CN107847847A - 用于从气流选择性去除硫化氢的交联大孔聚合物 - Google Patents
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Abstract
公开一种用于从天然去除硫化氢(H2S)的方法。此方法准备使包含H2S的天然气进料流通过吸附H2S的可再生吸附介质以提供H2S贫乏的天然气产物和H2S。本发明的可再生吸附介质是交联大孔聚合物吸附介质。
Description
技术领域
本发明大体上涉及可用于从气井流提取酸性气体的吸附剂。更确切地说,本发明涉及一种交联大孔聚合物吸附剂和用于从天然气流去除硫化氢气体的方法。
背景技术
来源于天然气储层、石油或煤的流体流通常含有大量杂质形式的酸性气体,例如二氧化碳(CO2)、硫化氢(H2S)、二氧化硫(SO2)、二硫化碳(CS2)、氰化氢(HCN)、硫化羰(COS)或硫醇。这些流体流可为气体,来自页岩热解的烃气体、合成气体等;或液体,如液化石油气(LPG)和液化天然气(NGL)。
在天然气处理中,通常需要从进料流去除含硫化合物以满足一些要求,例如天然气管道H2S浓度极限通常设定处于或小于4百万分率(ppm)。
用于去除酸性气体的各种组合物和方法是已知的并且描述在文献中。依据气体的流动速率和气流中的H2S浓度,已将不同技术应用于H2S去除以优化经济。常规的天然气资源通常具有极大的气体流动速率(例如大于500百万标准立方英尺/天(MMSCFD)),在这些情况下,使用液体烷醇胺单元。通常,胺水溶液目前在吸收塔中在低温或高压下反向接触包含酸性气体的气态混合物。总体H2S处理成本由于规模经济而极低(数美分/磅硫去除),然而,这类胺处理单元通常需要大量集资费用和操作费用。
近年来,已出现非常规资源,如来自页岩的资源。这些天然气资源通常具有小气流(例如小于100MMSCFD)并且含有相对低浓度的H2S(例如小于2000ppm)和低浓度的CO2(例如小于2%)。
活性碳已经用于去除烃流中的酸性气体,但其不具选择性。相对于CO2和其它组分选择性去除H2S是所期望的,因为其将减少总吸附单元并且也更容易处理浓缩H2S流。
一种在这类应用中选择性地去除H2S的方法已使用一次性H2S清除剂(液体三嗪或海绵铁),因为它们的集资费用低并且具有朝向H2S的选择性。然而,由于清除剂过度消耗,所以总的硫处理成本相对较高(大于$10/磅硫去除)。它们还产生需要特殊处置程序的有害废料。苛性碱处理也是行业中已知的,但是由于去除所有酸性组分,所以它在存在低含量H2S时或在不存在其它选择方案时保留用于H2S和硫醇去除。
氧化锌也已用于从烃流去除含硫化合物。然而,它的高成本和相当大的再生成本使得它用于处理以体积计含有明显量的含硫化合物杂质的烃流一般不经济。也因此,使用氧化锌和与它类似的其它化学吸附材料的不利之处在于为了获得所期望的含硫化合物负载特征,一般需要在使其与含硫流体流接触之前必须加热所述物流的额外能量消耗。
硫杂质的选择性物理吸附也是已知的。如本文所用,“物理吸附剂”是不与它去除的杂质发生化学反应的吸附剂。已研发出液相和气相方法。一种这类方法包含使含硫烃流通过具有大到足以吸附硫杂质的孔径的结晶沸石分子筛床或分子筛吸附剂床,回收未吸附的流出烃,直到获得所需含硫杂质负载程度的吸附剂,并且此后净化烃的吸附块并通过由其解吸附含硫化合物而使吸附剂再生。
常规地,吸附剂再生操作是变温或组合的变温和变压类型操作,其中热量输入是由对烃、分子筛吸附剂和含硫吸附物基本上呈惰性的热气供应。当在如丙烷、丁烷或液化石油气(LPG)的液相中处理烃时,天然气理想地适用于净化和吸附剂再生,条件是它可随后当场用作燃料,其中它构成相对于它的相对高成本的经济平衡。然而,通常,脱硫操作需要用于变温再生的天然气比可有利地作为燃料消耗的更多,并且因此构成再生气体的不足。通常情况下,结果是严重阻碍脱硫方法的成功设计和操作,尤其当在远离精炼厂的位置进行脱硫时。
然而,即使当在气相中用如结晶沸石分子筛和/或分子筛的物理吸附剂处理烃时,仍必须提供净化气体以使满载含硫化合物的吸附剂再生,涉及上文在使用液相烃流时提到的相同缺点。一般来说,将在吸附模式中来自吸附剂床的产物滑流用作使所用床再生的解吸附气体。在整个吸附循环期间将这种产物气体用于再生目的不利地减少了最终产物产率。此外,当利用这类物理吸附剂时,一般难以完全去除含硫化合物。
需要用于从天然气流分离H2S的可再生吸附剂(固-气接触),其方法比上文所论述的现有技术更经济和高效。
发明内容
本发明是一种用于从包含硫化氢(H2S)和任选的一种或多种杂质的天然气进料流去除、优选地选择性地去除H2S的方法,包含以下步骤:
(a)提供包含交联大孔聚合物吸附介质的吸附剂床,其中所述吸附介质吸附H2S;
(b)使所述天然气进料流通过交联大孔聚合物吸附剂床以提供H2S贫乏的天然气流和负载硫化氢的交联大孔聚合物吸附介质;
(c)进一步处理、回收、输送、液化或燃烧所述H2S贫乏的天然气流,
(d)通过使所吸附的H2S解吸附而使所述负载的交联大孔聚合物吸附介质再生以供再利用,
以及
(e)排出H2S以便收集、燃烧、转化成元素硫、再注入或转化成硫酸。
本发明的一个实施例是上文所公开的方法,其中所述交联大孔聚合物吸附剂是单乙烯基芳香族单体与聚乙二烯芳香族化合物交联的聚合物,优选地,所述单乙烯基芳香族单体占所述聚合物的92重量%至99.25重量%,并且所述聚乙二烯芳香族化合物占所述聚合物的0.75重量%至8重量%。
本发明的另一个实施例是上文所公开的方法,其中所述交联大孔聚合物吸附剂是选自苯乙烯、乙烯基苯、乙烯基甲苯、乙基苯乙烯、二乙烯基苯和叔丁基苯乙烯组成的组中的一个或多个的成员的聚合物;并且与选自二乙烯基苯、三乙烯基苯和乙二醇二甲基丙烯酸酯组成的组的成员,优选地选自苯乙烯、乙烯基苯、乙烯基甲苯、乙基苯乙烯和叔丁基苯乙烯组成的组的成员的聚合物,更优选地苯乙烯交联;并且与选自二乙烯基苯、三乙烯基苯和乙二醇二甲基丙烯酸酯组成的组的成员,更优选地二乙烯基苯交联;并且优选地,大孔树脂的总孔隙度是0.5至1.5cc/g,如通过氮吸附所测量的表面积是150至2100m2/g,并且平均孔径是10埃至100埃。
本发明的一个实施例是上文所公开的方法,其中负载的吸附剂的再生是通过使用加热气体和/或辐射热接触交换器来达成,优选地,负载的吸附介质的再生是通过使用变压吸附(PSA)方法、变温吸附(TSA)方法或其组合来达成,更优选地,负载的吸附介质的再生是通过使用微波加热系统来达成。
在本发明的另一个实施例中,上文所公开的方法是连续的。
附图说明
图1是根据本发明的天然气吸附和再生方法的示意图。
图2示出了本发明的交联大孔聚合物吸附介质关于包含不同含量H2S和CO2的N2的穿透曲线。
具体实施方式
原始天然气来自三种类型的井:油井、气井和凝液井。来自油井的天然气通常被称为“伴生气”。这种气体可以一定形式(自由气体)与油分离而存在或溶解于原油中(溶解气体)。来自存在极少或无原油的气井和凝液井的天然气被称为“非伴生气”。气井通常本身产生原始天然气,而凝液井产生自由天然气以及半液体烃凝液。无论天然气的来源是什么,一旦与原油(如果存在)分离,其通常以甲烷与其它烃的混合物形式存在;主要是乙烷、丙烷、丁烷和戊烷以及在较小程度上更重烃。
原始天然气和有时经处理的天然气通常含有大量杂质,如水或酸性气体,例如杂质形式的二氧化碳(CO2)、硫化氢(H2S)、二氧化硫(SO2)、二硫化碳(CS2)、氰化氢(HCN)、硫化羰(COS)或硫醇。如本发明方法中所用的术语“天然气进料流”包括任何天然气来源、原始或已经处理一次或多次以去除水和/或其它杂质的原始天然气。
合适的吸附剂是具有微观结构的固体。此类吸附剂的内表面优选地在100至2000m2/g之间、更优选地在500至1500m2/g之间并且甚至更优选地1000至1300m2/g。吸附剂床中吸附剂的内表面性质使得C2和更重烃得以吸附。合适的吸附介质包括基于氧化硅、硅胶、氧化铝或氧化硅-氧化铝、沸石、活性碳、负载聚合物的氯化银、含铜树脂的材料。最优选的吸附介质是多孔交联聚合物吸附剂或部分热解的大孔聚合物。优选地,吸附剂的内表面是非极性的。
在一个实施例中,本发明是使用吸附介质从包含H2S和任选地一种或多种杂质的天然气流提取H2S。大孔聚合物吸附剂从天然气流提取H2S的机制是吸附和吸收的组合;主要机制至少被认为是吸附。因此,术语“吸附”和“吸附剂”在本说明书通篇使用,但是这主要是为方便起见。本发明并不认为局限于任何特定机制。
当吸附介质已吸附任何量的H2S时,其被称为“负载”。负载包括从低含量H2S直到包括吸附H2S饱和的一系列吸附量。
术语“大孔”在所属领域中与“大孔网状”互换使用并且一般是指直径约或更大的孔。“中孔”被表征为在和更大但小于之间的孔。“微孔”被表征为小于的孔。这些类型的孔的改造分布产生对H2S的高吸附能力和在方便/实际化学工程方法更改(温度升高或减压[真空])下易于H2S解吸附的所需特性。产生微孔、中孔和大孔分布的方法可以不同方式实现,包括在惰性稀释剂或其它致孔剂存在下形成聚合物以导致相分离并且通过后交联形成微孔。
在一个实施例中,本发明的吸附介质是本发明的大孔聚合物吸附剂,其是经改造以具有大表面积、大孔隙体积和高吸附能力以及大孔、中孔和微孔的改造分布的后交联聚合物合成吸附剂。
优选地,本发明的大孔聚合物吸附剂是超高交联和/或亚甲基桥连的,具有以下特征:BET表面积等于或大于500m2/g并且优选地等于或大于1,000m2/g,粒度是300微米至1500微米、优选地500至1200微米。
可以聚合形成适用的大孔聚合物吸附剂的单体的实例是苯乙烯、烷基苯乙烯、卤苯乙烯、卤烷基苯乙烯、乙烯基苯酚、乙烯基苯甲醇、乙烯基苯甲基卤化物和乙烯基萘。包括在经取代的苯乙烯当中的是经邻位、间位和对位取代的化合物。具体实例是苯乙烯、乙烯基甲苯、乙基苯乙烯、叔丁基苯乙烯和乙烯基苯甲基氯,包括任何此类单体的邻位、间位和对位异构体,其分子结构允许此类型的异构化。其它单体实例是多官能化合物。一个优选类别是聚乙二烯化合物,其实例是二乙烯基苯、三乙烯基苯、乙二醇二甲基丙烯酸酯、二乙烯基硫醚和二乙烯基吡啶。优选聚乙二烯化合物是二乙烯基和三乙烯基芳香族化合物。多官能化合物也可以用作第一组单体的交联剂。
在一个实施例中,大孔聚合物吸附剂包含二乙烯基苯,其中所述二乙烯基苯可包含乙基苯乙烯。如果存在乙基苯乙烯,那么其优选地以等于或小于40%、更优选地等于或小于20%的量存在。
制备聚合物吸附剂的一个优选方法是通过使用膨胀剂使聚合物膨胀,接着交联膨胀状态的聚合物作为唯一交联反应或作为除在膨胀之前进行的交联以外的交联反应。当使用膨胀剂时,将使用足够的交联剂进行任何膨胀前交联反应以使得聚合物在与膨胀剂接触时膨胀而非溶解于试剂中。与所进行的阶段无关,交联程度还将影响聚合物的孔隙度并且可以变化以达到特定孔隙度。鉴于这些变化,交联剂的比例可以大幅变化,并且本发明并不限于特定范围。因此,交联剂可以介于聚合物的约0.25%至约45%的范围内。最佳结果一般是相对于聚合物使用约0.75%至约8%交联剂来获得,其余(未交联)单体占约92%至约99.25%(所有百分比都是以重量计)。
适用于本发明实践的其它大孔聚合物吸附剂是一种或多种单芳香族单体与一种或多种非芳香族单亚乙烯基单体的共聚物。后者的实例是丙烯酸甲酯、甲基丙烯酸甲酯和丙烯酸甲基乙酯。当存在时,这些非芳香族单体优选地占共聚物的小于约30重量%。
大孔聚合物吸附剂是通过常规技术制备,其实例公开在不同美国专利中。实例是USP 4,297,220;4,382,124;4,564,644;5,079,274;5,288,307;4,950,332;和4,965,083。这些专利中的每一个的公开内容以全文引用的方式并入本文中。
对于膨胀并且接着在膨胀状态交联的聚合物,在膨胀后的交联可以通过多种方式实现,其进一步公开在以上列举的专利中。一种方法是首先使聚合物卤烷基化,接着使其膨胀并且通过使卤烷基部分与相邻链上的芳香族基团反应形成烷基桥而交联。卤烷基化是通过常规手段实现,其实例是首先在非反应性条件下用卤烷基化剂使聚合物膨胀,同时包括弗里德-克拉夫茨催化剂(Friedel-Crafts catalyst)溶解于卤烷基化剂中。一旦聚合物膨胀,使温度升高至反应水平并且维持直到已发生所需程度的卤烷基化为止。卤烷基化剂的实例是氯甲基甲醚、溴甲基甲醚和甲醛与盐酸的混合物。在卤烷基化后,聚合物通过与惰性膨胀剂接触进一步膨胀。实例是二氯乙烷、氯苯、二氯苯、二氯化乙烯、二氯甲烷、二氯丙烷和硝基苯。弗里德-克拉夫茨催化剂也可以溶解于膨胀剂中,因为所述催化剂将用于后续交联反应。接着在催化剂存在下,将温度升高至介于约60℃至约85℃范围内的水平,并且进行桥连反应。一旦桥连反应完成,通过溶剂提取、洗涤、干燥或这些程序的组合去除膨胀剂。
完成的吸附剂的孔径分布和相关特性可以大幅变化并且无特定范围是本发明关键。在大部分应用中,最佳结果将在聚合物约0.5至约1.5cc/g范围内的孔隙度(总空隙体积)下获得。优选范围是约0.7至约1.3cc/g。在这些范围内,由大孔(即直径或更大的孔)贡献的量将优选地介于约0.025至约0.6cc/g范围内,并且最优选地约0.04至约0.5cc/g。聚合物的表面积,如通过氮吸附法(如熟知的BET方法)所测量,将在大部分应用中在约150至约2100m2/g、并且优选地约400至约1400m2/g的范围内。平均孔径将最通常介于约至约的范围内。
大孔聚合物吸附剂的形式同样并非关键并且可以是能够容纳和接触流动压缩气流的任何形式。颗粒状粒子和珠粒是优选的,尺寸范围介于约50至约5,000微米,其中约500至约3,000微米的范围尤其优选。与吸附剂接触可以通过气体的常规流动配置来实现,如通常用于流化床或填充床的那些配置。吸附剂也可以封入滤筒中以易于去除和置换并且更加控制气流路径(如径向流)。
大孔聚合物吸附剂可以在广泛范围的操作条件下有效地起作用。温度将优选地在不造成蒸气另外冷凝或吸附剂的物理或化学形式的任何变化的任何范围内。优选操作温度在5℃至75℃、并且最优选地10℃至50℃的范围内。一般来说,在环境温度下或在环境温度与高于环境10℃至15℃之间操作将提供令人满意的结果。进入吸附剂床的天然气流的压力也可以大幅变化,优选地从2psig(115kPa)扩展至1000psig(7000kPa)。压力将一般由将使用产品气体的设备单元指示。典型压力范围是100psig(795kPa)至300psig(2170kPa)。吸附剂床中天然气流的最少停留时间将为0.02秒并且推荐较长停留时间。天然气流贯穿床的空间速度将最常落入0.1英尺/秒至5英尺/秒的范围内,其中0.3英尺/秒至3英尺/秒的范围是优选的。最后,相对湿度可为至多100%的任何值,但是较低相对湿度是优选的。
上文所描述的本发明的交联大孔聚合物吸附剂可用于从包含H2S和一种或多种其它杂质的天然气选择性吸附硫化氢。
本发明的分离方法包含使包含H2S的天然气流通过填充有本发明的吸附剂的吸附剂床。优选地,选择性吸附的H2S可易于通过降低压力和/或通过增加吸附剂床的温度解吸附,产生再生吸附剂。
从天然气进料流分离H2S的分批、半连续和连续方法和装置是众所周知。图1描绘本发明的分离方法的一个实施例。分离方法包含以下步骤:(a)使天然气进料流3通过包含吸附剂床2的吸附单元10,所述吸附剂床包含本发明的吸附介质,其吸附H2S以获得硫化氢贫乏的天然气产物,将所述产物排出5(回收、进一步处理、经由管道或其它构件输送、液化、燃烧等),(b)将负载有H2S的吸附剂从吸附单元10输送11到包含构件32的再生单元20,从而通过使H2S 33从负载的吸附介质释放并形成再生吸附介质23而使负载的吸附介质再生,(c)其中再生吸附介质23输送8回到吸附单元10以供再利用,以及(d)排出29释放的H2S 33(收集、燃烧、由苛性碱中和、传送到克劳斯单元以转化成元素硫、再注入或例如经由WSA工艺单元转化成硫酸)。
虽然本发明的一个特别优选的实施例是出于说明性目的而在图1中公开,但是应认识到所公开的方法的变化或修改属于本发明的范围内。举例来说,在本发明的另一个实施例中,可以存在多个吸附剂床和/或可以如由USP 3,458,973所例示就地再生的吸附剂床,其以全文引用的方式并入本文中。
本发明方法的吸附步骤和/或再生步骤可以按分批方法、半连续方法、连续方法或其组合形式操作。举例来说,在本发明的一个实施例中,吸附步骤和再生步骤都可以按分批模式操作。在本发明的另一个实施例中,吸附步骤和再生步骤都可以按半连续模式操作。在本发明的另一个实施例中,吸附步骤和再生步骤都可以按连续模式操作。
或者,在本发明的一个实施例中,吸附步骤可以按分批、半连续或连续模式操作,而再生步骤以与吸附步骤不同的模式操作。举例来说,在本发明的一个实施例中,吸附步骤可以按分批模式操作,而再生步骤以连续模式操作。在本发明的另一个实施例中,吸附步骤可以按连续模式操作,而再生步骤以连续模式操作。吸附步骤和再生步骤的分批、半连续和连续模式的所有可能组合都被视为在本发明的范围内。
吸附在许多情形中是一个可逆过程。从吸附介质去除挥发物的实践可以通过减少介质上的压力、加热、或减压和加热的组合来实现。在任一情况中,所需结果是使所截留的H2S再挥发,并且随后将其从吸附剂去除以使其可以再用于捕捉额外H2S。优选地,本发明的吸附介质当再生时使所吸附的H2S以吸附量的等于或大于75%、更优选地等于或大于85%、更优选地等于或大于90%、更优选地等于或大于95%、更优选地等于或大于99%并且最优选地所吸附的几乎所有H2S的量解吸附。
出于去除所吸附的挥发物的目的,利用常规加热系统,如加热气体(空气或惰性气体)或辐射热接触交换器加热吸附介质的传统方式适于例如通过变压吸附(PSA)方法、变温吸附(TSA)方法或其组合作为吸附介质再生步骤的一部分用于本发明的H2S分离方法。如此再生的吸附剂可在用作吸附剂用于从天然气流去除H2S。
优选地,本发明的H2S分离方法采用微波加热系统作为吸附介质再生步骤的一部分。此类微波加热系统提供在降低的成本下以较高热效率从吸附介质去除H2S的加热系统和方法。
使用微波系统与本发明的吸附剂结合的一个优势在于其允许微波使介质的加热减到最少,但是使H2S的加热达到最大以促进解吸附。这类系统具有操作上比传统再生系统更简单并且减少热量对吸附剂材料自身的效应的益处。此外,当此解吸附方法与连续吸附方法(如移动填充床或类似器件)结合使用时,H2S去除可以经仔细调整以适应进料气体的组成。
优选地,用于本发明方法的再生系统能够以分批、半连续或连续方法操作。
实例
实例中所用的吸附介质描述如下。
吸附剂1是由单乙烯基芳香族单体和交联单体的大孔共聚物制成的具有等于或大于1,000m2/g的大表面积的多孔交联聚合物吸附剂,其中所述大孔共聚物已经在弗里德-克拉夫茨催化剂存在下在膨胀状态后交联。
穿透吸附剂-1,即本发明的交联聚合物吸附剂的硫化氢(H2S)是在不同含量的二氧化碳(CO2)存在下使用紫外光谱分析来测定。使用红外光谱分析测定CO2穿透。吸附剂-1在烘箱中在70℃下干燥过夜并装载在3/8in×8ft不锈钢柱(3.6g)中且暴露于含有各种含量H2S和CO2的氮气(N2)气流。
实例1至3
实例1包含1000ppm H2S和1000ppm CO2。实例2包含1000ppm H2S和1mol%CO2。实例3包含100ppm H2S和1mol%CO2。在25℃和1atm下所测量的流动速率为500cc/min并且在25℃下的背压为75psig。在2分钟内观察到CO2穿透并且快速斜升至1000ppm(实例1)或1%(实例2和3),表明CO2吸附极少。当出口中的H2S浓度达到1000ppm时,释放柱背压并使柱在60℃下暴露于500cc/min N2,直到在出口中观察不到H2S。实例1至3的H2S穿透曲线在图2中示出。
Claims (12)
1.一种用于从包含硫化氢(H2S)的天然气进料流去除H2S的方法,包含以下步骤:
(a)提供包含交联大孔聚合物吸附介质的吸附剂床,其中所述吸附介质吸附H2S;
(b)使所述天然气进料流通过所述交联大孔聚合物吸附剂床以提供H2S贫乏的天然气流和负载硫化氢的交联大孔聚合物吸附介质;
(c)进一步处理、回收、输送、液化或燃烧所述H2S贫乏的天然气流,
(d)通过使所吸附的H2S解吸附而使所述负载的交联大孔聚合物吸附介质再生以供再利用,
以及
(e)排出所述H2S以便收集、燃烧、由苛性碱中和、转化成元素硫、再注入或转化成硫酸。
2.根据权利要求1所述的方法,其中所述天然气流除H2S之外还包含一种或多种杂质,其中所述H2S是在一种或多种杂质存在下从所述天然气流选择性去除。
3.根据权利要求1所述的方法,其中所述交联大孔聚合物吸附剂是单乙烯基芳香族单体与聚乙二烯芳香族化合物交联的聚合物。
4.根据权利要求3所述的方法,其中所述单乙烯基芳香族单体占所述聚合物的92重量%至99.25重量%,并且所述聚乙二烯芳香族化合物占所述聚合物的0.75重量%至8重量%。
5.根据权利要求1所述的方法,其中所述交联大孔聚合物吸附剂是选自苯乙烯、乙烯基苯、乙烯基甲苯、乙基苯乙烯和叔丁基苯乙烯组成的组的成员的聚合物;并且与选自二乙烯基苯、三乙烯基苯和乙二醇二甲基丙烯酸酯组成的组的成员交联。
6.根据权利要求5所述的方法,其中所述交联大孔聚合物吸附剂的总孔隙度是0.5至1.5cc/g,如通过氮吸附所测量的表面积是150至2100m2/g,并且平均孔径是10埃至100埃。
7.根据权利要求1所述的方法,其中所述交联大孔聚合物吸附剂是苯乙烯的聚合物并且与二乙烯基苯交联。
8.根据权利要求1所述的方法,其中所述交联大孔聚合物吸附剂是包含二乙烯基苯和任选地乙基苯乙烯的聚合物。
9.根据权利要求1所述的方法,其中所述负载的吸附剂的再生是通过使用加热气体和/或辐射热接触交换器来达成。
10.根据权利要求1所述的方法,其中所述负载的吸附介质的再生是通过使用变压吸附(PSA)方法、变温吸附(TSA)方法或其组合来达成。
11.根据权利要求1所述的方法,其中所述负载的吸附介质的再生是通过使用微波加热系统来达成。
12.根据权利要求1所述的方法,其中所述方法是连续的。
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CN113735999A (zh) * | 2021-09-03 | 2021-12-03 | 浙江理工大学龙港研究院有限公司 | 一种具有高稳定性和柔韧性的多孔聚合物及其应用 |
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WO2019032283A1 (en) * | 2017-08-11 | 2019-02-14 | Dow Global Technologies Llc | METHOD FOR REMOVING SOFTENED COMPOUNDS FROM A GASEOUS FLOW |
JP2024500705A (ja) * | 2020-12-22 | 2024-01-10 | コモンウェルス サイエンティフィック アンド インダストリアル リサーチ オーガナイゼーション | 超架橋ポリマーを含む酸性ガス用吸収剤 |
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