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CN101952003A - 分离方法 - Google Patents

分离方法 Download PDF

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CN101952003A
CN101952003A CN2008800071052A CN200880007105A CN101952003A CN 101952003 A CN101952003 A CN 101952003A CN 2008800071052 A CN2008800071052 A CN 2008800071052A CN 200880007105 A CN200880007105 A CN 200880007105A CN 101952003 A CN101952003 A CN 101952003A
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fraction
rich
methane
separation
rectification
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H·施密特
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Linde GmbH
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Abstract

本发明描述了从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法，其中对富含烃类的馏份实施一级或多级降压，精馏分离甲烷，并对在甲烷分离中获得的甲烷贫化的馏份实施精馏分离C2、C2/CO2、C2+或C3+。根据本发明，精馏分离甲烷塔(M)的塔底加热装置(E2)经由C3冷却循环(V4，E4，E5，20～27)与精馏分离C2、C2/CO2、C2+或C3+塔(E)的塔顶冷却装置(E3)相连接。

Description

分离方法
技术领域
本发明涉及从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法，其中对富含烃类的馏份实施一级或多级降压，精馏分离甲烷，并对在甲烷分离中获得的甲烷贫化的馏份实施精馏分离C2、C2/CO2、C2+或C3+。
背景技术
在从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法中存在的基本要求是尽可能有效地利用已存在的冷量供应。这在粗煤气压力高的情况下发生，在此压力通常大于60巴，其中对富含烃类的馏份实施一级或多级降压。若为此使用多个膨胀透平，则可将它们并联和/或串联排列。
若待分离的富含烃类的馏份的压力低于40巴，则通过待分离的富含烃类的馏份可提供的冷量供应通常不足。这导致必须额外提供冷量。这例如借助于C2/3冷却循环而进行，其不仅用于待分离的富含烃类的馏份的预冷却，而且用于脱乙烷塔的冷凝器。
对于中等的粗煤气压力，在此压力通常在70至90巴之间，目前不存在工艺技术上有效的解决方案。目前在该压力范围内通常采用多级冷却循环。但这需要比较高的投资成本和运行成本，而且使此类方法无法不明显地复杂化。此外应当注意，待分离的富含烃类的馏份的温度波动导致脱甲烷塔的塔底温度同样发生波动，并与此同时无法按照规格提供C2或C3产品。
发明内容
本发明的目的在于提供避免了上述缺点的用于从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法。
为了实现该目的，建议从富含烃类的馏份分离出富含C2+或富含C3+的馏份的方法，其特征在于，精馏分离甲烷塔的塔底加热装置经由C3冷却循环与精馏分离C2、C2/CO2、C2+或C3+塔的塔顶冷却装置相连接。
根据本发明，现在仅采用优选以一级构成的C3冷却循环。其是在精馏分离甲烷塔的塔底加热装置与精馏分离C2、C2/CO2、C2+或C3+塔的塔顶冷却装置之间的“连接”。因此，得到在工艺技术上简单、同时有效的方法流程，其不仅成本低廉而且节约能源。此外，将导出的热量送至该过程，并因此在待分离的富含烃类的馏份的粗煤气温度可能的波动方面使脱甲烷过程实现更大的灵活性。
此外，根据本发明从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法可以在排出富含C2+/CO2的液体馏份的脱甲烷塔塔底中以及在排出待获得的C2、C2/CO2、C2+或C3+产品馏份的脱乙烷塔塔顶中在工艺技术上简单地控制和调节产品规格。
因为在已知的现有技术中，通常通过粗煤气实施脱甲烷塔的塔底加热，并通过冷却循环实施脱乙烷塔的塔顶冷却，与此相比根据本发明的方法则实现了脱甲烷塔的塔底加热与粗煤气冷却的分离，所以使塔底加热与塔顶冷却所需的控制简单化。这还适合于在启动和部分负荷运行时在工艺技术上的控制。
根据本发明从富含烃类的馏份分离出富含C2+的馏份的方法的另一个有利的实施方案的特征在于
-以一级构成C3冷却循环，
-在分离的热交换器中实施在C3冷却循环的冷却剂与塔底加热装置的介质和塔顶冷却装置的介质之间的热交换，
-将在精馏分离C2、C2/CO2、C2+或C3+塔中获得的液体馏份的部分流作为回流送至精馏分离甲烷塔。
下面依照在附图中所示的获得C2+产品馏份的方法实施例更详细地阐述根据本发明从富含烃类的馏份分离出富含C2+或富含C3+的馏份的方法及其另外的实施方案。
附图说明
图1所示为根据本发明的实施方案。
具体实施方式
富含烃类的馏份经由管道1送入第一膨胀透平X1。该富含烃类的馏份的压力优选在70至120巴之间。需要时，对富含烃类的馏份实施附图中未示出的预处理，其中去除非期望的组分，如水和二醇。
在第一膨胀透平X1中减压的富含烃类的馏份经由管道2送入热交换器E1，在其中与自身相对地进行冷却。从热交换器E1排出之后，将富含烃类的馏份分成两股部分流3和4。第一部分流3在热交换器E1中进一步冷却并完全冷凝之后送至脱甲烷塔M的塔顶。
第二部分流4在第二膨胀透平X2中减压，随后经由管道5同样送入脱甲烷塔M的塔顶区域。在此，第二部分流的输入点优选位于第一部分流的输入点下方。
还可代替两个串联设置的膨胀透平X1和X2，安装多于两个的膨胀透平，它们可以并联和/或串联的方式排列。
脱甲烷塔M优选在20至35巴之间的压力范围内运行。从脱甲烷塔M的塔顶区域经由管道6排出富含甲烷的气体馏份，在热交换器E1中与在管道2和3中待冷却的富含烃类的馏份或部分馏份相对地进行加热，随后压缩至所希望的输出压力。
此外，附图所示为由压缩级V1、V2和V3构成的三级压缩单元。在此，压缩器或压缩级V1和V2与膨胀透平X1和X2相连接，如虚线所示。在压缩至优选在50至120巴的范围内的所期望的输出压力之后，富含甲烷的气体馏份经由管道7送至其另外的用途。
脱甲烷塔M的塔底加热以如下方式实现：从脱甲烷塔M的塔底区域经由管道9排出富含C2+的馏份，在热交换器E2中与尚待说明的冷却循环的冷却剂相对地进行加热，随后经由管道10重新送入脱甲烷塔M。
从脱甲烷塔M的塔底经由管道8排出甲烷贫化的馏份，送至脱乙烷塔E。其优选在20至35巴之间的压力范围内运行。
从脱乙烷塔E的塔底经由管道16排出富含丙烷的液体馏份，借助泵P泵压至所期望的输出压力，并混入在管道7中处于更高压力下的富含甲烷的气体馏份。
在脱乙烷塔E的塔顶经由管道11排出气态C2产品馏份。在热交换器E3中与尚待说明的冷却循环的冷却剂相对地进行冷却，并部分冷凝，随后经由管道12送入分离器D。在该分离器D中产生的液体馏份经由管道15送入泵P2，在该泵P2中至少泵压至脱乙烷塔E中的压力，随后经由管道15送入脱乙烷塔E的塔顶区域。
在分离器D的塔顶经由管道13排出气态C2产品馏份，并送至其另外的用途。若C2产品馏份含有二氧化碳并且期望将其从C2产品馏份分离出，则在脱乙烷塔E下游设置附图中未示出的二氧化碳去除过程。
根据本发明，上述的脱甲烷塔的塔底加热装置与上述的脱乙烷塔的塔顶冷却装置经由C3冷却循环相连接。该C3冷却循环由管道段20至27、分离器D′、储存或储备容器D″、压缩机V4及两个后期冷却器E4和E5组成。
在压缩机V4中压缩至优选为8至16巴的所期望的循环压力的冷却剂经由管道20送入第一后期冷却器E4，在该第一后期冷却器E4中例如与冷却水相对地进行冷却。随后分成两股冷却剂部分流21和22，其中第一部分流送入第二冷却器E5，在该第二冷却器E5中与诸如冷却水的适当冷却介质相对地进行冷凝。
上述的第二冷却剂部分流经由管道22送入热交换器E2，在该热交换器E2中与管道9中待加热的液体流相对地进行冷凝，该液体流用于加热脱甲烷塔M的塔底。
随后将该冷却剂部分流经由管道23混入从第二后期冷却器E5经由管道24排出的第一冷却剂部分流，并引导通过储备容器D″。该储存或储备容器D″用于在设备或过程停止状态下储存冷却剂。随后该冷却剂经由管道25送入热交换器E3，并在该热交换器E3中与在管道11中待冷却的富含C2的气体馏份相对地进行蒸发。
随后经由管道26将经加热的冷却剂送入设置在压缩机V4上游的分离器D′。从其塔顶将气态冷却剂经由管道27送入压缩机V4。
根据本发明设置的C3冷却循环如附图所示的结构布置能够与在脱甲烷塔M和脱乙烷塔E中所实现的分离过程的各自负荷无关地运行冷却循环。
为了提高脱甲烷塔M中的C2产率，根据本发明方法的一个优选的实施方案，经由管道17排出在脱乙烷塔E中获得的液体馏份16的至少一部分流，在热交换器E1中过冷，随后经由管道18作为回流送入脱甲烷塔M。在此优选在待分离的富含烃类的馏份的部分流3的输入位置上方送入该部分流17/18。
需要强调的是，根据本发明的方法不仅可用于从富含烃类的馏份分离出富含C2+的馏份，而且还可用于从富含烃类的馏份分离出富含C2、C2/CO2或C3+的馏份。

Claims (4)

1.从富含烃类的馏份分离出富含C2、C2/CO2、C2+或C3+的馏份的方法，其中对富含烃类的馏份实施一级或多级降压，精馏分离甲烷，并对在甲烷分离中获得的甲烷贫化的馏份实施精馏分离C2、C2/CO2、C2+或C3+，其特征在于，精馏分离甲烷塔(M)的塔底加热装置(E2)经由C3冷却循环(V4，E4，E5，20～27)与精馏分离C2、C2/CO2、C2+或C3+塔(E)的塔顶冷却装置(E3)相连接。
2.根据权利要求1的方法，其特征在于，所述C3冷却循环(V4，20～27)以一级构成。
3.根据权利要求1或2的方法，其特征在于，在分离的热交换器(E2，E3)中实施在C3冷却循环的冷却剂与塔底加热介质和塔顶冷却介质之间的热交换。
4.根据权利要求1至3之一的方法，其特征在于，将在精馏分离C2、C2/CO2、C2+或C3+塔(E)中获得的液体馏份(16)的部分流(17，18)作为回流送至精馏分离甲烷塔(M)。
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