CN117679919A - 一种具有乙烷混合物回收的膜法天然气提氦设备及工艺 - Google Patents
一种具有乙烷混合物回收的膜法天然气提氦设备及工艺 Download PDFInfo
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 168
- 239000012528 membrane Substances 0.000 title claims abstract description 154
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 104
- 239000001307 helium Substances 0.000 title claims abstract description 103
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 239000003345 natural gas Substances 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims abstract description 63
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
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- 239000005977 Ethylene Substances 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
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Abstract
本发明涉及一种具有乙烷混合物回收的膜法天然气提氦设备及工艺,包括过滤分离器、膜分离系统、压缩机、脱氢单元及提纯单元。本发明采用深冷耦合膜分离法从油气田处理后的天然气中分离氦气并联产乙烷混合物,针对国内天然气贫氦、特贫氦、无工业利用价值的窘状,在回收氦气的同时提取具有较高附加值的乙烷混合物,使低品位氦气资源的提取变得经济可行,大大降低了氦气资源的工业品位,拓展了可利用氦气资源的范围;本发明特别适用于气田管输天然气在进入国家管网前提取氦气、乙烷混合物高附加值产品,实现气田经济效益最大化。
Description
技术领域
本发明涉及氦气生产技术领域,具体指一种具有乙烷混合物回收的膜法天然气提氦设备及工艺。
背景技术
氦气是宇宙中不可再生的战略资源,关系国计民生。我国氦气资源分布虽广,但是是品位很多,多属于贫氦、特贫氦。国内的天然气主要产自各大油气田,大约90%以管输天然气的形式输送至国家管网或下游用户。由于不具备开采价值,使有限的氦气资源得不到回收利用。
此外,天然气中通常含有一定量的(5%~15%)乙烷、丙烷以及更重的烃类组分(乙烷混合物),天然气中的乙烷混合物回收后可进一步分离得到乙烷、液化石油气和稳定轻烃等产品。这些产品是优质的化工原料和民用及工业燃料,具有很高的附加值,亦以普通天然气产品的价格送往下游。
现有技术中可以用于产气的油气田与下游天然气用户或国家管网之间提取氦气的大致分为两种:一种是直接采用深冷法从天然气中提取氦气,这需要将接近100%的组分全部节流减压、液化分离、气化、升压,需要额外的冷冻循环使低位温区达到近-190℃,过程中存在大量的不可逆损失、机械损失、热量损失,因此能耗大、投资高,特别是对国内的贫氦天然气无工业化价值;另一种是采用全常温法技术路线,虽然较深冷法有竞争力,但不能提取乙烷混合物,使高附加值产品按天然气的收益流失到下游管网。
例如,CN202973762U公开了一种天然气低温提氦系统,包括原料气冷却器、一级提浓塔、二级提浓塔、深冷器、膨胀机组、氮气压缩机和氮气缓冲罐,采用后膨胀+氮循环制冷两塔分离技术;该技术是利用深冷法直接从天然气中提取氦气,其必须将全部甲烷液化去生产微量的氦气,经济性差,在国内贫氦上无应用业绩。CN212292809U提供了一种多级提氦装置及氦气分离系统,用于从天然气中提取氦气,包括多级膜分离单元和除氢单元,多级膜分离单元包括至少三级膜分离组,分别为第一级膜分离组至第N级膜分离组,每一级膜分离组的渗透气出口与下一级膜分离组的进气口连通,除氢单元设置于任意相邻的两级膜分离组之间;该技术在节能上比深冷法具有一定优势,但对于贫氦天然气未考虑回收高附加值的乙烷混合物(C2+),在氦气价格较低时,经济效益差。CN217148577U公开了一种从低含氦BOG中提取高纯氦气的系统,包括一级膜分离器、二级膜分离器、一段脱氢单元、二段脱氢单元、PSA单元、低温吸附单元等,BOG连接第一压缩机后连接一段脱氢,再连接一级膜分离器入口,一级膜分离非渗透气排出系统;一级膜分离渗透气连接第二压缩机后连接二级膜分离器入口;二级膜分离非渗透气连接一段脱氢单元入口进行循环;二级膜分离渗透气连接第三压缩机后连接二段脱氢单元,再连接变压吸附单元入口;PSA吸附器顶部氦气出口连接低温吸附单元后获得高纯氦气;该法采用BOG深冷+膜分离工艺路线,原料条件限定为LNG产生的BOG,而国内LNG消费占比仅约10%,严重制约了天然气资源中氦气回收利用问题。
因此,对于目前从天然气中提取氦气的技术,有待于做进一步的改进。
发明内容
本发明所要解决的第一个技术问题是针对现有技术的现状,提供一种能在回收氦气的同时提取具有较高附加值的乙烷混合物的膜法天然气提氦设备。
本发明所要解决的第二个技术问题是针对现有技术的现状,提供一种特别适用于气田管输天然气在进入国家管网前提取氦气、乙烷混合物高附加值产品,实现气田经济效益最大化的具有乙烷混合物回收的膜法天然气提氦设备。
本发明所要解决的第三个技术问题是针对现有技术的现状,提供一种具有乙烷混合物回收的膜法天然气提氦工艺。
本发明解决上述技术问题所采用的技术方案为:
一种具有乙烷混合物回收的膜法天然气提氦设备,包括:
过滤分离器,具有供甲烷混合气输入的入口,用于脱除甲烷混合气的润滑油雾、水和机械杂质;
膜分离系统,进口与所述过滤分离器的出口相连接,用于对物料进行渗透分离得到送天气然管网的非渗透气及氦气提浓后的渗透气;
压缩机,与所述膜分离系统相连接,用于对物料进行至少一次加压;
脱氢单元,与所述压缩机的相连接,用于对一次加压后工艺气中的氢进行脱除;以及
提纯单元,用于降低工艺气的水露点并脱除CH4、N2、Ar、O2、Ne中的至少一种。
优选地,所述膜分离系统包括依次串接的一级膜分离器、二级膜分离器、三级膜分离器,所述一级膜分离器与二级膜分离器之间设置有一级压缩机,所述二级膜分离器与三级膜分离器之间设置有二级压缩机。
优选地,所述脱氢单元包括有串接于所述二级压缩机级间的一级脱氢反应器,所述二级压缩机用于将输入一级脱氢反应器的工艺气加压至第一压力、将输入三级膜分离器的工艺气加压至第二压力,所述第一压力小于或等于第二压力。
优选地,所述三级膜分离器的下游设置有三级压缩机,该三级压缩机位于所述提纯单元的上游,所述脱氢单元还包括有串接于所述三级压缩机级间的二级脱氢反应器,所述三级压缩机用于将输入二级脱氢反应器的工艺气加压至第三压力、将输入提纯单元的工艺气加压至第四压力,所述第三压力小于或等于第四压力。
进一步优选,所述第一压力小于第二压力,所述第三压力等于第四压力。
优选地,所述二级膜分离器与二级压缩机之间设置有能对来自膜分离系统及提纯单元的含氦气体进行收集的缓冲器,该缓冲器具有与所述二级膜分离器的渗透气侧相连接的第一入口、与提纯单元的尾气出口相连接的第二入口、与三级膜分离器的渗透气侧直接或间接连接的第三入口、与二级压缩机的入口相连接的出口。
本发明还包括尾气混合罐及再回收膜分离器,所述再回收膜分离器设于三级膜分离器与缓冲器之间,用于将三级膜分离器渗透气侧所得工艺气进一步分离提浓,所述再回收膜分离器的渗透气侧的出口与尾气混合罐的入口相连通,所述再回收膜分离器的非渗透气侧的出口与缓冲器的第三入口相连通;所述一级膜分离器的非渗透侧的出口、二级膜分离器的非渗透侧的出口均与尾气混合罐的入口相连通,所述尾气混合罐的出口连接天气然管网。
优选地,所述提纯单元包括依次串接的干燥单元及吸附单元,所述干燥单元用于将水露点降至3℃~6℃,所述吸附单元用于脱除剩余的CH4、N2、Ar、O2、Ne杂质中的至少一种,所述吸附单元输出高纯氦气。
优选地,所述的甲烷混合气来自天然气深冷分离乙烷工段并经送料管线输送至过滤分离器,所述送料管线与天气然管网之间连接有旁路且该旁路上设置有能在管网压力达高限时打开旁路的旁路控制器;所述天然气深冷分离乙烷工段中设置有能根据流量比例自动调节干气流量的干气循环控制器。
一种具有乙烷混合物回收的膜法天然气提氦工艺,包括以下步骤:
甲烷混合气首先进入过滤分离器脱除全部润滑油雾、水和机械杂质,进入一级膜分离器,非渗透气直接送至尾气混合罐,渗透气为常压或负压,氦气浓度约0.5%~0.7%,通过一级压缩机升压后送至二级膜分离器,渗透气氦气浓度变为3%~4%,通过缓冲器被二级压缩机首先压缩至第一压力从级间抽出进入一级脱氢反应器,在催化剂的作用下将H2脱除至不高于1ppmv返回级间继续压缩至比第一压力大的第二压力进入三级膜分离器,在渗透侧氦气浓度被提浓为45%~56%送至三级压缩机入口,首先被升压至第三压力从级间抽出送至二级脱氢反应器将工艺气中的残氢脱除至20ppbv以下,继续被压缩至与第三压力相等的第四压力,进入干燥单元将水露点降至3℃~6℃,再经吸附单元脱除剩余的CH4、N2、Ar、O2、Ne杂质中的一种或几种后得到纯度为99.999%的氦气;
其中,三级膜分离器的非渗透气氦气浓度3%~6%经再回收膜分离器进一步提浓至16%~20%汇入缓冲器进行回收;吸附单元的尾气氦气亦汇入缓冲器进行回收;
二级膜分离器、再回收膜分离器的非渗透气同样汇入尾气混合罐作为外输天然气产品送入天然气管网。
优选地,为防止膜分离工段突然跳闸对乙烷回收工段造成影响,设置旁路控制器自动在管网压力达3.5MPa打开旁路阀。
优选地,为了提高乙烷回收工段的循环干气的可靠供给,设置干气循环控制器,根据流量比例(8%~12%)自动调节干气流量。
优选地,膜分离器渗透测压力可控制在-20kPa~20kPa,由其出口的压缩机进行自动控制,也可在压缩机前设置抽真空设备,如真空泵或真空抽吸器。
本发明的天然气深冷分离乙烷工段为部分干气回流工艺(RSV)。
本发明对多股低压气体设置了缓冲器,无论是一级膜分离、二级膜分离或者三级膜分离后,具体根据循环气汇入位置确定,有效的抑制压力波动和均匀组分,使膜分离器和压缩机操作平稳。设置多级加氢,有效的控制温升,更有利于保证高纯氦气产品质量。
在本发明中,尤为重要的是,本发明将天然气深冷分离乙烷工段的低温位控制在-110℃以上,优选为-90℃~-110℃,进一步优选为-100℃,相较于现有技术中深冷提取氦气需要至少-190℃的条件,本发明不仅节能效果显著,而且由于本发明只把占比5%~15%乙烷混合物(C2+)液化而不将全部天然气液化,膜分离工段不需脱碳、脱硫,提高了整个工艺氦气及乙烷混合物收率,本发明整个工艺的氦气回收率可达90%~93%,乙烷混合物的收率在95~99%。
优选地,本发明可在提纯单元后增加液氦流程生产液氦。本发明膜分离工段的膜的级数、脱氢的级数根据原料气的条件和回收率的要求综合确定,不限制具体数量。本发明脱氢单元的位置、循环气的汇入位置为针对假定参数的最佳位置,实际应用时可以根据具体情况有多种变化。
为了提高膜分离气的分离性能,可以将每级压缩机作为热源,用压缩机末级冷却器作为温度调节措施,入膜温度控制在40℃~55℃为宜。为了降低膜的投资,可以在每级膜分离器的渗透侧设置抽真空装置,提高真空度。
与现有技术相比,本发明的优点在于:
本发明采用深冷耦合膜分离法从油气田处理后的天然气中分离氦气并联产乙烷混合物,针对国内天然气贫氦、特贫氦、无工业利用价值的窘状,在回收氦气的同时提取具有较高附加值的乙烷混合物,使低品位氦气资源的提取变得经济可行,大大降低了氦气资源的工业品位,拓展了可利用氦气资源的范围;本发明特别适用于气田管输天然气在进入国家管网前提取氦气、乙烷混合物高附加值产品,实现气田经济效益最大化;
本发明采用深冷耦合膜分离法,从贫氦天然气(0.005-0.05%He)中提纯氦气、同时提取乙烷混合物,剩余不含乙烷混合物和氦气的贫气送往下游,最大限度地回收了天然气产品中的高附加值组分,实现了油气田产品的多元化;该法较传统的全深冷流程能耗低,同时又克服了全常温法产品单一的缺点;
本发明较单一的膜分离法,增产了具有较高附加值的乙烷混合物,使得特贫氦资源的提取具备了工业化价值,实现了气田产品多元化,增加了国家氦气储备;乙烷混合物作为乙烯裂解的优质原料,大大提升了乙烯的收率,从而实现上下游全产业链效益最大化;本发明采用与深冷法耦合工艺,节省了膜分离的前处理系统、脱碳、脱硫环节,大大简化了流程;
国内主流的BOG深冷提氦技术对原料限定为LNG的BOG,而国内天然气约90%以气态形式消费,BOG深冷提氦技术市场前景小,本发明提出的技术适用于下游用户为气态形式的用户,市场占比90%,当氦气含量在0.005%以上且乙烷混合物含量在5%以上,日处理量在200万方时,可获得较好的经济效益,利于推广。
附图说明
图1为本发明实施例的结构示意图;
其中,过滤分离器(1)、一级膜分离器(2)、一级压缩机(3)、二级膜分离器(4)、缓冲器(5)、二级压缩机(6)、一级脱氢反应器(7)、三级膜分离器(8)、三级压缩机(9)、二级脱氢反应器(10)、干燥单元(11)、吸附单元(12)、再回收膜分离器(13)、尾气混合罐(14)、旁路控制器(15)、干气循环控制器(16)。
具体实施方式
以下结合附图实施例对本发明作进一步详细描述。
如图1所示,本实施例具有乙烷混合物回收的膜法天然气提氦设备包括:
过滤分离器1,具有供甲烷混合气输入的入口,用于脱除甲烷混合气的润滑油雾、水和机械杂质;
膜分离系统,进口与过滤分离器1的出口相连接,用于对物料进行渗透分离得到送天气然管网的非渗透气及氦气提浓后的渗透气;
压缩机,与膜分离系统相连接,用于对物料进行至少一次加压;
脱氢单元,与压缩机的相连接,用于对一次加压后工艺气中的氢进行脱除;以及
提纯单元,用于降低工艺气的水露点并脱除CH4、N2、Ar、O2、Ne中的至少一种。
具体的,本实施例的膜分离系统包括依次串接的一级膜分离器2、二级膜分离器4、三级膜分离器5,一级膜分离器2与二级膜分离器4之间设置有一级压缩机3,二级膜分离器4与三级膜分离器8之间设置有二级压缩机6。
脱氢单元包括有串接于二级压缩机6级间的一级脱氢反应器7,二级压缩机6用于将输入一级脱氢反应器7的工艺气加压至第一压力、将输入三级膜分离器8的工艺气加压至第二压力,第一压力小于第二压力。三级膜分离器8的下游设置有三级压缩机9,该三级压缩机9位于提纯单元的上游,脱氢单元还包括有串接于三级压缩机9级间的二级脱氢反应器10,三级压缩机9用于将输入二级脱氢反应器10的工艺气加压至第三压力、将输入提纯单元的工艺气加压至第四压力,第三压力等于第四压力。
二级膜分离器4与二级压缩机6之间设置有能对来自膜分离系统及提纯单元的含氦气体进行收集的缓冲器5,该缓冲器5具有与二级膜分离器4的渗透气侧相连接的第一入口、与提纯单元的尾气出口相连接的第二入口、与三级膜分离器8的渗透气侧间接连接的第三入口、与二级压缩机6的入口相连接的出口。
本实施例还包括尾气混合罐14及再回收膜分离器13,再回收膜分离器13设于三级膜分离器8与缓冲器5之间,用于将三级膜分离器8渗透气侧所得工艺气进一步分离提浓,再回收膜分离器13的渗透气侧的出口与尾气混合罐14的入口相连通,再回收膜分离器13的非渗透气侧的出口与缓冲器5的第三入口相连通;一级膜分离器2的非渗透侧的出口、二级膜分离器4的非渗透侧的出口均与尾气混合罐14的入口相连通,尾气混合罐14的出口连接天气然管网。
本实施例的提纯单元包括依次串接的干燥单元11及吸附单元12,干燥单元11用于将水露点降至3℃~6℃,吸附单元12用于脱除剩余的CH4、N2、Ar、O2、Ne等全部杂质,吸附单元12输出高纯氦气。
本实施例的甲烷混合气来自天然气深冷分离乙烷工段A并经送料管线a输送至过滤分离器1,送料管线a与天气然管网之间连接有旁路且该旁路上设置有能在管网压力达高限时打开旁路的旁路控制器15;天然气深冷分离乙烷工段A中设置有能根据流量比例自动调节干气流量的干气循环控制器16。
本实施例具有乙烷混合物回收的膜法天然气提氦工艺,包括以下步骤:
来自气田处理厂的压力约为3.5MPa管输天然气,氦气含量约0.05%,乙烷混合物含量约5%~15%,首先进入天然气深冷分离乙烷工段A回收乙烷混合物;天然气经过前端净化、预冷、部分冷凝送入脱甲烷塔,在约-100℃,1.7MPa的条件经闪蒸、气提进行分离,在塔底获得其中大约95%~99%的乙烷混合物作为外输产品,同时在塔顶抽出甲烷混合气(CH4、N2、Ar、He、H2、少量C2+)经板式换热器复热、膨胀机增压端压缩至约3.0MPa,送至膜分离工段提纯氦气;
甲烷混合气首先进入过滤分离器1脱除全部润滑油雾、水和机械杂质,进入一级膜分离器2,非渗透气几乎不减压直接送至尾气混合罐14,渗透气为常压或负压,氦气浓度约0.5%~0.7%,通过一级压缩机3升压至3.0MPa,送至二级膜分离器4,渗透气氦气浓度变为3%~4%,通过缓冲器5被二级压缩机6首先压缩至1.5MPa、150℃从级间抽出进入一级脱氢反应器7,在催化剂钯的作用下将H2脱除至1ppmv返回级间继续压缩至3.2MPa进入三级膜分离器8,在渗透侧氦气浓度被提浓为45%~56%送至三级压缩机9入口,首先被升压至1.5MPa、150℃从级间抽出送至二级脱氢反应器10将工艺气中的残氢脱除至20ppbv以下,继续被压缩至1.5MPa,进干燥单元11将水露点降至3℃~6℃,再经吸附单元12脱除剩余的CH4、N2、Ar、O2、Ne等杂质后得到纯度为99.999%的氦气;
其中,三级膜分离器8的非渗透气氦气浓度约3%~6%经再回收膜分离器13进一步提浓至16%~20%汇入缓冲器5进行回收;吸附单元12的尾气氦气含量较高亦汇入缓冲器5进行回收;
二级膜分离器4、再回收膜分离器13的非渗透气同样汇入尾气混合罐14作为外输天然气产品送入天然气管网;
旁路控制器15自动在管网压力达3.5MPa打开旁路阀;干气循环控制器16根据流量比例(8%~12%)自动调节干气流量;
各膜分离器渗透测压力控制在-20kPa~20kPa,由其出口的压缩机进行自动控制。
整个工艺的氦气回收率达90%~93%,乙烷混合物的收率在95~99%。
Claims (10)
1.一种具有乙烷混合物回收的膜法天然气提氦设备,其特征在于包括:
过滤分离器,具有供甲烷混合气输入的入口,用于脱除甲烷混合气的润滑油雾、水和机械杂质;
膜分离系统,进口与所述过滤分离器的出口相连接,用于对物料进行渗透分离得到送天气然管网的非渗透气及氦气提浓后的渗透气;
压缩机,与所述膜分离系统相连接,用于对物料进行至少一次加压;
脱氢单元,与所述压缩机的相连接,用于对一次加压后工艺气中的氢进行脱除;以及
提纯单元,用于降低工艺气的水露点并脱除CH4、N2、Ar、O2、Ne中的至少一种。
2.根据权利要求1所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述膜分离系统包括依次串接的一级膜分离器、二级膜分离器、三级膜分离器,所述一级膜分离器与二级膜分离器之间设置有一级压缩机,所述二级膜分离器与三级膜分离器之间设置有二级压缩机。
3.根据权利要求2所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述脱氢单元包括有串接于所述二级压缩机级间的一级脱氢反应器,所述二级压缩机用于将输入一级脱氢反应器的工艺气加压至第一压力、将输入三级膜分离器的工艺气加压至第二压力,所述第一压力小于或等于第二压力。
4.根据权利要求3所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述三级膜分离器的下游设置有三级压缩机,该三级压缩机位于所述提纯单元的上游,所述脱氢单元还包括有串接于所述三级压缩机级间的二级脱氢反应器,所述三级压缩机用于将输入二级脱氢反应器的工艺气加压至第三压力、将输入提纯单元的工艺气加压至第四压力,所述第三压力小于或等于第四压力。
5.根据权利要求4所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述第一压力小于第二压力,所述第三压力等于第四压力。
6.根据权利要求2所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述二级膜分离器与二级压缩机之间设置有能对来自膜分离系统及提纯单元的含氦气体进行收集的缓冲器,该缓冲器具有与所述二级膜分离器的渗透气侧相连接的第一入口、与提纯单元的尾气出口相连接的第二入口、与三级膜分离器的渗透气侧直接或间接连接的第三入口、与二级压缩机的入口相连接的出口。
7.根据权利要求6所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:还包括尾气混合罐及再回收膜分离器,所述再回收膜分离器设于三级膜分离器与缓冲器之间,用于将三级膜分离器渗透气侧所得工艺气进一步分离提浓,所述再回收膜分离器的渗透气侧的出口与尾气混合罐的入口相连通,所述再回收膜分离器的非渗透气侧的出口与缓冲器的第三入口相连通;所述一级膜分离器的非渗透侧的出口、二级膜分离器的非渗透侧的出口均与尾气混合罐的入口相连通,所述尾气混合罐的出口连接天气然管网。
8.根据权利要求1~7中任一项所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述提纯单元包括依次串接的干燥单元及吸附单元,所述干燥单元用于将水露点降至3℃~6℃,所述吸附单元用于脱除剩余的CH4、N2、Ar、O2、Ne杂质中的至少一种,所述吸附单元输出高纯氦气。
9.根据权利要求1~7中任一项所述的具有乙烷混合物回收的膜法天然气提氦设备,其特征在于:所述的甲烷混合气来自天然气深冷分离乙烷工段并经送料管线输送至过滤分离器,所述送料管线与天气然管网之间连接有旁路且该旁路上设置有能在管网压力达高限时打开旁路的旁路控制器;
所述天然气深冷分离乙烷工段中设置有能根据流量比例自动调节干气流量的干气循环控制器。
10.一种具有乙烷混合物回收的膜法天然气提氦工艺,其特征在于包括以下步骤:
来自天然气深冷分离乙烷工段的甲烷混合气首先进入过滤分离器脱除全部润滑油雾、水和机械杂质,进入一级膜分离器,非渗透气直接送至尾气混合罐,渗透气为常压或负压,氦气浓度约0.5%~0.7%,通过一级压缩机升压后送至二级膜分离器,渗透气氦气浓度变为3%~4%,通过缓冲器被二级压缩机首先压缩至第一压力从级间抽出进入一级脱氢反应器,在催化剂的作用下将H2脱除至不高于1ppmv返回级间继续压缩至比第一压力大的第二压力进入三级膜分离器,在渗透侧氦气浓度被提浓为45%~56%送至三级压缩机入口,首先被升压至第三压力从级间抽出送至二级脱氢反应器将工艺气中的残氢脱除至20ppbv以下,继续被压缩至与第三压力相等的第四压力,进入干燥单元将水露点降至3℃~6℃,再经吸附单元脱除剩余的CH4、N2、Ar、O2、Ne杂质中的一种或几种后得到高纯氦气;
其中,所述天然气深冷分离乙烷工段的低温位控制在-110℃以上。
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