的发电的副产品引入大气中。 
各种方法和装置已经被开发用于从空气中除去CO2。例如，我们最近公布的用捕获溶剂从周围空气中有效提取二氧化碳(CO2)的方法，这些溶剂从空气中物理地或者化学地结合和除去二氧化碳。一类实用的CO2捕获吸附剂包括强碱性氢氧化溶液，如氢氧化钠或氢氧化钾，或碳酸盐溶液，如碳酸钠或碳酸钾盐水。示例参见公布的PCT申请PCT/US05/29979和PCT/US05/029238。 
隔离的CO2也有许多用途：这包括CO2在温室中的应用，在此处较高水平的CO2有助于促进植物生长。CO2也可提供给藻类培养。研究人员指出藻类可以从富集CO2的空气流中除去高达90％的气态CO2，也可以降低周围空气中CO2的浓度。 
发明内容
本发明提供了一种系统，即用于从空气中提取二氧化碳(CO2)并将提取的CO2传送到受控环境的方法和装置。 
在第一种示范实施方式中，本发明从周围空气中提取CO2并将提取的CO2传送到温室。优选地，使用具有强湿度功能的强碱性离子交换树脂，也就是随湿度降低能够吸收CO2而随湿度增加释放CO2的离子交换树脂，从周围空气中提取CO2。本发明的几个方面也可用于将CO2从收集器介质转移到温室的空气空间，在此CO2被再次固定于生物量中。在本发明优选的实施方式中，使用位于靠近温室的提取器(extractor)将CO2从空气提取到温室，并将提取的CO2直接传送到温室内部，用于使温室空气富含CO2以便促进植物生长。 
在本发明的第二种示范实施方式中，本发明允许将CO2从收集器介质转 移到藻类培养，在此CO2被固定于生物量中。然后藻类生物量可用于生产生化化合物、肥料、土壤调节剂、保健食品和生物燃料等，这里仅举出几个应用或最终用途的例子。 
本发明还揭露了气相中的CO2作为碳酸氢根离子的转移。在一种实施方式中，使用石灰藻类，它可内在地产生碳酸钙CaCO3，并将CaCO3沉淀为石灰石。 
因此，从广泛概念上讲，本发明利用如上述PCT/US05/29979和PCT/US06/029238所描述的若干二氧化碳提取技术之一从空气中提取二氧化碳：其中碳酸盐/碳酸氢盐溶液用作主要的CO2吸附剂，载有CO2的吸附剂可直接用作藻类饲料。当使用离子交换树脂提取CO2时，例如我们上述的PCT/US06/029238申请教导的那样，利用二级(secondary)碳酸盐/碳酸氢盐洗液将CO2从树脂剥离，然后该碳酸盐/碳酸氢盐洗液用作藻类饲料。在优选的另外的实施方式中，可在光照增强的生物反应器中用碳酸盐喂养藻类。 
因此，本发明提供一种简单的、相对低成本的从周围空气捕获CO2随后将捕获的CO2处理的解决方案。 
附图简要说明 
从以下详细说明结合附图可看出本发明进一步的特点和优点，其中 
图1是说明根据本发明的湿敏离子交换树脂的用途的方框流程图； 
图2a和2b是根据本发明的CO2提取器/温室填充器的示意图，其中过滤单元外墙； 
图3a和3b是根据本发明的CO2提取器/温室填充器的示意图，其中过滤单元靠近温室顶； 
图4是根据本发明的显示过滤器单元安排的CO2提取器/温室填充器的示意图； 
图5是根据本发明的一种可选实施方式显示过滤器单元安排在轨道上的CO2提取器/温室填充器的示意图； 
图6是根据本发明的一种可选实施方式包括对流塔的CO2提取器/温室填充器的示意图； 
图7是根据本发明的利用适合收集器介质湿度波动的CO2提取器和藻类培养的示意图； 
图8是根据本发明的利用适合收集器溶液波动的CO2提取器和藻类培养的示意图； 
图9是根据本发明的通过电透析过程转移气态CO2的CO2提取器和藻类培养的示意图； 
图10是根据本发明的通过电透析过程转移碳酸氢盐的CO2提取器和藻类培养的示意图； 
图11是根据本发明的将藻类培养用于收集器再生的CO2提取器和藻类培养的示意图； 
图12是与图11类似的将营养液用于收集器再生的CO2提取器和藻类培养的示意图，； 
图13是根据本发明的利用透气膜的CO2提取器和藻类培养的示意图； 
图14是根据本发明的利用阴离子渗透膜的CO2提取器和藻类培养的示意图； 
图15是与图14类似的CO2提取器和藻类培养的示意图； 
图16是根据本发明的包括一淋浴的CO2提取器和藻类培养的示意图；以及 
图17是与图16类似的CO2提取器和藻类培养的示意图。 
具体实施方式
从广泛概念上讲，本发明一方面利用上述专利申请或本文揭露的常规CO2提取方法或改进的CO2提取方法从周围空气中提取二氧化碳，并将至少一部分提取的CO2释放到一封闭环境。 
在第一种示范实施方式中，该封闭环境为温室。优选地但不是必需地，CO2提取器位于靠近温室，并且在一种优选实施方式中提取器还为对强光敏感的农作物在温室生长提供遮荫，和/或为温室降低冷却要求。 
在捕获CO2的一种途径中，树脂介质通过与温暖高度湿润的空气接触而再生。已经表明湿度刺激存储介质中存储的CO2的释放，通过这种方法可 使CO2浓度达到3％-10％，并且在排空/脱水系统中可达到近100％。在该途径中，CO2返回气相，没有液体介质被携带与收集器材料接触。 
CO2提取器紧邻温室，将其移到温室外以收集CO2，移到温室内排出CO2。在这种实施方式中，CO2提取器优选包括一湿敏离子交换树脂，其中离子交换树脂干燥时提取CO2，暴露于高湿度时放出CO2。湿度波动最好适合用在干旱气候。在这样的环境下，提取器暴露于温室外部的干热空气中，CO2提取自该空气。然后，将提取器移到温室的暖湿环境中，在此离子交换树脂放出CO2。除了将提取器从温室外部移到内部以及相反移动的能量外，整个过程不需要任何直接的能源投入即可完成。 
离子交换树脂商业上可获得，用于如水软化和净化。我们已经发现，某些商业上获得的离子交换树脂为湿敏离子交换树脂，包括强碱树脂，可有利地用于根据本发明的从空气中提取CO2。有了这种材料，湿度越低，树脂上负载的碳平衡越高。 
因此，在高湿度水平表现出载有CO2并与CO2特定分压相平衡的树脂，若湿度增加将呼出CO2，湿度降低将吸收CO2。这种影响很大，并且很容易将平衡分压改变几百甚至几千ppm。如果与其总吸收能力相比，树脂上额外吸收或损失的碳也是大量的。 
湿度还可能对传热系数有影响，即反应动力学可能会随着湿度的变化而变化。然而，测量的进出树脂的流量可能极大地取决于实际分压和热力学平衡压之间的差异。当平衡压随湿度变化时，流量大小会受到影响而反应动力学无实际变化： 
此外，动力学也有可能受其他问题的影响。例如，我们发现的特别有用的离子交换材料是购自加利福尼亚圣克莱门特Snowpure公司的阴离子I-200离子交换膜材料。制造商介绍阴离子I-200离子交换膜材料为强碱性，1型功能的离子交换材料。这种材料，可被认为是根据美国专利No.6503957制成并被认为包括图表封装或-部分封装-在无活性的如聚丙烯一样的聚合物中的小树脂。我们已经发现，如果先水合这种材料，然后将其干燥，该材料就变得多孔并易于让空气通过。水合/脱水制备被认为主要起膨胀聚丙烯粘合剂的作用，并且对树脂有极少或没有永久性的影响，而随后的湿度波动对聚丙烯粘 合剂没有观察到的影响。我们已发现这些强碱性离子交换树脂材料具有从干燥空气中提取CO2，当湿度提高无其它干预时释放CO2的能力。这些直接从干燥时的空气中提取CO2，湿度提高时呼出CO2的材料以前未曾有报道。 
如上所述，使用前有必要先水合这种材料然后干燥，于是该材料变得多孔并易于让空气通过。水合前，该膜材料实质上非多孔或至少不允许可观量的空气通过该膜。然而，水合和干燥后，该材料被认为在水合下树脂膨胀时经历了聚丙烯基质的不可逆变形。一旦该材料已经变形，即使树脂颗粒干燥收缩后，聚丙烯基质也维持其延伸的形状。因此，对于上述实质上非多孔材料如Snowpure离子交换材料来说，有必要在使用前通过水合然后干燥来事先准备该材料。 
我们观察到CO2在树脂上的平衡分压随着湿度变化而变化。湿度或者改变树脂的状态，或者可选地改变整个系统，需要考虑的整个系统是CO2/H2O树脂系统。当不受理论约束时，人们认为CO2粘附树脂的自由能是与树脂相平衡的H2O分压的函数。 
这就有可能使树脂随湿度简单的摆动吸收或呼出CO2而不需要诉诸会增加能量成本的理论波动和/或压力波动，能量成本对系统总的CO2平衡具有不利影响。 
这种波动中涉及的水量似乎相当小。湿度波动的可能性也使我们以涉及的最小水损失从空气收集器重新获得CO2。 
其它强碱1型和2型官能离子交换树脂可在商业上从不同的供应商包括道公司，杜邦公司和罗门哈斯公司获得，也可有利地用于本发明，或者获取自制造商，或者遵照如美国专利No.6,503,957的教导形成异质离子交换膜。 
图1说明了本发明的第一种实施方式。将主离子交换过滤材料4设置在再循环周期上。当打开阀门V1并推动它穿过排气口2时，主泵1或第二泵(未显示)可用于除去系统中大部分空气。这时阀门V1关闭，并通过打开阀门V2和V3将二级离子交换捕获树脂转入系统。二级离子交换树脂可用于提供湿度，并可能提供一些热。热蒸汽刺激CO2从主离子交换过滤材料4释放，其然后在二级离子交换树脂上被捕获，该二级离子交换树脂与CO2分压仍处于不平衡状态。系统中水的体积保持很小，因为它可以再循环且不被二 级树脂吸收。当CO2从主离子交换树脂材料14卸载，并被二级离子交换树脂吸收时，大部分水循环通过装置。可被转移或吸收的水量远小于被转移的CO2量。循环结束时，主离子交换过滤材料14得到更新而二级离子交换捕获树脂载有CO2。 
该系统可以用于从空气捕获介质，如二级树脂上的离子交换树脂中转移CO2，而不必洗涤或润湿主树脂。这具有两个优点。首先，主树脂不直接暴露于过去使用的并在我们上述PCT申请PCT/US061/029238中描述的化学品例如胺中。第二，我们已经看到湿树脂直到干透才对吸收二氧化碳有效。因此，它有利于避免材料的润湿，从而以这种用低压蒸汽洗涤树脂的方式运作。蒸汽压力可小于100pa，并由此在类似环境值的温度下达到饱和。然而在较高温度较高蒸汽压力下，CO2交换明显加快。升高温度的缺点是增加能源消耗。 
这里描述的设计是更广泛的一类设计中的具体实例，该类设计中用能吸收CO2而不吸收水的任何其它吸附剂材料代替二级树脂。这种吸附剂可包括液体胺，离子液体，固体CO2吸附剂如锆酸锂、硅酸锂、氢氧化镁或氢氧化钙，或任意广泛类别的能从含水蒸汽和CO2的气体混合物中吸收CO2的化学或物理吸附剂。该中心概念在于利用湿度波动而不是压力或温度波动来从主吸附剂中除去CO2，而不带它与二级吸附剂直接物理接触。 
在温室中用于提高作物产量的应用
如上所述，通过提高温室气体中的二氧化碳水平可提高温室中的作物产量。本发明将二氧化碳引入温室而不燃烧向空气排放矿物燃料CO2的燃料。更具体地，我们已发现可以采用湿敏离子交换树脂来从外界空气捕获CO2，然后通过暴露树脂于暖湿温室空气中将CO2释放在温室内。 
位于温暖的例如美国西南发现的沙漠气候中的温室，外界CO2的负载可在温度较为凉爽的夜间进行，这样可提高CO2的吸收能力。在较凉爽的气候中，温室部分依赖辐射供暖，我们的CO2负载系统不需要让冷空气进入以补充CO2，由此降低了采用矿物燃料消耗来供暖的需要，除非温度下降很低使得燃料加热成为必要。 
在一种实施方式中，我们采用了由湿敏离子交换活性材料制成的几种过滤器。在循环的一部分将过滤器暴露于由自然气流通过热对流或鼓风机驱动的外界空气中。优选避免鼓风机，因为它们增加不必要的能量损耗。在循环的第二部分，来自温室内的潮湿空气优选被驱动(如通过鼓风机)穿过过滤材料，然后释放CO2进入温室大气。由于温室的气候控制无论如何将典型地依赖风扇系统，所以很少有或没有能量损耗。 
因为植物在夜间呼吸，在一些温室设计中，有可能通过牵引温室空气穿过过滤器以从温室空气中除去CO2。然后该过滤器可以暴露于较高湿度下以促进白天释放CO2进入温室。 
在一种实施方式中，如图2A和2B所示，过滤器单元10靠近温室的外墙12，外部空气或温室空气选择性由此处通过，视情况而定，可经过绕枢轴旋转安装的墙板14。此外，如图3A和3B所示，过滤器材料10可位于温室顶18外或靠近温室顶18，外界空气或温室空气选择性由此通过，视情况而定，可经过绕枢轴旋转安装的顶板20。 
在本发明的另一种实施方式中，如图4所示，过滤器单元10可从温室外移到温室内，在温室外它们从空气中提取CO2，在温室内它们释放捕获的CO2。这样做的一个可能的选择是将过滤单元安装在绕枢轴旋转安装的墙或顶板22上，墙或顶板22可以翻转，以便将温室外的过滤单元暴露于温室内，反之亦然。温室内的过滤单元可以通过鼓风系统使空气从中吹过。外部的过滤单元暴露于周围空气中。在一种优选的实施方式中，如图4所示，外部的过滤单元10靠近由太阳能驱动的对流塔24的底端。优选地，入口安装在对流塔的底端，在此凉空气通过自然对流进入并向塔上方流动。 
在另一种实施方式中，如图5所示，将过滤单元10移入或移出温室，如悬停在轨道26上。 
参考图6，温室还有另一种选择是将对流塔作为双重玻璃墙设在温室外部，并利用产生的对流流体来收集外部CO2。该双重墙还有利于降低白天对内部的热负荷，并由此降低空气交换的需要，这样使温室有可能维持高水平的CO2。该双重墙还可减少夜间的热损失。 
在该实例中，可设置防护玻璃表面40来保持热远离玻璃房42的主顶， 产生屋顶表面上方周围空气的对流流体44。周围空气的对流穿过CO2吸收过滤介质46，该介质可以通过某种机构，如旋转顶板48与第二类似的过滤介质50交换位置，在此由温室内部鼓风机52驱动的空气穿过过滤介质，当过滤介质暴露于温室外部的周围空气时，释放捕获的CO2。由于温室内的空气是潮湿的，CO2很容易从过滤介质中释放，并增加了温室中可用的CO2。 
这种单元的一个优点在于它可以不燃烧燃料在高水平CO2下运转。因为CO2传送到温室内而没有向温室内吹入空气，这就提供了减少温室内外之间空气交换的可能性，由此改善了温室的热管理和水分管理。 
在本发明第二种示范实施方式中，CO2被提取并传送到藻类或细菌生物反应器。这可以利用常规的CO2提取方法或通过利用如我们上述PCT申请所揭露或此处所揭露的改进提取方法，例如通过湿度波动来完成。湿度波动有利于提取的CO2传送到藻类，因为物理分离允许使用任何收集器介质而不关注该介质和海藻培养溶液之间的相容性。气态CO2的转移允许选择任何藻类物种，包括巨型和微型藻，海洋或淡水藻。因此，所要培育的藻类物种的选择可以仅依赖于收集器所在地的环境因素和水质。例如，使用的藻类物种可选自天然生长于某地的藻类，它们会独特地适应当地的大气、环境和水质条件。 
以气态形式转移捕获的CO2有两个优点。第一个优点是收集器介质和/或收集器再生溶液将不接触藻类培养溶液和/或藻类。第二个就是所有种类的藻类都能吸收气态CO2。 
根据具体藻类的CO2耐受，可用泵连续抽取富含CO2的空气，穿过几个藻类培养，以便降低CO2耐受和增强CO2吸收效率。此外可将空气稀释到最佳CO2浓度。 
参考图7，本发明的一种实施方式利用了使用湿度波动从收集器介质驱走气态CO2这一事实。湿度波动将捕获的CO2以气态CO2形式从收集器110转移到藻类培养116。当遇到湿度增加或用水弄湿时，载有CO2的阴离子交换收集器介质将放出气态CO2。当供应CO2的气体流的湿度下降和/或收集器介质变干时，收集器介质将吸收更多的气态CO2。 
本发明在收集器介质和藻类培养上方提供了一个公用的顶部空间。当物 理地分开收集器介质和藻类培养液时，这就将藻类暴露在气态CO2中。然后增加封闭的顶部空间容积内的湿度。此外可选择将收集器介质润湿。从收集器介质放出的CO2很快扩散到整个顶部空间并接触藻类培养液的表面。 
然后经气体扩散或用再循环泵使顶部空间气体鼓泡通入藻类培养液，将CO2转移到藻类培养。随着藻类从顶部空间除去CO2，收集器介质继续排气直至达到平衡。藻类培养液可机械搅拌。所有其它营养素和光照视需要被提供给藻类。然后可将藻类收集到藻类收获机120中。 
润湿的收集器介质上方顶部空间的CO2浓度达到20％；或0.2大气分压。该浓度可通过收集器介质和顶部空间的体积/体积比率来调节。在湿度波动/润湿期间，收集器介质还能释放60％的捕获CO2。 
此外，为了转移CO2也有可能从收集器介质体积中用泵抽气通入藻类培养。如果藻类池暖而潮湿，来自藻类池的水分再次通过湿度波动机制足以刺激CO2从干树脂中的释放。 
参考图8，在本发明的另一种实施方式中，周围空气中的CO2浓度能使离子交换介质吸满CO2达到CO2被束缚为碳酸氢根离子的水平。本发明使用碱性溶液提供收集器介质的再生。在再生过程中，溶液中的阴离子组分变为近100％的碳酸氢根。水性碳酸氢盐溶液在大气条件下不稳定，并释放气态CO2。通过利用再循环泵使顶部空气鼓泡进入溶液可增强气态CO2排放。 
一种可选实施方式在收集器再生溶液和藻类培养液上方设置了公用顶部空间。当分开再生溶液和藻类培养液时，藻类暴露在气态CO2中。在其它方面，该顶部空间运转与上面所讨论的收集器介质顶部空间类似。 
参考图9，本发明的另一种可选实施方式使用电渗析(ED)方法来从负载的收集器溶液中释放气态CO2。然后释放的CO2被转移到藻类培养216。气态CO2通过电渗析(ED)方法从收集器210转移到藻类培养的优点是在该方法的所有阶段，收集器溶液或吸附剂与藻类培养液在物理上相互分离。这就防止两种溶液的混合，并且还防止溶液之间的离子交换。ED方法与湿度波动方法相同。并且在湿度过程时，物理分离允许使用任何收集器介质和任何藻类而不考虑介质和藻类培养液之间的相容性。 
本发明的一种可选实施方式利用了可用ED方法将气态CO2排出收集器 再生溶液这一事实。在ED方法中，负载的收集器再生溶液分成两股流进入ED单元(ED cell)214。质子跨过二级膜236加到第一股流，无机碳以CO2形式排出，而钠离子穿过阳离子膜234转移进入第二股流。除了钠离子外，氢氧根离子也穿过另一二级膜236加到第二股流中，由此将该股流中的碳酸氢盐中和为碳酸盐。 
第一股流以水或稀碳酸氢钠溶液形式退出ED单元，而第二股流以浓缩的碳酸钠溶液形式退出。将两股流合并以形成新鲜的收集器溶液。从第一股流排出的气态CO2鼓泡进入藻类培养并固定为生物量。 
从盐水中除去无机碳时，该溶液变得碱性更强，需要加入额外的碳酸氢盐来维持pH。过滤使我们能回收一些流体，并由此从生物器中回收水和钠。在一种具体实践中，电化学单元(electrochemical cell)将在两个分开的流体循环之间运行，一个相当偏碱性，在收集器和电化学单元的碱性侧之间运行，另一个在藻类反应器和电池酸性侧之间在近中性pH下运行。碳酸从单元的碱性侧转移到酸性侧。该步骤再生了洗涤液并用CO2重新装载该流体。 
通过在藻类中加入碳酸氢盐吸附剂，可以将CO2从吸附剂中除去而不必先将CO2转化回到CO2气体。而且，通过为空气捕获方选择合适的吸附剂材料，洗涤液的pH可保持相当低，而且如果使用能耐受相当高pH的藻类，需要由电渗析构成的pH差异变得相当小，在一些实施中，可以完全除去渗析单元。 
参考图10，本发明的另一种实施方式用ED方法来降低收集器溶液中的碳酸氢盐浓度并增加藻类培养液中的碳酸氢盐浓度。收集器溶液以碳酸氢盐形态进入ED单元214，而藻类培养液以碳酸盐形态进入ED单元。当这些流体退出ED单元时，收集器溶液为碳酸盐形态而藻类培养液为碳酸氢盐形态。 
由于阳离子从藻类培养液转移到收集器溶液，藻类溶液被降低到其常态的大约一半；而收集器溶液大约是其常态的两倍。为了弥补钠的不平衡，一半有负载的收集器溶液(碳酸氢盐形式)从收集器被直接转移到藻类培养。 
在根据本发明的方法方案中，阳离子穿过阳离子交换膜234从藻类溶液转移到收集器溶液。藻类培养液主要包含钠离子，但也有钾、镁和钙离子以及微量的其它金属离子。镁和钙的潜在转移应该受到关注，因为这两种离子 形成相当不溶的碳酸盐和氢氧化物。这些盐的形成也被称为障眼物(scaling)，能够破坏ED单元的膜和/或收集器介质。 
在藻类生长周期开始时，将钙和镁加到藻类培养中作为矿质营养素。随着藻类生物量增加，钙和镁被吸收进入生物量，它们在藻类培养液中的浓度减小。同时，随着碳酸氢盐溶液转变为碳酸盐溶液，培养液pH增加。如果镁、钙和碳酸根离子的存在超过它们的溶度积，化学沉淀将进一步减小镁和钙离子浓度。 
具有减小的钙和镁浓度以及高pH的用尽的培养液被送入ED单元。培养液在那里从碳酸盐转变为碳酸氢盐溶液，并且其pH相应减小。随着碳酸根离子浓度减小，该溶液可保持更多的钙和镁。因此障眼物不大可能在ED单元的这部分发生。 
然而，同时，包含钙和镁的阳离子从藻类培养液216被转移到ED的半单元(half-cell)收集器溶液。在这个半单元中，来自收集器的碳酸氢盐溶液转变为碳酸盐溶液：碳酸盐浓度和pH增大。此外，用反渗透单元224可从碳酸氢盐溶液中除去过量的水。 
设计该方法的目的是退出的收集器溶液的pH接近进入的藻类溶液的pH。因此，只要一切保持平衡障眼物就不应该发生。然而，保持完美的平衡在宏观尺度上可能并不总是实用，并且在ED单元内的微观尺度上也不可能。有可能在膜表面形成具有增大的氢氧根或阳离子浓度的微小层或囊(layers orpockets)。膜表面的增大的浓度可能在收集器溶液半单元中引起障眼物。 
为了将障眼物减到最少，钙和镁阳离子的流量必须减到最小。这在从海水生产盐，氢氧化钠生产，以及通过电渗析处理脱脂牛奶中都是众所周知的问题(T.Sata，1972；T.Sata et al.，1979，2001；J.Balster，2006)。为了将流量减到最小，将两个半单元分开的阳离子膜必须为可选择的单价离子。一般地，强酸性阳离子交换膜二价比单价离子显示更大的运输数量。据推测这是由于对带负电荷的固定离子交换位点的较高的静电吸引。现有技术表明随着膜上电荷密度降低二价阳离子的运输数量减少。 
已经有两种商业上可购到的高单价阳离子选择性膜被确定特别适用于这一过程。一种膜是由旭玻璃公司(Asahi Glass)生产，商品名为Selemion CSV。第二种是由德山苏打公司(Tokuyama Soda)生产，商品名为 CIMS。Selemion CSV的运输数量(t)为：t(Na)＜0.92且t(Ca，Mg)＜0.04。Neosepta CIMS的运输数量为t(Na，K)＝0.92且t(Ca，Mg)＝0.10。运输数量被定义为电渗析期间阳离子的等价流量除以总等价流量。 
本发明的该方面用单价阳离子选择性膜来使多价阳离子从藻类培养液到收集器再生溶液的转移最小化。任何随时间形成的障眼物将用酸溶液除去。 
在进入ED单元前，藻类培养液和收集器溶液都被过滤以避免膜被颗粒污染。通过有机清除离子交换树脂，有机分子将从藻类培养液中被清除。 
参考图11，在本发明另一种实施方式中，通过将有负载的收集器溶液310加入藻类，从空气中捕获的CO2也被转移到藻类。有负载的收集器溶液富含碳酸氢钠。将营养素添加到收集器溶液中，它就成为藻类的原料。在本发明该实施方式中溶液原料不能再循环，使得该收集器溶液成为消耗品。 
在该方法中，随着越来越多的碳酸氢钠被加入，藻类培养液316含盐量将增大。碳酸氢钠在藻类生长过程中被转变为碳酸盐。为了降低碳酸盐浓度和放慢盐化，剩余的一些营养素可作为酸而不是作为钠盐被加入，这将会使碳酸根离子转化为碳酸氢根并使钠增加最小化。 
此外，碳酸氢钠吸附剂可直接加到藻类反应器以便为藻类提供CO2，随着碳酸钠被返回空气提取站，藻类在进一步处理中被除去。 
许多藻类可以利用碳酸氢钠作为碳源。另外比起CO2，一些藻类优选碳酸氢盐作为碳源。这些通常是产于碱性湖泊的藻类，在那里无机碳主要以碳酸氢盐存在。这些藻类可以忍受pH值8.5-11的大幅波动。其它藻类可用HCO3-作为碳源，但需要pH值范围低于pH＝9，这就需要通过鼓泡CO2通入碳酸氢盐/碳酸盐溶液。 
藻类利用碳源通过光合作用生产生物量。因为光合作用需要CO2而非碳酸氢盐，所以藻类催化下列反应： 
HCO3 -→CO2+OH-
在HCO3 -存在下，将变成： 
HCO3 -+OH-→CO3 -2+H2O 
藻类在碳酸氢盐溶液中的生长导致溶液发生下列变化：(1)HCO3 -浓度 的降低；(2)CO3 -2浓度的降低；以及(3)pH值的增加。 
本发明的另一种实施方式将藻类培养液用于收集器再生。碳酸盐形式的收集器介质可以从周围空气中吸收气态CO2，直到介质的阴离子组分为接近100％的碳酸氢根。在这种状态下，收集器介质充分负载且CO2吸收即将停止。碳酸盐溶液可用在再生中，以使有负载的收集器介质通过离子交换返回到碳酸盐形式。通过与充分负载的收集器介质进行离子交换，再生溶液中的离子组分可以从100％碳酸根变为近100％碳酸氢根。在逆流再生过程中，当碳酸盐再生溶液转变为碳酸氢盐溶液时，收集器介质中可加入碳酸盐形式。当再生溶液为碳酸氢盐溶液时它被充分负载，因为它不能从收集器介质中除去任何碳酸氢盐。 
将藻类引入该过程，以通过碳酸氢盐脱水和中和(参见上文)从负载的再生溶液中除去捕获的CO2。藻类将释放的CO2用于生物量生长。再生溶液从碳酸氢盐变回到碳酸盐溶液。 
在这个过程中，碳酸盐再生溶液和收集器介质被再利用，而周围空气的CO2变为藻类生物量，如图11所示。 
该方法提供了离子交换收集器介质吸收空气CO2的循环。在吸收期间，收集器介质从碳酸盐变为碳酸氢盐形式。然后再生溶液从有负载的收集器介质中引出CO2。这次交换中，收集器介质转变回到其碳酸盐形式，而再生溶液从碳酸盐变为碳酸氢盐溶液。最后，通过将CO2固定在生物量中，藻类从有负载的再生溶液中除去气态CO2。该步骤中，藻类催化从碳酸氢盐到CO2和碳酸盐的反应。CO2的碳被绑定到藻类生物量中。碳酸盐留在溶液中。然后由此产生的再生溶液成为碳酸盐形式。 
在本发明的另一种实施方式中，藻类培养液被用作收集器再生溶液。这意味着收集器再生溶液除了碳酸盐将包含其它藻类所需的营养素。其中在与收集器介质进行离子交换期间，营养素是与碳酸盐阴离子发生竞争的阳离子。 
该方法中将不使用硅藻，因为它们需要硅土，而硅土不能被碳酸盐洗液从收集器介质中充分除去。 
在藻类培养基中发现的其它典型的阴离子营养素为：硝酸根(NO3 -)、硫酸根(SO4 -2)和磷酸根(PO4 -3)。磷也可能根据pH以二元(HPO4-)或一 元(H2PO4 -)磷酸根存在。 
用于典型藻类培养基的硝酸根、硫酸根和磷酸根浓度为： 
  营养素  Bold培养基摩尔浓度(M)  Zarouk培养基摩尔浓度(M)
  NaHCO3    0.2
  NaNO3  0.00882  0.029
  MgSO4-7H2O  FeSO4-7H2O  K2SO4  总S  0.0003   ∑＝0.003  0.0008 0.0018 0.0058 ∑＝0.0084
  K2HPO4  KH2PO4  总P  0.00043 0.00129 ∑＝0.00172  0.0029 ∑＝0.0029
然而，现有技术已经表明藻类可以在比典型培养基所含的低的多的营养素浓度中生长。 
为了消除营养素浓度对收集器介质的影响，将含营养素的再生溶液混合如下：0.14M CO3 -2，0.04M NO3 -，0.0017M S04 -2和0.0017M H2PO4 -1。这些代表藻类培养基中发现的最高浓度，因此是最坏的情况。 
然后，用这种“最坏情况”的溶液冲洗收集器介质直到溶液和收集器介质之间达到平衡。在碳酸盐溶液的pH时，磷以二元磷酸盐(HPO4 -2)形式存在。二元磷酸盐呈足够碱性足以吸收CO2。因此，收集器介质上的二元磷酸盐阴离子的存在将不会降低介质的CO2的吸收能力。可以确定的是，平衡时收集器介质总交换位点的约50％被碳酸盐和磷酸盐离子占据，而另50％被硝酸盐和硫酸盐占据。虽然其它营养素超过碳酸盐，但它们没有完全取代它；相反，达到了负离子平衡，它将不利用额外的溶液体积改变收集器介质。 
实验表明在最坏的情况下，收集器介质吸收CO2的能力失去大约50％。然而，如上面引用的研究所确定，溶液中营养素的浓度在藻类生长期间会大大衰竭。例如，硝酸盐是目前为止无机碳之后最丰富的营养素，可达到0.002M，仅是最坏情况下实验所用浓度的5％。磷酸盐降低到最坏情况下的 45％。 
此外，用营养素耗尽的溶液洗涤过的收集器介质将损失约20％吸收CO2的能力。因此有可能使用收集器介质，并用来自藻类生长介质的碳酸盐溶液洗涤它。 
在代谢或衰竭期间，藻类将分泌或释放有机化合物进入溶液。该溶液用于收集器介质之前，将从溶液中清除这些有机物。有机物清除可用吸附型的离子交换树脂或其它方法处理。 
这个方法不使用硅藻属，因为它们需要硅土，而硅土不能用碳酸盐洗液从收集器介质中充分除去。 
本发明实施方式优选的藻类具有以下特征：它们适应高离子强度液体；它们能在约8.5-11的pH范围内生长；它们能耐受渐进的pH变化；它们能用碳酸氢盐作为其碳源；它们需要极少的硅土作为营养素；它们能够将溶液pH从8.5改变到11或以上；它们能将营养素浓度减小到低水平；它们能用于生化、农业、水产业、食品、生物燃料等。 
良好的候选对象为，但不限于：生活在碱性水中的藻类，如钝顶螺旋藻(Spirulina platensis)、梭形螺旋藻(Spirulina fusifomis)、螺旋藻sp.(Spirulinasp.)、微小四角藻(Tetraedron minimum)等。 
该实施方式有许多其它选择。将有负载的收集器介质(营养素耗尽的碳酸氢盐溶液)和新鲜的营养素一起加到藻类培养中；藻类培养利用碳酸氢盐作为其无机碳源，通过将约50％碳酸氢盐的碳吸收进入其生物量并将剩余的50％改变为碳酸根阴离子。同时，藻类培养耗尽了溶液中营养素浓度。培养液被过滤，收获生物量，向CO2收集器分流营养素耗尽的溶液。营养素耗尽的溶液被清除掉有机物和其它对收集器介质有害的物质。此时富含碳的该溶液可用于再生该收集器。该方法中每个碳酸根阴离子被两个碳酸氢根阴离子取代，直到收集器溶液已负载。有负载的收集器溶液和上述新鲜的营养素一起被加到藻类培养液。 
该方法可以连续环路或分批过程运行，考虑位置、藻类类型等看哪一种更实际。该方法可采用已经使用并经证明的藻类培养技术或新技术。例如，已证明在加利福尼亚州、夏威夷、菲律宾和墨西哥以及其它地方的露天池塘 可成功培养螺旋藻、小球藻、布朗纤维藻和其它物种。根据国家可再生能源实验室(NREL)，露天池塘例如所谓的“比赛池(race ponds)”是栽培大量海藻生物量的最经济的方法。 
培养可使用太阳能、人工照明或两者都有，取决于藻类物种和操作地点。藻类培养液可搅拌以便将藻类返回最强光入口区。或者光可以通过镜子、光纤或其它手段被带入藻类培养。 
藻类可以悬浮在溶液中或固定不动。当悬浮时，藻类遵循它们自身的生长模式：单细胞、群生、簇团等。自然生长模式与所用的技术可能不是最佳匹配。例如，小的单细胞藻类可能需要精细的收获方法。 
如果将自身附在表面上，藻类可自然固定生长，如巨型藻。或者藻类也可以被固定：用k-卡拉胶或海藻酸钠成珠，在聚氨酯泡沫上，在过滤材料上，或作为生物膜固定在柱填充物上，或其它方式。 
在固定状态下，藻类仍然可以悬浮，如以珠子形式，并随着溶液流动。此外，当溶液渗透经过时，固定的藻类可在圆柱或其它装置中静止。 
在本发明的另一种实施方式中，收集器介质被浸到藻类培养物(AlgarCulture)中。这可以以分批方法或连续方法完成。在分批方法中，将收集器介质一批批轮流浸入藻类培养物和暴露于周围空气。在连续方法中，收集器介质沿着路径连续移动，其在该路径上交替浸入藻类培养物或暴露于空气。最简单的实践将是围绕其中心连续旋转的收集器介质的圆盘。该圆盘在藻类培养物中淹没至其中心点，这样，在任何时候，收集器介质的一半淹没在液体中而另一半暴露在空气中。 
在本发明该实施方式中，收集器介质可在高养分含量和低营养素含量时潜在地浸入藻类培养液。因此，收集器介质的CO2能力是其总能力的50-80％。空气暴露时间可以调整以考虑能力的降低。 
参考图12，本发明的另一种实施方式揭露了通过洗涤有负载的收集器介质中的藻类，从收集器溶液转移到藻类的碳酸氢钠。但收集器溶液中不添加营养素。替代地，通过一个两次分离洗涤循环将营养素提供给藻类，该洗涤循环由富含营养素缺乏碳的溶液组成。 
在这个过程中，藻类将交替着浸入缺乏营养素的碳酸氢盐溶液(有负载 的收集器溶液)和缺乏无机碳的营养素溶液326。洗涤之间将采用短的冲洗周期。冲洗将被加到溶液的预洗涤中。 
针对所使用的藻类种类，营养素和碳酸氢钠的洗涤周期将被优化。也可混合或依次连续使用一个或多个藻类种类以优化碳酸氢盐溶液(有负载的收集器溶液)向碳酸盐溶液(新鲜的收集器溶液)的转化。在应用于收集器介质之前，新鲜的收集器溶液可过滤以除去颗粒，并清除有机分子或其它有害内容物。 
该方法可进行设计以利用悬浮的藻类或固定的藻类。如果藻类是悬浮的，该方法必须以分批方法运行，藻类必须从溶液中被过滤。为易于过滤，藻类可以“固定”在悬浮珠上，以便增大粒径。 
涉及固定藻类的方法可使用自然生长固定的藻类，例如将自身附在表面上的巨型藻，或形成生物膜的微型藻等。 
除了本申请披露的其它方法外，藻类还可以固定在圆柱、倾斜管道、池塘或其它容器内。可安置这些容器以允许重力流体流动。固定可发生在容器壁和底部和/或安装在那里的如板、包等结构上面。视需要可通过自然光照、人工光照、镜子、光纤等把光带入容器。 
参考图13，本发明的另一种实施方式将气态CO2穿过疏水微孔膜434从有负载的收集器溶液410转移到藻类培养液416。气态CO2可穿过疏水膜从碳酸氢盐溶液转移进入碳酸盐溶液；且两种液体流之间的CO2分压差足以驱动该转移。可注意到，水的转移是从较稀溶液到较浓溶液。由于膜是疏水性的，所以转移的是气态水分子。 
经过简化，该方法可描述为被微孔的疏水膜分开的两个半单元。第一半单元438具有负载的收集器溶液(碳酸氢钠溶液)；而第二半单元418具有藻类培养(含营养素和藻类的碳酸氢钠溶液) 
收集器溶液半单元反应的定义如下： 
2HCO3 -(aq)→CO2(g)+CO3 -2(aq)+H2O 
接着，CO2(g)穿过膜扩散进入藻类培养半单元。藻类培养半单元中的反应将遵循以下两种方式之一： 
藻类消耗CO2(g) 
或 
CO3 -2(aq)+CO2(g)+H2O→2HCO3 -(aq) 
和 
HCO3 -(aq)+OH-→CO3 -2(aq)+H2O 
从半单元反应可以看出，随着碳酸氢盐通过释放气态CO2反应生成碳酸盐，收集器溶液的pH不断增大。在平衡体系中，通过藻类生长气态CO2被固定在生物量中时，藻类培养液将不改变其pH。藻类培养将优选接近碳酸盐溶液。该条件将使收集器溶液和藻类培养之间的气态CO2分压差最大化。 
两个半单元的物理安排可以采取多种形式，包括但不限于在此描述的几种安排。每种安排都将优化液体膜接触区域和溶液体积的比率。一般来说，收集器溶液运行穿过浸在藻类培养中的膜通道是有利的，因为这将为藻类培养提供光照。在膜管道含有藻类培养的情况下，导管内将有光照供给。 
膜管道可以有多种形状。例如，它们可以是平行的膜片，形成夹在膜之间的溶液的片流。或者它们可以是管状，管横截面采取不同形式，如圆形、正方形、长方形、波浪形等。管可以形成螺旋或其他形状以增大它们穿过溶液的路径长度。 
该过程可以分批程序、连续环路方法或其组合来运行。视需要将提供光照和营养素。 
在纯分批方法中，一批被带入膜的有负载的收集器溶液与一批藻类培养接触和离开以达到平衡。 
在纯连续环路方法中，两种溶液都在连续环路中流动。有负载的收集器溶液将沿着膜路径流动，穿过该膜路径将气态CO2转移到藻类溶液中；从那里它进入收集器介质的再生系统，在该系统中它负载CO2然后再进入膜导管。藻类溶液将随着藻类固定气态CO2流过膜路径；从那里它将进入收获系统420，其中一些或所有藻类被从溶液中除去然后再进入膜系统进行新的CO2固定和藻类生长。连续流体或环路程序可用这两种流体的并行流动或逆流流动。 
转移CO2穿过疏水性膜的主要优点在于离子不能跨过藻类培养进入收集器溶液。藻类溶液中含有的阳离子包括碱土金属，随着pH增大它可以沿收 集器溶液路径产生障眼物。藻类溶液中含有的阴离子，如硝酸根和硫酸根，在收集器介质上与碳酸盐竞争，由此降低收集器介质的CO2容量。因此，阻止离子进入收集器溶液是有利的。因为构成藻类营养素的离子不能越界进入收集器溶液，藻类培养的营养素内容物可以永久保持在用于藻类生长的最佳浓度。 
另外，现有技术揭露了疏水膜，这些膜也是疏有机性的，并且阻碍有机分子从藻类溶液向收集器溶液的转移。任何可能被转移到收集器溶液的有机物将在它进入收集器介质之前被从收集器溶液中除去。例如，这可通过清除落在离子交换树脂上的有机化合物来完成。 
该膜因为其疏水性、CO2渗透性、疏有机性以及水突破压而被选中。优选的用于该方法的藻类为那些在碳酸盐溶液中生长旺盛并能利用气态CO2和碳酸氢盐的藻类。然而，也可使用其它藻类来优化全过程。 
参考图14，本发明的另一种实施方式将碳酸氢盐穿过阴离子渗透膜从收集器溶液410转移进入藻类培养液418。收集器溶液与阴离子渗透膜434的一侧相接触，而藻类培养液与膜的另一侧相接触。 
溶液沿着浓度梯度交换阴离子。为了优化该阴离子交换，可让溶液在逆流中运行通过膜。该溶液也可以顺流运行以优化该系统的其它部分。此外，该方法可设置为分批方法而不是连续流方法。 
藻类培养溶液可被送入阴离子交换过程，和悬浮在溶液中的藻类一起或没有藻类。参见图15。溶解的有机化合物可在进入膜腔室之前从藻类培养溶液中除去。 
如上所述，营养素影响应用。如果将包括藻类在内的整个藻类培养送入膜交换中，营养素浓度将很高，收集器溶液将获得高的营养素浓度。这可能导致收集器介质的CO2吸收能力降低达50％。如果将没有藻类的培养液送入膜交换，该过程可以设定为将营养素耗尽的溶液送入，在该情况下收集器能力可能会降低达20％。 
两种溶液中的阳离子不会发生交换，这大大降低了产生障眼物的可能性。 
此外，我们可以将捕获的CO2直接注入藻类-围兜反应器合成燃料的生产单元。一种具体的简单设计是设置运载湿敏离子交换树脂的桨轮或圆盘等， 将它们首先暴露在水面以上，在此从空气中提取CO2，然后缓慢旋转使部分浸入水面以下，在此释放CO2以便为CO2提供高的空气/水转移比率。 
参考图16，在另一种实施方式中，有可能在提取站140用弱碱性的洗涤水喷淋离子交换树脂；类似第一种实施方式，以弥补水从生物反应器的蒸发或生产损失。随着洗涤水从主树脂上方淌下，它将带起被束缚的CO2并将其滴入生物反应器系统142。 
此外，如图17所示，树脂142可在夜间加入水中以保留由于呼吸作用可能从藻类损失的CO2。由此通过防止夜间CO2从生物反应器的释放，我们能改善藻类的CO2吸收效率。在这种实施方式中，二级树脂在该系统中起碳缓冲剂的作用。在夜间这种缓冲剂储存藻类释放的CO2，而白天它向藻类提供CO2，而它的CO2含量可由空气收集器所收集的CO2来补充。一旦被捕获，CO2就从再生主树脂时所用的较浓洗涤液转移至树脂。为使藻类处于空气收集器之外而进行的水过滤一般来说不成问题，因为在循环之间，空气端的主树脂被设计为完全干透。 
这种向二级树脂的转移也可以不必在封闭潮湿系统中直接接触，如图1所示，通过进行湿度波动来完成，该湿度波动避免与水直接接触。虽然这种系统失去了上述不把CO2带回到气相的优点，但它具有不用化学品而使藻类池塘缓冲于恒定pH的其它优点。 
在本发明的优选实施方式中，如图18所示，为了降低水损失，增加收率并更好地限制藻类，我们采用了带有光照集中器152的生物反应器150。这种系统可由被镜子或反射镜系统包围的玻璃管建成，该系统馈入可散布光穿过大的液体容积的光纤光管。利用带有光照集中器的生物反应器的优点在于它们大大降低了水表面并因此降低水损失。因此，可以就近收集CO2而不直接干预藻类反应器。实际的空气收集器可以利用镜像系统来引导空气流动。 
通常藻类在光照汇集的时候固定CO2，在黑暗周期时呼吸CO2。通过将额外的收集器介质在关键时机添加到该系统，将CO2捕获。例如，收集器介质可以浸入藻类培养。在这种情况下，它将在呼吸时随着培养液pH降低储存碳酸氢盐和释放碳酸盐，并且它将在光合作用时随着培养液pH增大释放碳酸氢盐和储存碳酸盐。 
收集器介质也可以放置在藻类培养附近的空气空间以吸收从培养液中释放的CO2。这在封闭结构中将特别有效。放置在培养液附近的收集器介质可利用上述方法再生。 
本申请旨在包括在本专利中描述的无机碳转移方法的任何组合，视需要利用任意组合的藻类培养来优化该方法。优化包括但不限于在任何气候条件或可控制的气候条件下，优化碳转移效率、碳转移速率、生物量的市场价值(如油含量、淀粉含量等)、藻类生产效率以及藻类生长速率。 
虽然已经结合采用湿敏离子交换树脂材料用于从周围空气中提取CO2和通过湿度波动将提取的CO2传送到温室这一优选实施方式对本发明进行了说明，本发明的优点可以根据我们上述的PCT申请PCT/US05/29979和PCT/LTS06/029238中(Attorney Docket Global 05.02PCT)描述的几种方案，通过用吸附剂从空气中提取二氧化碳，并适当操控该吸附剂将提取的CO2释放到温室来实现。 

Claims (26)

1.一种从周围空气中除去二氧化碳的方法，包括将周围空气与吸附剂接触以从空气中吸收二氧化碳，其中吸附剂具有取决于湿度的二氧化碳保持能力，和通过将该吸附剂进行润湿或湿度波动从吸附剂释放二氧化碳，以及将释放的二氧化碳传送到受控环境中的步骤。
2.如权利要求1所述的方法，其中吸附剂包括强碱性、湿敏离子交换树脂。
3.如权利要求1所述的方法，其中受控环境为温室内或者含有藻类培养物的生物反应器。
4.如权利要求2所述的方法，其中离子交换树脂为异质离子交换膜的组分。
5.如权利要求4所述的方法，包括使用前首先水合然后干燥该膜的预处理离子交换膜的步骤。
6.如权利要求5所述的方法，其中离子交换树脂包括强碱性1型或2型官能离子交换树脂。
7.如权利要求3所述的方法，其中生物反应器具有渗滤机构，用于携带释放的二氧化碳与藻类培养物接触。
8.如权利要求3所述的方法，其中生物反应器具有顶部空间，用于携带释放的二氧化碳与藻类培养物接触。
9.如权利要求8所述的方法，其中吸附剂在浸入藻类培养物时释放二氧化碳。
10.如权利要求9所述的方法，其中藻类随后被浸入营养液。
11.如权利要求1所述的方法，其中为除去的二氧化碳产生了碳积分。
12.一种从空气中提取二氧化碳的方法，包括：
设置湿度敏感的第一吸附剂的储藏室，
将空气在第一H2O分压下与第一吸附剂接触，此时二氧化碳被吸收在第一吸附剂上，和
提高H2O分压，此时二氧化碳被第一吸附剂排出。
13.如权利要求12所述的方法，其中吸附剂包括强碱性1型或2型官能离子交换树脂。
14.如权利要求12所述的方法，进一步包括：
使第一吸附剂与第二吸附剂相互作用，此时二氧化碳从第一吸附剂吸收到第二吸附剂上；和
提高H2O分压，此时二氧化碳被第二吸附剂排出。
15.如权利要求14所述的方法，其中第一吸附剂和第二吸附剂各自包括强碱性1型和2型官能离子交换树脂。
16.如权利要求14所述的方法，其中第一吸附剂和第二吸附剂处于选择性地封闭环再循环系统中。
17.一种用于从周围空气中提取二氧化碳的装置，包括一吸附剂储藏室，该吸附剂暴露于周围空气中并且具有取决于湿度的二氧化碳保持能力，和用于将该吸附剂进行润湿或湿度波动以从吸附剂释放二氧化碳的工具。
18.如权利要求17所述的装置，其中吸附剂包括异质离子交换膜。
19.如权利要求18所述的装置，其中膜的离子交换树脂包括湿敏离子交换树脂。
20.如权利要求19所述的装置，其中离子交换树脂包括强碱性1型或2型官能离子交换树脂。
21.如权利要求17所述的装置，进一步包括将释放的二氧化碳传送到温室内或者传送到含有藻类培养物的生物反应器的工具。
22.如权利要求21所述的装置，其中吸附剂安装在建在温室墙壁内的可移动夹具上。
23.如权利要求21所述的装置，其中吸附剂靠近温室附近的对流塔的低端。
24.一种从周围空气中除去二氧化碳的装置，包括：
一提取器，包含用于从空气中除去二氧化碳的湿度敏感的吸附剂；
一分离站，用于分离二氧化碳和吸附剂；和
一传送系统，用于将二氧化碳从提取器传送到含有藻类的生物反应器。
25.如权利要求24所述的装置，其中分离站利用湿度波动分离二氧化碳和吸附剂。
26.如权利要求24所述的装置，进一步包括用于收获藻类的收获机。
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