CN111321020A - 调节第三渗透物吸入压力的膜渗透处理气流的设备和方法 - Google Patents
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Abstract
本发明涉及用于对至少包含甲烷和二氧化碳的进料气流进行膜渗透处理的设备,包括用于压缩进料气流的压缩机A、接收来自压缩机的气流并供应第一渗透物和第一渗余物的第一膜分离单元、接收第一渗余物并供应第二渗透物和第二渗余物的第二膜分离单元、接收第一渗透物并供应第三渗透物和第三渗余物的第三膜分离单元、至少一个测量第一膜分离单元入口处的进料气流的压力的装置、至少一个测量第二渗余物中的CH4浓度的装置和根据进料气流的测定压力和在第二渗余物中测定的甲烷浓度来调节第三渗透物的吸入压力的至少一个压缩机B,每个膜分离单元都包括至少一个膜,所述膜对二氧化碳的渗透性比对甲烷的渗透性更好。本发明还涉及用于控制上述设备的方法。
Description
技术领域
本发明涉及一种用于对包含甲烷和二氧化碳的气流进行膜渗透处理以生产富含甲烷的气流的设备,所述气流的甲烷含量满足其使用要求,并且涉及一种用于控制这种设备的方法。
本发明尤其涉及沼气的纯化,其目的是按照用于注入天然气网络的规格来生产生物甲烷。
背景技术
沼气是有机物质在无氧降解(厌氧发酵)——也称为甲烷化——过程中产生的气体。这可能是自然降解-因此在沼泽地或家庭垃圾填埋场中可以观察到-但是沼气的产生也可以是废物在称为甲烷化反应器或沼气池的专用反应器中甲烷化的结果。
由于其主要成分是甲烷和二氧化碳,沼气是一种强大的温室气体;同时,它也构成了在化石燃料日益稀缺的情况下非常有价值的可再生能源。
沼气主要包含甲烷(CH4)和二氧化碳(CO2),其比例可以根据获取的方式而变化,但也以微量形式包含较小比例的水、氮气、硫化氢、氧气和其它有机化合物。
尽管按干气计算,沼气平均包含30%至75%的甲烷、15%至60%的二氧化碳、0%至15%的氮气、0%至5%的氧气和微量化合物,但取决于已分解的有机物和所使用的技术的不同,成分的比例也有所不同。
沼气以各种方式投入盈利性用途。经过轻度处理后,可将其在生产现场附近投入盈利性用途,以便供应热、电力或两者的混合(热电联产);高二氧化碳含量会降低其热值,增加压缩和运输的成本,并限制这种将其就近投入盈利性用途的方式的经济效益。
更大程度地纯化沼气可以使其投入更广泛的用途;特别地,对沼气的深度纯化会产生一种沼气,该沼气已纯化至天然气规格,并且可以替代天然气;这样纯化的沼气被称为“生物甲烷”。因此,生物甲烷以区域内可再生的比例补充了天然气资源;它可以投入与化石来源的天然气完全相同的用途。可以将其送入天然气网络、汽车加气站;也可以将其液化以采用液化天然气(LNG)等形式储存。
根据以下当地情况来确定将生物甲烷投入盈利性用途的方式:当地的能源需求,将其作为生物甲烷燃料投入盈利性用途的可能性,以及特别是附近是否有天然气运输或分销网络。通过在给定区域内开展活动的各方(农民,制造商,市政当局)之间建立协同作用,生物甲烷的生产有助于该区域获取更大的能源自主。
在收集沼气与获得生物甲烷(可以压缩或液化的最终产品)之间,需要完成许多步骤。
特别地,在旨在分离出二氧化碳以生产纯化的甲烷流的处理之前需要几个步骤。第一步骤是压缩已产生并在大气压下引入的沼气,并且可以使用压缩机以常规方式获得这种压缩。接下来的步骤旨在去除沼气中的腐蚀性成分,即硫化氢和挥发性有机化合物(VOC);以传统方式使用的技术是变压吸附(PSA)并在活性炭上捕集。接下来的步骤是分离二氧化碳,以便最终获得其后续使用所需纯度的甲烷。
二氧化碳是通常存在于天然气中的污染物,并且通常的做法是需要将其除去。为此,根据情况使用各种技术;其中,当CO2含量高时,膜技术表现特别出色;因此,它可用于分离源自释放的气体或植物或动物废物沼气池的沼气中存在的CO2。
用于纯化气体的膜气体分离方法,无论它们是否采用一个或多个膜段,都需要以低成本生产出所需品质的气体,同时最大程度地减少可投入盈利性用途的气体的损失。因此,在沼气纯化的情况下,所进行的分离主要是CH4/CO2分离,该分离需要允许生产根据其用途包含85%以上的CH4、优选95%以上的CH4、更优选97.5%以上的CH4的气体,同时最大程度地减少残留气体中的CH4损失和纯化成本,后者在很大程度上与对膜上游的气体进行压缩的设备的电力消耗相关联。
天然气网络优选接收甲烷浓度恒定的甲烷流,使得使用生物甲烷的设备能够一致地运行。
在此基础上,出现的一个问题是提供一种设备,该设备能够获得恒定浓度的甲烷流。
发明内容
本发明的一种解决方案是一种用于对至少包含甲烷和二氧化碳的进料气流进行膜渗透处理的设备,该设备包括:
-用于压缩进料气流的压缩机A,
-第一膜分离单元,其能够接收来自压缩机的气流并供应第一渗透物和第一渗余物,
-第二膜分离单元,其能够接收第一渗余物并供应第二渗透物和第二渗余物,
-第三膜分离单元,其能够接收第一渗透物并供应第三渗透物和第三渗余物,
-至少一个用于测量第一膜分离单元的入口处的进料气流的压力的装置,
-至少一个用于测量第二渗余物中的CH4浓度的装置,和
-至少一个压缩机B,用于根据进料气流的测定压力和在第二渗余物中测定的甲烷浓度来调节第三渗透物的吸入压力,
其中每个膜分离单元都包括至少一个膜,所述至少一个膜对二氧化碳的渗透性比对甲烷的渗透性更好。
附图说明
图1示出根据本发明的设备的示例。应当注意,在该图1中,压缩机B好比真空泵P。
具体实施方式
根据情况,根据本发明的设备可以具有以下特征中的一个或多个特征:
-第三渗余物被再循环到压缩机A上游的进料气流中;
-第二渗透物被再循环到压缩机A上游的进料气流中;
-在这些膜分离单元中使用的这些膜具有相同的选择性;
-至少一个膜分离单元包括至少两个膜。
本发明的主题还是一种用于控制本发明中定义的设备的方法,该方法包括以下步骤:
a)测量第一膜分离单元的入口处的进料气流的压力,
b)测量第二渗余物中的CH4浓度,
c)将在步骤a)中测得的压力和在步骤b)中测得的浓度与设定值进行比较,并确定相对于这些设定值的差值,
以及
d)借助于压缩机B调节第三渗透物的吸入压力的步骤。
根据情况,根据本发明的方法可以具有以下特征中的一个或多个特征:
-在步骤d)中,借助于压缩机B调节第三渗透物的吸入压力,并借助于压缩机A或借助于渐进式截止阀和加压阀调节进料气流的压力;
-调节进料气流的压力包括升高或降低该压力;
-在调节步骤中,使压缩机B加速或减速。应当注意,压缩机B的加速将使得可以降低第三渗透物的压力水平,而压缩机B的减速将使得可以升高第三渗透物的压力水平;
-比较步骤和调节步骤由数据传输和数据处理装置自动执行;
-进料气流是沼气。
数据传输和数据处理装置例如可以是可编程控制器类型的工业处理器。
Claims (11)
1.一种用于对至少包含甲烷和二氧化碳的进料气流进行膜渗透处理的设备,包括:
-用于压缩进料气流的压缩机A,
-第一膜分离单元,其能够接收来自所述压缩机的气流并供应第一渗透物和第一渗余物,
-第二膜分离单元,其能够接收所述第一渗余物并供应第二渗透物和第二渗余物,
-第三膜分离单元,其能够接收所述第一渗透物并供应第三渗透物和第三渗余物,
-至少一个用于测量所述第一膜分离单元的入口处的进料气流的压力的装置,
-至少一个用于测量所述第二渗余物中的CH4浓度的装置,和
-至少一个压缩机B,其用于根据所述进料气流的测定压力和在所述第二渗余物中测定的甲烷浓度来调节所述第三渗透物的吸入压力,
其中,每个膜分离单元都包括至少一个膜,所述至少一个膜对二氧化碳的渗透性比对甲烷的渗透性更好。
2.根据权利要求1所述的设备,其特征在于,所述第三渗余物被再循环到所述压缩机A上游的进料气流中。
3.根据权利要求1或2所述的设备,其特征在于,所述第二渗透物被再循环到所述压缩机A上游的进料气流中。
4.根据权利要求1至3中任一项所述的设备,其特征在于,在这些膜分离单元中使用的膜具有相同的选择性。
5.根据权利要求1至4中任一项所述的设备,其特征在于,至少一个膜分离单元包括至少两个膜。
6.一种用于控制根据权利要求1至5中任一项所述的设备的方法,包括以下步骤:
a)测量所述第一膜分离单元的入口处的进料气流的压力,
b)测量所述第二渗余物中的CH4浓度,
c)将在步骤a)中测得的压力和在步骤b)中测得的浓度与设定值进行比较,并确定相对于这些设定值的差值,
以及
d)借助于压缩机B调节第三渗透物的吸入压力的调节步骤。
7.根据权利要求6所述的方法,其特征在于,在步骤d)中,借助于所述压缩机B调节所述第三渗透物的吸入压力,并且借助于所述压缩机A或借助于渐进式截止阀和增压阀调节所述进料气流的压力。
8.根据权利要求7所述的方法,其特征在于,所述进料气流的压力的调节包括升高或降低所述压力。
9.根据权利要求6至8中任一项所述的方法,其特征在于,在所述调节步骤中,对所述压缩机B进行加速或减速。
10.根据权利要求6至9中任一项所述的方法,其特征在于,所述比较的步骤和所述调节步骤由数据传输和数据处理装置自动执行。
11.根据权利要求6至10中任一项所述的方法,其特征在于,所述进料气流是沼气。
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CN104043318A (zh) * | 2013-03-11 | 2014-09-17 | 艾森曼股份公司 | 用于从沼气中提取高纯度甲烷的方法和实施该方法的设备 |
WO2014183977A1 (de) * | 2013-05-15 | 2014-11-20 | Evonik Industries Ag | Steuerung der gaszusammensetzung einer gasseparationsanlage mit membranen |
WO2015036709A1 (fr) * | 2013-09-16 | 2015-03-19 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé pour une épuration finale de biogaz pour produire du biomethane |
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CN107921362A (zh) * | 2015-09-10 | 2018-04-17 | 阿克西奥姆应用处理技术有限责任公司 | 用于将气体混合物分离的装置和方法 |
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WO2012000727A1 (de) * | 2010-07-01 | 2012-01-05 | Evonik Fibres Gmbh | Verfahren zur trennung von gasen |
AT513644B1 (de) * | 2012-11-27 | 2014-09-15 | Tech Universität Wien | Permeatorsystem zur Trennung von Gasgemischen |
AT515137B1 (de) * | 2013-12-02 | 2016-01-15 | Johann Gruber-Schmidt | Verfahren zur Trennung, Aufreinigung und Aufkonzentration von Gasgemischen |
PT3585500T (pt) * | 2017-02-03 | 2023-10-17 | Air Liquide Advanced Tech Us Llc | Método e sistema integrados de ptsa/membranas para remoção de h2s e co2 do biogás |
US10569217B2 (en) * | 2018-01-24 | 2020-02-25 | Air Liquide Advanced Technologies U.S. Llc | Production of biomethane using a high recovery module |
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US20150336046A1 (en) * | 2012-11-14 | 2015-11-26 | Evonik Fibres Gmbh | Control of gas composition of a gas separation system having membranes |
CN104043318A (zh) * | 2013-03-11 | 2014-09-17 | 艾森曼股份公司 | 用于从沼气中提取高纯度甲烷的方法和实施该方法的设备 |
WO2014183977A1 (de) * | 2013-05-15 | 2014-11-20 | Evonik Industries Ag | Steuerung der gaszusammensetzung einer gasseparationsanlage mit membranen |
WO2015036709A1 (fr) * | 2013-09-16 | 2015-03-19 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé pour une épuration finale de biogaz pour produire du biomethane |
CN107921362A (zh) * | 2015-09-10 | 2018-04-17 | 阿克西奥姆应用处理技术有限责任公司 | 用于将气体混合物分离的装置和方法 |
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US11504668B2 (en) | 2022-11-22 |
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