CN101820964A - 大部分为乙醇和水的混合物的脱水方法 - Google Patents
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Abstract
大部分为乙醇和水的混合物的脱水方法,该混合物被分流成作为回流被导向蒸馏塔(32)的第一分进料流(3),而第二分进料流(4)被导向蒸发器单元(31)作为蒸发器入口流并作为蒸发器出口流(6)离开蒸发器单元顶部。来自蒸馏塔(32)的顶部排放流(7)被返回并且与蒸发器出口流(6)在过压下合并为合并流(8),且合并流(8)在压缩机单元(33)中被压缩,生成合并的压缩流(10),该流(10)进入脱水单元(34),在其中它被分成富水渗透流(14)和基本为无水乙醇形式的渗余流(11)。渗透流(14)在冷凝器(39)中在负压下冷凝,之后渗透流(15)被泵(42)增压成流(16),该流(16)被进料到由换热器(36)供给外部热能的蒸馏塔(32)中,并分成富水的底部排放流(18)和富含乙醇的顶部排放流(7)。渗余流(11)在蒸发器单元(31)的渗余物换热器(37)中作为能源使用,然后作为产品流(12)被排放。
Description
本申请涉及一种如权利要求1的特征部分所定义的包含大部分乙醇和水的混合物的脱水方法。
背景技术
工业上,水和乙醇经常以组合物的形式存在,该组合物不适于这些化合物中的任何一种的进一步应用。作为一种原料,乙醇适合作为多种工艺的溶剂或作为能源。例如,水和乙醇的组合物在工艺中以不同比例存在,其目的是提供基本无水的乙醇作为由生物原料产生的能源。就此而论,乙醇一般指生物乙醇。
一般使用传统的蒸馏方法来生产稍微高于组合物共沸点的具有水含量的乙醇。为了进一步减少乙醇/水组合物的水含量,以增加乙醇的效用及其作为产物的价值,尝试了在以下的段落中描述的不同的方法。
为此目的,多组分蒸馏(也称为共沸蒸馏)已经并仍在使用。相对高的能耗和化学品的使用是这种技术的特征。有已知的用于多组分蒸馏的工艺解决方案,其中包含能量回收,因此包括工艺蒸汽的机械再压缩。在JP专利59196833、FR专利2855170和JP专利60226837中可以找到例子,其描述了串联细合操作的具有工艺蒸汽再压缩的蒸馏塔。
另一个方法称作萃取蒸馏。该方法也涉及用于萃取步骤的化学品的使用。US专利号5294304和JP专利61254177描述了这样的工艺,其中工艺蒸汽的再压缩被包含在总的能量***中。
其它两种技术是分子筛和蒸汽渗透,其中上游蒸汽在蒸发器中产生或直接从传统的蒸馏过程中得到。这种技术中的排放流是渗余物(基本无水的乙醇),和包含具有更大或更小份额乙醇的水的渗透物,其一般被冷凝下来并随后在蒸馏塔中回收。传统的具有蒸发器的方法消耗能量,以用于蒸发进料液体并回收渗透的乙醇部分,包括在所述渗透物的蒸馏步骤中产生回流液体。
US专利2007000769描述了传统的没有工艺蒸汽再压缩的分子筛方法。分子筛和蒸汽渗透的主要不同之处是,这样的使用分子筛的脱水步骤是以间歇方式进行的,因此大量的分子筛槽被相互交换并且没有进行生产的槽被进行再生工艺。以这种方式,工艺的上游和下游以连续的方式操作,且来自分子筛脱水单元的排放流是类似蒸汽渗透的渗余物和渗透物。
采用液体方式进料通过膜的膜分离,又称为全蒸发,也是一种被使用的技术。通过这种技术排放的渗透物流也是蒸汽的形式,而渗余物是液相。与传统的蒸汽渗透相比,能量消耗相对较低,因为不需要供应能量来蒸发进料的渗余物部分。所供应的能量而是用于蒸发渗透物并回收渗透物中的乙醇部分,也包括生成到所述渗透物的蒸馏步骤的回流液体。因为膜暴露在进料中的可能的杂质中,就膜的寿命而言,全蒸发是一种较不耐用的技术。有已知的涉及全蒸发的方法,其中包括工艺蒸汽的机械再压缩。例如,JP专利63059308描述了用于乙醇的全蒸发的方法。来自膜的渗透物在作为进料蒸气进入蒸馏步骤之前,流经蒸汽压缩步骤。该方法中,工艺蒸汽的压缩的后果是渗透物可以维持为蒸汽而进入蒸馏塔,因而降低了否则从渗透物中回收乙醇所需要的能量的量。
另一个渗透物再压缩的例子被记载在JP专利5137969中,其中蒸汽形式的渗透物的压力增加用于在提供的冷却水的温度下冷凝,而非必须使用需要能量的制冷单元所产生的冷却介质。
发明目的
本发明的一个目的是提供一种从大部分为乙醇和水的液体混合物中分离水的低能量方法。
进一步的目的是在工业条件下能够实现第一个目的,即,采用具有最高可能的操作可用度的成本有效的全规模装置。
发明内容
上述目的通过在权利要求1中定义的本发明的方法来实现。
本发明的优选的实施方案通过从属权利要求公开。
一种大部分为乙醇和水的混合物的脱水方法,其包括蒸发、蒸馏、压缩、换热和蒸汽渗透或分子筛,处于液相的大部分为乙醇和水的进料被分流成作为回流被加入蒸馏塔的第一分进料流,而另一分进料流被进料到蒸发器作为蒸发器进料流并作为蒸发器排放流离开蒸发器的顶部,而来自蒸馏塔的上部排放流被返回并且与蒸发器排放流在过压下合并为合并流,且该合并流在压缩机单元中被压缩,生成压缩的合并流,该压缩的合并流进入脱水单元被分成富水渗透流和基本无水的渗余流,渗透流随后在冷凝器中在由真空***产生的负压下被冷凝,并以液体形式被增压并作为进料流加入通过换热器接收外部热能的蒸馏塔中,并被分成基本上为水的底部排放流和富含乙醇的顶部排放流,渗余流在蒸发器单元的渗余物换热器中作为能源使用,然后作为产品流被排放。
所属领域技术人员将意识到该混合物能够并通常将含有更少量的除乙醇和水之外的组分,例如变性剂和少量的杂醇油和重质醇。
根据本发明,只对蒸馏塔强制地提供外部能量。该方法以这样的方式设计,其中除了渗透物的乙醇部分的回收外,该能量被完全用于进料流的蒸发。没有排除也给蒸发器提供外部能量的可能性,但不是强制性的。以蒸汽渗透方式进行的脱水单元的驱动力是渗余物侧和渗透物侧之间的水蒸气压力差,其实际上通过在负压下移走渗透物同时在过压下提供进料蒸气来实现。
在下文,以优选的实施方案的方式并参考附图更加完整地描述本方法。
本发明的具体实施方案
图1是本发明的优选实施方案的流程图。
图2是本发明的较简单的实施方案的流程图。
应该了解的是,如果没有指出其他内容,以下具体图形形式的举例说明涉及一种装置,该装置包括基于蒸汽渗透的脱水单元34。除非有不同指定,所有工艺流的相关量的表示都是重量%。
图1显示了供给的富含乙醇的进料流1如何在换热器35中预热成为预热了的进料流2并在此以后分成第一分进料流3和第二分进料流4,第二分进料流4具有在换热器41中进一步预热的内流5。第一分进料流3作为回流进入蒸馏塔32,而第二分进料流4进入蒸发器单元31。第一分进料流3通常对应于进料流1的小于20%。来自蒸发器单元31的蒸发器出口流6与来自蒸馏塔32的顶部排放流7合并。进料流1一般具有70%或更多的乙醇含量,并更优选80%或更多。在采用分子筛脱水的情况下,相应的特征是80%或更多,并更优选90%或更多。
通过工艺流6和7合并的流8进入压缩机单元33,且如此压缩的合并流9进入气体冷却器41,来自气体冷却器41的如此冷却的工艺流10,其一般具有在2-8绝压巴范围内的压力(依赖于脱水方法且如果采用蒸汽渗透来脱水的话也依赖于膜的类型),进入了一般基于分子筛或蒸汽渗透的脱水单元34。从脱水单元34排放出基本无水的渗余流11和富含水的渗透流14。渗余流11一般具有至多2%的水。对于生物乙醇,在渗余物中水含量的要求是<0.3%,其通过本方法在用于脱水单元的正常工艺条件下是能得到的。压缩机单元33保证了富含乙醇的渗余流是在比蒸发器单元31中的蒸发温度更高的饱和温度下,因此通过与蒸发器单元31相连的换热器37中换热,工艺流中的潜能在本方法中被利用。与已论述的一样,以在换热器35中与进料流1换热的方式,来自换热器37的冷凝的渗余流12能释放更多的能量。基本无水的乙醇产品流13离开换热器35。
富含水的渗透流14,其一般含有5-40%的乙醇,在冷凝器39中在由真空泵43所例示的真空***产生的负压(0-1绝压巴)下被冷凝,之后液体渗透流15被增压成为增压的渗透流16且在换热器40中预热并随后作为工艺流17以液体进料形式进入蒸馏塔32。来自蒸馏塔32的底部排放流18在换热器40中向增压的渗透流16释放热能,然后作为基本上纯净的水(一般多于99%的水)的排放流19离开工艺。
将外部热能提供给与蒸馏塔32连接的过程,且更具体地通过与蒸馏塔32连接的换热器36来提供。与蒸发器单元31有关的额外的能量可以任选地依靠下文论述的换热器38提供。分别进入相关的换热器36和换热器38中的加热介质20和22一般是热液体或蒸汽。
就蒸汽渗透而言,脱水单元34的寿命受任何存在于它的进料蒸气中的杂质的影响。为了避免不期望的挥发性组分例如杂醇油在蒸馏塔32中的积聚,可在塔上设置一个侧线出口(未示出)。为了避免不期望的组分例如盐、其他固体物质和重质(高沸)醇积聚在蒸发器单元31的液体池中,一少量液体流(未示出),其一般少于进料流1的5%,被从蒸发器单元31排放至工艺流17或回流3,作为到蒸馏塔32的少量进料或回流,其中不期望的组分随底部排放流18离开蒸馏塔32或者经由所提到的塔的侧线出口离开蒸馏塔32。如果上述少量液体流被从蒸发器31的液体池中带到蒸馏塔32中,采用本方法,能量消耗将不会增加。
图2显示了本发明的一个比图1更简单的实施方案。通过在图2中已经留出的解释,区别可以被最简单地解释,也就是换热器35、38、40和41,它们通常存在于工业装置中,但为了达到本发明的基本优点,它们不是必须的。在换热器(预热器)35和40中回收的能量可以,例如,被用于其他目的。另一个例子是进料流1在进入时已经是热的,并且工艺流12因此将与其他流体或为了其他目的而进行换热。
通过对比图2与图1中的工艺流,可以观察到在图2中的工艺流12对应于图1中的工艺流12和13两者,在图2中的工艺流16对应于图1中的工艺流16和17两者,和在图2中的工艺流18对应于图1中工艺流18和19两者。
如同关于附图1所提及的,进料流1在被分流并在蒸馏塔32和蒸发器单元31之间分配之前,一般被预热。这种预热优选地以在图1中的换热器35中与渗余流12进行换热的方式来进行。
进一步优选的是压缩机单元33是机械蒸汽压缩机。或者,压缩机单元可以基于蒸气喷射器装置的工艺蒸气的热再压缩,为此使用高压乙醇蒸气作为喷射器的驱动蒸气。替代方案将提供较小程度的能量回收。
可能且经常优选的是,除了来自渗余物的潜能(通过换热器37提供)外,也将外部能量提供至蒸发器单元31。这些外部能量可在接收加热介质22的换热器38中提供。
渗透流14构成了到蒸馏塔32的入口(进料)流17的基础。渗透流14首先在由换热器39和冷却介质24所例示的一个或多个换热器中在负压下冷却并冷凝,此后被由泵42所例示的一个或多个泵增压成增压的渗透流16。负压(真空)是除水的一个重要的驱动力,其可通过由在换热器39的排放侧的真空泵43所例示的真空***来实现。进一步优选的是,为了优化工艺的能量消耗,使冷凝的渗透流16与来自蒸馏塔32的底部排放流18进行换热,然后使如此加热的渗透流17进入蒸馏塔32。
在蒸发器单元31的下游,蒸发器出口流6与来自蒸馏塔32的顶部排放流7合并,并且合并流8被压缩,其导致了压缩的合并流10的过热加热。可以优选的是在这一流体进入脱水单元34前对其进行冷却。冷却可以例如发生在一个具有冷却介质5的换热器41中,冷却介质5可以是到本工艺的进料流的一个分支,由此回收的净供给热能被利用到工艺中的其他地方。
采用来自渗余流12的显热来预热进料液体1。主要量的进料在蒸发器单元31中蒸发。通过被用作回流液体3,少量的进料在蒸馏塔32中蒸发。进料流1的第三部分5在进入蒸发器单元31前能进一步在换热器41中预热。或者,通过被直接加到已压缩的、过热气体流9中,工艺流5在压缩机单元33中蒸发。
能量回收的主要部分是在适合的压缩机设备中通过工艺蒸汽的机械再压缩而实现的。用于压缩机设备的驱动能量可以是电能或热能。如果使用热能,来自所使用的设备的废能可以全部或部分地作为本专利方法的能量供应。供应给压缩机设备的电机的能量的大部分(约90-95%),构成了在整个工艺中的有用能量。
计算例
没有MVR并具有内部产生的回流液体(*)的传统蒸汽渗透(**):
-进料浓度:在水中的85%EtOH
-产能:10.000kg/h
-总热能消耗:3200kW
-总电能消耗:25kW
-进料浓度:在水中的95%EtOH
-产能:10.000kg/h
-总热能消耗:2400kW
-总电能消耗:25kW
在蒸汽渗透(*)(**)情况下的本方法:
-进料浓度:在水中的85%EtOH
-产能:10.000kg/h
-总热能消耗:1150kW
-总电能消耗:175kW
-进料浓度:在水中的95%EtOH
-产能:10.000kg/h
-总热能消耗:375kW
-总电能消耗:175kW
对于进料中有85%EtOH的情况,减少的能量消耗=约60%
对于进料中有95%EtOH的情况,减少的能量消耗=约80%
(*)不包括热损失和提供给制冷***用于为冷凝器生产冷却介质的任何能量
(**)与蒸汽渗透的情况相比,分子筛的能量消耗降低量将更少,这主要是因为可对比的能量需求再生过程。
Claims (11)
1.一种大部分为乙醇和水的混合物的脱水方法,包括蒸发、蒸馏、压缩、换热和蒸汽渗透或分子筛,特征在于,将大部分为乙醇和水的进料流(1)分流成作为回流被导向蒸馏塔(32)的第一分进料流(3),而第二分进料流(4)被导向蒸发器单元(31)作为蒸发器入口流并作为蒸发器出口流(6)离开蒸发器单元顶部,而来自蒸馏塔(32)的顶部排放流(7)被返回并且与蒸发器出口流(6)在过压下合并为合并流(8),且合并流(8)在压缩机单元(33)中被压缩,生成合并的压缩流(10),该流(10)进入脱水单元(34),在其中它被分成富水渗透流(14)和基本为无水乙醇形式的渗余流(11),渗透流(14)在冷凝器(39)中在由真空泵(43)所举例说明的真空***产生的负压下冷凝,之后渗透流(15)被泵(42)增压成流(16),该流(16)被进料到由换热器(36)供给外部热能的蒸馏塔(32)中,并分成富水的底部排放流(18)和富含乙醇的顶部排放流(7),而渗余流(11)在蒸发器单元(31)的渗余物换热器(37)中作为能源使用,然后作为产品流(12)被排放。
2.根据权利要求1的方法,特征在于,进料流(1)在被分流并分配到蒸馏塔(32)和蒸发器单元(31)中之前被预热。
3.根据权利要求2的方法,特征在于,进料流(1)在换热器(35)中通过与产品流(12)换热而被预热。
4.根据权利要求1的方法,特征在于,压缩机单元(33)是机械蒸汽压缩机。
5.根据权利要求1的方法,特征在于,除了通过渗余物换热器(37)由渗余物(11)提供的能量外,蒸发器单元(31)还由换热器(38)供应外部热能(22)。
6.根据权利要求1的方法,特征在于,渗透流(16)在形成蒸馏进料流(17)之前在换热器(40)中通过与来自蒸馏塔(31)的底部排放流(18)换热而被预热。
7.根据权利要求1的方法,特征在于,来自压缩机单元(33)的压缩的合并工艺流(10)在进入脱水单元(34)前被直接或间接冷却。
8.根据权利要求1的方法,特征在于,乙醇在进料流(1)中的相对量是至少70%,更优选至少80%。
9.根据权利要求1的方法,特征在于,当脱水单元(34)是分子筛时,乙醇在进料流(1)中的相对量是至少80%,且更优选至少90%。
10.根据权利要求1的方法,特征在于,将有限的液体流从蒸发器单元(31)的液体池经由蒸馏进料(16或17)或经由进入蒸馏塔的回流(3)引至蒸馏塔(32)。
11.根据权利要求1的方法,特征在于,渗余流(11)一般含有至多2%的水,更优选地至多0.3%的水。
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KR101596111B1 (ko) * | 2013-01-16 | 2016-02-22 | 주식회사 엘지화학 | 알칸올의 제조 장치 |
US8926718B2 (en) | 2013-03-15 | 2015-01-06 | Celanese International Corporation | Thermochemically produced ethanol compositions |
DE102014222071A1 (de) * | 2014-10-29 | 2016-05-04 | Gea Wiegand Gmbh | Destillationsanlage |
CN107510949A (zh) * | 2017-09-26 | 2017-12-26 | 深圳市蓝石环保科技有限公司 | 一种mvr蒸发*** |
KR102226466B1 (ko) * | 2019-06-25 | 2021-03-11 | 주식회사 앱스필 | 투과증발 원리를 이용하는 탈수 공정 시스템 |
US20210040509A1 (en) * | 2019-08-05 | 2021-02-11 | Bioleap, Inc. | Dehydration energy recycling system and method |
CN112843766B (zh) * | 2020-12-29 | 2022-06-14 | 复榆(张家港)新材料科技有限公司 | 变压吸附分离溶剂水二元共沸物的吸附分离工艺 |
US12005381B2 (en) * | 2021-10-15 | 2024-06-11 | Whitefox Technologies Limited | Heat integrated process and system for ethanol production using vapor recompression |
Family Cites Families (22)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6055117B2 (ja) | 1983-04-21 | 1985-12-03 | 新燃料油開発技術研究組合 | 無水エタノ−ルの製造方法および装置 |
JPS60226837A (ja) | 1983-12-01 | 1985-11-12 | Res Assoc Petroleum Alternat Dev<Rapad> | 無水エタノ−ルの製造装置および無水エタノ−ルの製造法 |
JPS61254177A (ja) | 1985-05-02 | 1986-11-11 | Hitachi Zosen Corp | エタノ−ル含有液からのエタノ−ル抽出法 |
GB8601081D0 (en) * | 1986-01-17 | 1986-02-19 | Distillers Co Carbon Dioxide | Removing water from ethanol |
JPS6359308A (ja) | 1986-08-29 | 1988-03-15 | Mitsui Eng & Shipbuild Co Ltd | 有機液体の分離装置 |
JPS63254987A (ja) * | 1987-04-13 | 1988-10-21 | Ube Ind Ltd | アルコ−ル醗酵液の脱水濃縮方法 |
JPS63258601A (ja) * | 1987-04-15 | 1988-10-26 | Ube Ind Ltd | 有機物水溶液の濃縮方法 |
US5294304A (en) | 1989-11-14 | 1994-03-15 | Ministry Of International Trade And Industry | Process for the recovery of absolute ethanol by vapor compression extractive distillation |
JPH07227517A (ja) * | 1994-02-17 | 1995-08-29 | Nisso Eng Kk | 液体混合物の分離方法 |
EP0695574B1 (en) | 1994-08-04 | 1999-01-27 | Praxair Technology, Inc. | Gas separation with fractional purge for pre- or post-purification |
WO2004073841A1 (ja) | 2003-02-21 | 2004-09-02 | Bussan Nanotech Research Institute, Inc. | 水溶性有機物の濃縮方法 |
US7867365B2 (en) * | 2003-03-28 | 2011-01-11 | Thermal Kinetics Systems, Llc | Ethanol distillation with distillers soluble solids recovery apparatus |
FR2855170B1 (fr) | 2003-05-21 | 2006-07-28 | Ungda | Procede de deshydratation d'ethanol et de flegmes ethanoliques par distillation azeotropique en economie d'energie |
EP1506807A3 (en) * | 2003-08-13 | 2005-04-13 | Generon IGS, Inc. | Air dehydration membrane |
US7294174B2 (en) * | 2003-08-13 | 2007-11-13 | Generon Igs, Inc. | Air dehydration membrane |
WO2005051533A1 (en) * | 2003-11-24 | 2005-06-09 | Council Of Scientific And Industrial Research | Preparation of molecular sieve used for the dehydration of the alcohol |
CN101163528A (zh) * | 2005-04-20 | 2008-04-16 | 白狐技术有限公司 | 分离方法 |
BRPI0600553A (pt) | 2006-02-24 | 2007-11-20 | Siemens Ltda | processo e sistema para a produção de álcool por destilação de múltiplo efeito |
DE102006062885A1 (de) * | 2006-10-18 | 2008-12-11 | Gea Wiegand Gmbh | Anlage zum Destillieren von Trinkalkohol, insbesondere Whiskey |
DE102006049173A1 (de) | 2006-10-18 | 2008-04-30 | Gea Wiegand Gmbh | Anlage zum Destillieren von Alkohol, insbesondere Ethylalkohol aus fermentierter Maische |
EP1947463A1 (en) | 2007-01-16 | 2008-07-23 | Roche Diagnostics GmbH | Collection of liquid analytical samples for clinical analytical purpose |
BRPI0815750B1 (pt) * | 2007-08-27 | 2019-03-06 | Membrane Technology And Research, Inc. | “processo para recuperar um solvente orgânico de uma mistura de solvente/água” |
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2007
- 2007-10-12 NO NO20075207A patent/NO328571B1/no unknown
-
2008
- 2008-10-09 EP EP08838277.5A patent/EP2209541B1/en active Active
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Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104341268A (zh) * | 2013-08-09 | 2015-02-11 | 中国石油天然气股份有限公司 | 一种燃料乙醇连续脱水方法 |
CN104341268B (zh) * | 2013-08-09 | 2016-08-10 | 中国石油天然气股份有限公司 | 一种燃料乙醇连续脱水方法 |
CN106170468A (zh) * | 2013-12-24 | 2016-11-30 | 英国石油有限公司 | 醇组合物的处理 |
TWI663149B (zh) * | 2013-12-24 | 2019-06-21 | 英商Bp有限公司 | 醇類組成物的處理 |
CN106170468B (zh) * | 2013-12-24 | 2020-03-13 | 英国石油有限公司 | 醇组合物的处理 |
CN108774109A (zh) * | 2018-05-31 | 2018-11-09 | 胡雯 | 一种乙醇脱水设备 |
CN108774109B (zh) * | 2018-05-31 | 2021-03-19 | 胡雯 | 一种乙醇脱水设备 |
CN109663477A (zh) * | 2018-12-30 | 2019-04-23 | 安徽广信农化股份有限公司 | 一种制备氯甲酸乙酯的废料处理方法 |
CN110841320A (zh) * | 2019-12-18 | 2020-02-28 | 肥城金塔酒精化工设备有限公司 | 四效溶剂回收节能***及方法 |
CN111298472A (zh) * | 2020-04-17 | 2020-06-19 | 江苏时顺工程技术有限公司 | 一种用于酒精法生产乙醛的酒精循环蒸发*** |
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KR20100068488A (ko) | 2010-06-23 |
WO2009048335A1 (en) | 2009-04-16 |
BRPI0817555A2 (pt) | 2015-03-31 |
US20100270139A1 (en) | 2010-10-28 |
DK2209541T3 (en) | 2016-08-15 |
EP2209541B1 (en) | 2016-04-27 |
JP5442621B2 (ja) | 2014-03-12 |
JP2011502960A (ja) | 2011-01-27 |
EP2209541A1 (en) | 2010-07-28 |
CN101820964B (zh) | 2013-01-02 |
EP2209541A4 (en) | 2011-09-14 |
NO20075207L (no) | 2009-04-14 |
KR101532988B1 (ko) | 2015-07-02 |
NO328571B1 (no) | 2010-03-22 |
US8425733B2 (en) | 2013-04-23 |
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