CN102334001B - 液化方法和*** - Google Patents
液化方法和*** Download PDFInfo
- Publication number
- CN102334001B CN102334001B CN2009801459553A CN200980145955A CN102334001B CN 102334001 B CN102334001 B CN 102334001B CN 2009801459553 A CN2009801459553 A CN 2009801459553A CN 200980145955 A CN200980145955 A CN 200980145955A CN 102334001 B CN102334001 B CN 102334001B
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- Prior art keywords
- heat exchanger
- stream
- gaseous refrigerant
- expander
- expansion
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 78
- 239000003507 refrigerant Substances 0.000 claims abstract description 157
- 238000001816 cooling Methods 0.000 claims abstract description 71
- 238000005057 refrigeration Methods 0.000 claims abstract description 42
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 49
- 239000007788 liquid Substances 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 21
- 239000003345 natural gas Substances 0.000 claims description 19
- 230000008016 vaporization Effects 0.000 claims description 18
- 238000009834 vaporization Methods 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000000284 extract Substances 0.000 claims description 4
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 12
- 239000012071 phase Substances 0.000 description 9
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 8
- 230000006835 compression Effects 0.000 description 7
- 238000007906 compression Methods 0.000 description 7
- 239000002826 coolant Substances 0.000 description 6
- 239000001294 propane Substances 0.000 description 6
- 238000004804 winding Methods 0.000 description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 5
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 5
- 229910052782 aluminium Inorganic materials 0.000 description 5
- 238000007667 floating Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- VOPWNXZWBYDODV-UHFFFAOYSA-N Chlorodifluoromethane Chemical compound FC(F)Cl VOPWNXZWBYDODV-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000001273 butane Substances 0.000 description 4
- ILEDWLMCKZNDJK-UHFFFAOYSA-N esculetin Chemical compound C1=CC(=O)OC2=C1C=C(O)C(O)=C2 ILEDWLMCKZNDJK-UHFFFAOYSA-N 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000001282 iso-butane Substances 0.000 description 4
- 235000013847 iso-butane Nutrition 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- 230000005514 two-phase flow Effects 0.000 description 4
- 238000013459 approach Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 230000007704 transition Effects 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000013526 supercooled liquid Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 230000008646 thermal stress Effects 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000035882 stress Effects 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
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- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
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- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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Abstract
使用闭环制冷***液化进料气体,其中使冷却的压缩气态制冷剂流(150)膨胀(136)以提供第一膨胀气态制冷剂流(154),第一膨胀气态制冷剂流(154)基本上为蒸汽且用于通过间接热交换(110)来冷却且基本上液化进料气流(100)。基本上液化的进料气流(102)优选地通过与第二膨胀气态制冷剂流(172)间接热交换(112)而过冷,第二膨胀气态制冷剂流(172)优选地也基本上为蒸汽且可由冷却的压缩气态制冷剂流(170)或者由第一膨胀气态制冷剂流(152)的一部分提供。用于压缩气态制冷剂流(146)的冷却负荷由第一膨胀气态制冷剂流(152)的一部分(160)、通过与进料气体进行所述热交换(110)而部分地温热的气态制冷剂(156)和/或通过所述过冷(112)而温热的第二膨胀气态制冷剂流(174)提供。
Description
背景技术
液化方法和***是已知的,其中通过以逆布雷顿循环(Brayton cycle)使气态制冷剂膨胀而产生制冷。这些方法和***通常采用两个膨胀器,其中使气态制冷剂在设备压降公差内膨胀到基本上相同压力。一些***还包括多于两个膨胀器,其中冷膨胀器排放压力高于其余膨胀器的排放压力。这些方法和***具有潜在地简单的压缩***(因为并无流引入到压缩级之间)和简单的热交换器(因为存在更少的通路和集管)。另外一些方法和***是开环***,其利用液化流体作为制冷剂。
但用于液化的先前方法和***由于若干原因是有问题的。举例而言,使用简单压缩***和简单热交换器不能得到改进的效率。此外,使用开环***的成本节省并不胜过使用闭环***的灵活性。
需要一种液化方法和***,其中预冷、液化和过冷的步骤更安全、高效且可靠。
发明内容
本发明的实施例通过提供安全、高效和可靠的***和过程用于液化,特别地用于天然气液化而满足本领域中的这种需要。
根据一个示范性实施例,公开了一种使用闭环制冷***的液化方法,该方法包括以下步骤:(a)在至少一个压缩机中压缩气态制冷剂流;(b)在第一热交换器中冷却该压缩气态制冷剂流;(c)在第一膨胀器中使自第一热交换器的冷却的压缩气态制冷剂流的至少第一部分膨胀以提供第一膨胀气态制冷剂流;以及,(d)在第二热交换器中通过与自第一膨胀器的第一膨胀气态制冷剂流的至少第一部分进行间接热交换而冷却且基本上液化进料气流以形成基本上液化的进料流,其中离开第一膨胀器的第一膨胀气态制冷剂流基本上为蒸汽。
根据另一示范性实施例,公开了一种使用闭环制冷***的液化方法,该方法包括以下步骤:(a)在低压压缩机中压缩气态制冷剂流;(b)在高压压缩机中进一步压缩该压缩气态制冷剂流;(c)在第一热交换器中冷却该压缩气态制冷剂流;(d)在第一膨胀器中使自第一热交换器的冷却的压缩气态制冷剂流的至少第一部分膨胀以提供第一膨胀气态制冷剂流,其中自第一膨胀器的第一膨胀气态制冷剂流提供对第二热交换器和第一热交换器的冷却;(e)通过在第二热交换器和第一热交换器中与自第一膨胀器的第一膨胀气态制冷剂流进行间接热交换器来冷却并基本上液化进料气流;以及,(f)通过在过冷器交换器中与离开第二膨胀器的第二膨胀气态制冷剂流进行间接热交换而过冷该冷却且基本上液化的进料气流,其中离开第一膨胀器的第一膨胀气态制冷剂流和离开第二膨胀器的第二膨胀气态制冷剂流基本上为蒸汽,且第二膨胀气态制冷剂流的压力低于第一膨胀气态制冷剂流的压力。
根据又一示范性实施例,公开了一种用于液化的闭环***,其包括:制冷回路,该制冷回路包括:第一热交换器;第二热交换器,其流体地联接到第一热交换器;第一膨胀器,其流体地联接到第一热交换器且适于自第一热交换器接受制冷剂流;第二膨胀器,其流体地联接到第二热交换器且适于自第二热交换器接受制冷剂流;以及,第三热交换器,其流体地联接到第一膨胀器且适于接受自第一膨胀器的第一膨胀气态制冷剂流和进料气流,其中自第一膨胀器的第一膨胀气态制冷剂流和自第二膨胀器的第二膨胀气态制冷剂流基本上为蒸汽流。
如本文所用的术语“基本上”在液相或气相的情形下表示相关流分别具有至少80摩尔%,优选地至少90摩尔%,特别地至少95摩尔%的液体含量或蒸汽含量,且可完全为液体或蒸汽。举例而言,陈述“离开第一膨胀器的第一膨胀气态制冷剂流基本上为蒸汽”表示该流为至少80摩尔%蒸汽且可为100摩尔%蒸汽。
根据另一示范性实施例,公开了一种使用具有至少两个膨胀器的闭环蒸汽膨胀循环来液化气态进料的方法,其中,第二膨胀器的排放压力低于第一膨胀器的排放压力,以及第一膨胀器提供液化气态进料所需制冷的至少一部分。
附图说明
前文的简要总结以及下文示范性实施例的详细描述,当结合附图阅读时更好理解。出于说明本发明的实施例的目的,在附图中示出本发明的示范性构造,但本发明并不限于所公开的具体方法和仪器。在附图中:
图1示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图2示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图3示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图4示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图5示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图6示出涉及本发明多方面的示范性预冷制冷***和方法的流程图;
图7a是根据本发明的一实施例的冷却曲线的曲线图;
图7b是根据本发明的一实施例的冷却曲线的曲线图;
图7c是根据本发明的一实施例的冷却曲线的曲线图;
图8示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图9示出涉及本发明多方面的示范性气体液化***和方法的流程图;
图10示出涉及本发明多方面的示范性气体液化***和方法的流程图;以及
图11示出涉及本发明多方面的示范性气体液化***和方法的流程图。
具体实施方式
在一个示范性实施例中,液化过程可使用两个膨胀器且离开两个膨胀器的气态制冷剂流在每个膨胀器的排放中可基本上为蒸汽。由此术语“膨胀器”可用于描述在做外部功的同时使气体膨胀的诸如离心涡轮机或往复式膨胀器这样的装置。该过程可基本上等熵且通常被称作膨胀功或可逆绝热膨胀且不同于通过阀的等焓(焦耳-汤普森)节流。
冷膨胀器的排放压力可低于温热(最温热)的膨胀器的排放压力以实现更冷温度。自冷膨胀器的排放的气态制冷剂可用于过冷该液化产物。自温热(最温热)膨胀器的排放的制冷剂可用于液化。使用两种不同压力可更好地匹配例如天然气液化(即,预冷、液化和过冷)的冷却曲线。自温热(最温热)膨胀器的排放的气态制冷剂流可引入于气态制冷剂压缩机的级之间。进料气流和/或气态制冷剂可在闭环压缩循环中由另一制冷剂(诸如丙烷)预冷。进料气流和/或气态制冷剂也可例如由自第三膨胀器的气态制冷剂预冷。
在另一示范性实施例中,自温热(最温热)膨胀器的排放的气态制冷剂流可在单独压缩机中被压缩到最终排放压力,该单独压缩机的吸入压力高于用于压缩源自冷膨胀器的排放的气体的压缩机的吸入压力。
进料气流和/或制冷剂可例如通过汽化液态制冷剂预冷,液态制冷剂诸如CO2、甲烷、丙烷、丁烷、异丁烷、丙烯、乙烷、乙烯、R22、HFC制冷剂(包括但不限于R410A、R134A、R507、R23)或其组合。环保的氟化烃和其混合物可优选地用于离岸或浮动应用。举例而言,CO2可用作制冷剂。CO2预冷最小化物理占据面积,特别是对于离岸浮式采油贮油和卸油(FPSO)应用而言。
液态制冷剂可在一系列热交换器中在不同压力汽化,在多级压缩机中压缩,冷凝且被节流至待重新汽化的适当压力。利用适当密封***,压缩机吸入压力可保持在真空以允许冷却到更低温度。或者,该进料气流和/或气态制冷剂可通过在第三膨胀器中使相同气态制冷剂膨胀而预冷。
在另一示范性实施例中,进料气流可通过在第一组热交换器中与气态制冷剂间接热交换而冷却,第一组热交换器包括其中不冷却气体的至少一个热交换器。气态制冷剂可在第二组热交换器中冷却,第二组热交换器包括至少一个交换器。第一组热交换器可包括例如缠绕盘管热交换器。第二组热交换器可包括例如板翅式钎焊铝(芯)型热交换器。
在又一示范性实施例中,进料气流可在热交换器中冷却,气态制冷剂的一部分可在中间点(优选地在预冷部段与液化部段之间)自热交换器抽取。气态制冷剂可通过在属于第二组热交换器的热交换器中使液态制冷剂汽化而预冷。这种制冷剂可为例如氟化烃或CO2。
在另一示范性实施例中,进料气流可通过在一系列釜或壳管式热交换器中使液态制冷剂汽化而预冷。气态制冷剂的一部分也可在属于第二组热交换器的多流热交换器中冷却。气态制冷剂的另一部分可通过在一系列釜或壳管式热交换器中使液态制冷剂汽化而冷却至大约相同温度,一系列釜或壳管式热交换器可单独于用于预冷进料气流的热交换器或与之合并。
现参看具体附图,可采用各种实施例。在一个示范性实施例中且如图1所示,进料气流100可例如在热交换器110中由温热的氮气态制冷剂流154冷却和液化。
例如,进料气流100可为天然气。虽然本文所公开的液化***和方法可用于液化除了天然气之外的气体且因此进料气流100可为除了天然气之外的气体,但出于说明目的,其余示范性实施例将参考进料气流100为天然气流。
部分温热流154的一部分(流156)可从热交换器110抽取以平衡需要更少制冷的热交换器110的预冷(温热)部段。气态制冷剂流158可离开热交换器110的温热端以例如再循环。
例如离开热交换器110的冷端的基本上液化的天然气(LNG)流102可在过冷器交换器112中由温热气态制冷剂流172过冷,且在离开过冷器交换器112的冷端之后例如作为液化天然气产物104回收。气态制冷剂流174可离开过冷器交换器112的温热端。
气态低压制冷剂流140可在低压制冷剂压缩机130中压缩。所得到的流142可与流158和166合并且可作为流144进入高压制冷剂压缩机132。低压制冷剂压缩机130和高压制冷剂压缩机132可包括由环境热沉冷却的后冷却器和中间冷却器。热沉可例如为自水塔的冷却水、海水、淡水或空气。为了简单起见,中间冷却器和后冷却器未示出。
自高压制冷剂压缩机132的排放的高压制冷剂流146可在热交换器114中冷却。所得到的流148可被分成流150和168。
流150可在膨胀器136中膨胀以产生流152。膨胀器136可例如为蒸汽膨胀器。蒸汽膨胀器可为任何膨胀器,其中排放基本上为蒸汽(即,其中排放流为至少80%蒸汽)。流152可在热交换器110(上述流154)与热交换器116(作为流160)之间分配。流160可在热交换器116中温热。所得到的流162可与自热交换器110的流156合并。所得到的流164还可在热交换器114中被进一步温热以产生流166。
流168可在热交换器116中冷却。所得到的流170可在膨胀器138中膨胀以产生上述流172,流172然后可在过冷器交换器112中被温热。膨胀器138可例如为蒸汽膨胀器。所得到的流174可在热交换器116中被进一步温热以产生流176。流176可在热交换器114中被进一步温热以产生流140。
热交换器114可由制冷***120冷却,制冷***120包括至少一级汽化液态制冷剂,例如诸如CO2、甲烷、丙烷、丁烷、异丁烷、丙烯、乙烷、乙烯、R22、HFC制冷剂(包括但不限于R410A、R134A、R507、R23)或其组合。使用CO2作为预冷液态制冷剂被认为最小化物理占据面积,特别是对于浮式采油贮油和卸油(FPSO)应用而言。也可采用使用气态制冷剂的其它制冷循环。
热交换器114、116可例如合并成一个交换器。热交换器114、116也可例如为板翅式钎焊铝(芯)型热交换器。
热交换器110、112可例如合并或安装在彼此的顶部。热交换器110、112可例如为板翅式钎焊铝(芯)型热交换器。热交换器110、112也可例如为缠绕盘管型热交换器,其确保更好的安全性、耐用性和可靠性。例如可使用稳固型热交换来冷却天然气,因为天然气的冷却涉及可造成热交换器上更显著热应力的相变。可使用缠绕盘管热交换器,因为它们在相变期间通常不太易受热应力,包含泄漏好于芯型热交换器,且通常不易受水银腐蚀。缠绕盘管热交换器也可例如提供在壳侧上更低的制冷剂压降。
制冷剂压缩机132、134可例如由电动马达驱动或者直接由一个或多个燃气轮机驱动器驱动。可例如从具有发电机的燃气轮机和/或蒸汽轮机得到电力。
制冷剂压缩机132、134的压缩负荷的部分可从膨胀器136、138得到。这通常意味着循序压缩的至少一级,或者在单级压缩的情况下,整个压缩机或并联的压缩机直接地或间接地由膨胀器驱动。例如,直接驱动通常意味着共同轴,而间接驱动涉及使用例如齿轮箱。
在图2至图5和图8至图11中,为了简单起见,对应于图1中示出的实施例或其它相应实施例中的元件或流体流的元件或流体流用相同附图标记来表示。
在另一示范性实施例中且如图2所示,自高压制冷剂压缩机132的排放的流146被分成两个流246、247。流246在热交换器214中冷却以产生流248,流248被分成流168和250。流247绕过热交换器214且在制冷***220中冷却,制冷***220包括至少一级汽化液态制冷剂。汽化可发生于釜中,例如诸如壳管式热交换器,其中沸腾的制冷剂在壳侧上,如图6所示。所得到的流249与流250合并以形成进入膨胀器136的流150。
在又一示范性实施例中且如图3所示,天然气进料流100例如可在制冷***320中预冷,制冷***320包括至少一级汽化液态制冷剂。所得到的流301可在热交换器310中液化以产生基本上液态的流102。自310的气态制冷剂,流356,可与流162合并,类似于图1和图2中流156。
制冷***320和220例如可合并成一个制冷***,其中例如液态制冷剂在系列热交换器的壳侧上沸腾且天然气和蒸汽制冷剂流在管回路中冷却。制冷剂压缩机和冷凝器优选地是两个***共用的,如图6所示。
在又一示范性实施例中且如图4所示,流146可被分成两个流446、447。流446可在热交换器214中冷却以产生流448。流447可绕过热交换器214且可在膨胀器434中膨胀。所得到的流449可与流156和162合并以形成流464,流464可以与图1和图2中的流164相同的方式进入热交换器214。
在另一示范性实施例中且如图5所示,可以循序方式实现膨胀。流548可与流249合并以产生流150,流150可在膨胀器136中膨胀。流160的一部分可在热交换器116中被部分地温热(流570)且可在膨胀器138中膨胀。因此,膨胀器138的入口压力可接近膨胀器136的排放压力。
流166可引入于气态制冷剂压缩机的级之间或可与流158合并以产生流544,流544在单独的压缩机532中压缩以产生流546。在此情况下,流140可在压缩机530中压缩以产生与流546相同压力的流542。配置的选择可取决于压缩机装配和相关联的成本。合并的流542和546可被分成流547和247。流547可在热交换器214中冷却以产生流548,且如图2所示,流247可绕过热交换器214且可在制冷***220中冷却。
过冷产物104可在阀590中被节流到较低压力。所得到的流506可部分为蒸汽。阀590可例如替换为液压涡轮机。流506可在相分离器592中分成液态产物508和闪蒸汽580。流580可在压缩机594中冷压缩以产生流582,流582可在接近流160和174温度的温度。在替代方案中,流580也可在过冷器交换器112中或在单独热交换器中由流102的一部分温热。
流582可在热交换器116中被温热以产生流584,流584可在热交换器214中被进一步温热以产生流586。流586可通常被压缩到更高压力且例如用作燃料用于一个或多个发电机、蒸汽轮机、燃气轮机或电机用于发电。
图5所示的三种修改(循序膨胀、平行气态燃料压缩机和自闪蒸气体回收制冷)也可应用于在其它示范性实施例中所示的配置。
图6示出在图1至图3和图5中所描绘的预冷制冷***的示范性实施例。流630可为气态制冷剂和/或天然气进料,其可在热交换***620(对应于先前图中的***120、220和320)中冷却以得到流632。
气态制冷剂可在制冷剂压缩机600中压缩。所得到的流602可在冷凝器604中完全冷凝。液态的流606可在阀607中节流且在热交换***620的高压蒸发器中部分地汽化以产生两相流608,两相流608然后可在相分离器609中分离。蒸汽部分610可作为高压流引入于600的级之间。液体部分611可在阀612中节流且在热交换***620的中压蒸发器中部分地汽化以产生两相流613,两相流613然后可在相分离器614中分离。蒸汽部分615可作为中压流引入于600的级之间。液体部分616可在阀617中节流,在热交换***620的低压蒸发器中完全汽化以作为低压流617引入于600的级之间。因此,制冷可以在对应于三个蒸发器压力的三个温度水平下供应。也可能具有多于三个或少于三个蒸发器和温度/压力水平。
流602可例如为超临界的,在高于临界压力的压力。它然后可在冷凝器604中冷却而不发生相变以产生稠密流体606。超临界流606可在节流后变成部分液体。
图7a至图7c示出图1所示的示范性实施例的冷却曲线的曲线图。图7a示出合并的热交换器114、116。图7b代表热交换器110。可以看出提取流156显著地改进了交换器效率。图7c示出过冷器交换器112。
在又一示范性实施例中且如图8所示,可使用类似于图1的***,但气态制冷剂可在仅一个压力水平提供制冷。举例而言,膨胀器138的排放压力可与膨胀器136基本上相同。流152可例如被分成流860和854。流854可在对应于液化部段与过冷部段之间过渡的中间位置引入到合并的液化器/过冷器交换器810的壳侧。在那里,它与温热流172混合。流856可在例如对应于预冷部段与液化部段之间过渡的热交换器810内的中间位置提取。因此热交换器810可与用于中间液化部段的大部分制冷剂良好地平衡。
流860可在热交换器116中温热以产生流862。流862可与流856合并以产生流864。流864可在热交换器114中温热以形成流840,与自热交换器810的温热端的流858合并,且引入到制冷剂压缩机830的吸入。压缩机830可例如具有多个级。同样,为了简单起见,未示出中间冷却器和后冷却器。
在另一示范性实施例中且如图9所示,可使用类似于图1的***,但液化器热交换器110和热交换器116和114可合并为热交换器916和914。热交换器914和916也可合并。过冷器交换器112可与热交换器916合并。所有三个交换器914、916和112可例如合并成单个热交换器。进料气流100可在热交换器914中冷却以形成流901。流901可在热交换器916中进一步冷却以形成基本上液化的气流102。
在又一示范性实施例中且如图10所示,可使用类似于图8的***,但可如图4包括第三膨胀器434。额外膨胀器434可替换制冷***120以提供制冷来预冷该气态制冷剂,在此情况下为流447。
在又一示范性实施例中且如图11所示,可使用类似于图8的***,但冷膨胀器138与液化器热交换器810的顶部段一起取消。预冷的气态制冷剂流1148在单个膨胀器1136中膨胀。所得到的膨胀流1154用于在例如液化器热交换器810中使该天然气进料100液化。
此示范性实施例特别适用于产生在温热温度范围的液态天然气。这些温度范围可包括例如-215℉(-137℃)至-80℉(-62℃)。
对本领域技术人员来说,显然的是在图1中的预冷***120可被如图10所示的额外膨胀器替换,或者可如图2中在交换器114外部。如果使用两个膨胀器,一个用于预冷,一个用于液化,那么它们可在两个不同压力排放,自温热(预冷)膨胀器的更高压流引入于低压制冷剂压缩机与高压制冷剂压缩机之间,如在图1中那样。
下面为本申请的一些方面和实施例。
#1. 一种使用闭环制冷***的液化方法,该方法包括以下步骤:
(a)在至少一个压缩机中压缩气态制冷剂流;
(b)在第一热交换器中冷却该压缩气态制冷剂流;
(c)在第一膨胀器中使自第一热交换器的冷却的压缩气态制冷剂流的至少第一部分膨胀以提供第一膨胀气态制冷剂流;以及
(d)冷却且基本上液化进料气流以在第二热交换器中通过与自第一膨胀器的第一膨胀气态制冷剂流的至少第一部分进行间接热交换而形成基本上液化的进料气流,其中离开第一膨胀器的第一膨胀气态制冷剂流基本上为蒸汽。
#2. 根据#1的方法,还包括通过在过冷器交换器中与离开第二膨胀器的第二膨胀气态制冷剂流进行间接热交换而过冷该冷却且基本上液化的进料气流,其中离开第二膨胀器的第二膨胀气态制冷剂流基本上为蒸汽。
#3. 根据#2的方法,其中#1的步骤(a)的压缩气态制冷剂流通过以下步骤发生:
(a)(1)在低压压缩机中压缩该气态制冷剂流;以及
(a)(2)在高压压缩机中进一步压缩该气态制冷剂流。
#4. 根据#3的方法,其中离开第二膨胀器的第二膨胀气态制冷剂流的压力小于离开第一膨胀器的第一膨胀气态制冷剂流的压力。
#5. 根据#1的方法,其中在#1的步骤(d)中自第一膨胀器的第一膨胀气态制冷剂流的第一部分通过在第二热交换器中进行间接热交换而冷却该进料气流,且自第一膨胀器的第一膨胀气态制冷剂流的第二部分在第三热交换器中冷却自该第一热交换器的该冷却的压缩气态制冷剂流的第二部分。
#6. 根据#1的方法,还包括通过与包括至少一级汽化液态制冷剂的补充制冷***进行间接热交换来提供对第一热交换器的补充冷却。
#7. 根据#6的方法,其中汽化液态制冷剂包括CO2、甲烷、丙烷、丁烷、异丁烷、丙烯、乙烷、乙烯、R22、HFC制冷剂(其包括R410A、R134A、R507、R23)或其组合。
#8. 根据#1的方法,其中用于液化的进料气流是天然气流。
#9. 根据#8的方法,其中天然气液化发生于浮式采油贮油和卸油(FPSO)船只上。
#10. 根据#1的方法,其中气态制冷剂流是氮气流。
#11. 根据#3的方法,还包括:在第三热交换器和第一热交换器中温热离开第一膨胀器的第一膨胀气态制冷剂流的第二部分以形成温热的气态制冷剂流,且在#3的步骤(a)(1)与步骤(a)(2)之间合并该温热的气态制冷剂流与离开低压压缩机的压缩气态制冷剂流。
#12. 根据#5的方法,其中离开第一膨胀器的第一膨胀气态制冷剂流的第三部分在第二膨胀器中膨胀之前在第三热交换器中加热。
#13. 根据#2的方法,还包括:从第二热交换器的中间位置提取在第二热交换器中下降的气态制冷剂流的一部分,在第一热交换器中加热该气态制冷剂流的提取部分,以及,在#3的步骤(a)(1)与步骤(a)(2)之间合并该温热的气态制冷剂流与离开低压压缩机的压缩气态制冷剂流。
#14. 根据#1的方法,其中第一热交换器和第三热交换器是单个热交换器。
#15. 根据#1的方法,其中第二热交换器和过冷器交换器是单个热交换器。
#16. 根据#1的方法,其中第一热交换器和第三热交换器是板翅钎焊铝(芯)型热交换器。
#17. 根据#1的方法,其中第二热交换器和过冷器交换器是缠绕盘管式热交换器。
#18. 根据#3的方法,还包括:
使离开该高压压缩机的压缩气态制冷剂流分流;在补充制冷***中冷却离开该高压压缩机的压缩气态制冷剂流的第一部分,该补充制冷***包括至少一级汽化液态制冷剂,以及,在#1的步骤(c)中合并该压缩气态制冷剂流的冷却的第一部分与自第一热交换器的冷却的压缩气态制冷剂流的第一部分以在第一膨胀器中膨胀,以及其中在#1的步骤(b)中离开该高压压缩机的压缩气态制冷剂流的第二部分在第一热交换器中被冷却。
#19. 根据#18的方法,还包括:在#1的步骤(d)之前,在包括至少一级汽化液态制冷剂的补充制冷***中预冷该进料气流。
#20. 根据#19的方法,其中用于预冷该进料气流的补充制冷***和用于冷却离开该高压压缩机的压缩气态制冷剂流的第一部分的补充制冷***是单个补充制冷***。
#21. 根据#3的方法,还包括:使离开该高压压缩机的该压缩气态制冷剂流分流;在第三膨胀器中使离开至少一个压缩机的压缩气态制冷剂流的第一部分膨胀,在第一热交换器中温热该压缩气态制冷剂流的膨胀的第一部分,且然后在#3的步骤(a)(1)与步骤(a)(2)之间合并压缩气态制冷剂流的温热、膨胀的第一部分与离开低压压缩机的压缩气态制冷剂流,以及在#1的步骤(b)中在第一热交换器中冷却离开该高压压缩机的压缩气态制冷剂流的第二部分。
#22. 根据#4的方法,还包括:使离开该高压压缩机的压缩气态制冷剂流分流;在第三膨胀器中使离开该高压压缩机的压缩气态制冷剂流的第一部分膨胀;在第一热交换器中温热该压缩气态制冷剂流的膨胀的第一部分,以及然后在#3的步骤(a)(1)与步骤(a)(2)之间合并压缩气态制冷剂流的温热、膨胀的第一部分与离开该低压压缩机的压缩气态制冷剂流,以及在#1的步骤(b)中在第一热交换器中冷却离开该高压压缩机的压缩气态制冷剂流的第二部分。
#23. 根据#2的方法,还包括:节流该过冷液化进料气体流,在相分离器中分离该节流的过冷液化进料气流为液体产物和闪蒸汽,其中该闪蒸汽可被进一步压缩、温热和用作能量产生的燃料。
#24. 根据#1的方法,还包括:在高压储存罐中储存该冷却且基本上液化的进料气流。
#25. 一种使用闭环制冷***的液化方法,该方法包括以下步骤:
(a)在低压压缩机中压缩气态制冷剂流;
(b)在高压压缩机中进一步压缩该压缩气态制冷剂流;
(c)在第一热交换器中冷却该压缩气态制冷剂流;
(d)在第一膨胀器中使自第一热交换器的冷却的压缩气态制冷剂流的至少第一部分膨胀以提供第一膨胀气态制冷剂流;其中自第一膨胀器的第一膨胀气态制冷剂流提供对第二热交换器和第一热交换器的冷却;
(e)通过在第二热交换器和第一热交换器中与自第一膨胀器的第一膨胀气态制冷剂流进行间接热交换器来冷却并基本上液化进料气流;以及
(f)通过在过冷器交换器中与离开第二膨胀器的第二膨胀气态制冷剂流进行间接热交换而过冷该冷却且基本上液化的进料气流;
其中离开第一膨胀器的第一膨胀气态制冷剂流和离开第二膨胀器的第二膨胀气态制冷剂流基本上为蒸汽,且其中第二膨胀气态制冷剂流的压力低于第一膨胀气态制冷剂流的压力。
#26. 一种用于液化的闭环***,包括:
制冷回路,该制冷回路包括:
第一热交换器;
第二热交换器,其流体地联接到第一热交换器;
第一膨胀器,其流体地联接到第一热交换器且适于自第一热交换器接受制冷剂流;
第二膨胀器,其流体地联接到第二热交换器且适于自第二热交换器接受制冷剂流;以及
第三热交换器,其流体地联接到第一膨胀器且适于接受自第一膨胀器的第一膨胀气态制冷剂流和进料气流,
其中自第一膨胀器的第一膨胀气态制冷剂流和自第二膨胀器的第二膨胀气态制冷剂流基本上为蒸汽流。
#27. 根据#26的***,其还包括过冷器交换器,其流体地联接到第三热交换器和第二热交换器且适于自第三热交换器接受进料气流。
#28. 根据#26的***,还包括:
(a)低压制冷剂压缩机,其流体地联接到第一热交换器;以及
(b)高压制冷剂压缩机,其流体地联接到第一热交换器和低压制冷剂压缩机,适于自第一热交换器和低压制冷剂压缩机接受制冷剂流。
#29. 根据#28的***,其中自第二膨胀器的第二膨胀气态制冷剂流的压力低于自第一膨胀器的第一膨胀气态制冷剂流的压力。
#30. 根据#28的***,还包括补充制冷***,其适于向第一热交换器提供冷却,其中补充制冷***包括至少一级汽化液态制冷剂。
#31. 根据#30的***,其中汽化液态制冷剂包括CO2、甲烷、丙烷、丁烷、异丁烷、丙烯、乙烷、乙烯、R22、HFC制冷剂(其包括R410A、R134A、R507、R23)或其组合。
#32. 根据#26的***,其中进料气流是天然气流。
#33. 根据#32的***,其中该***用于浮式采油贮油和卸油(FPSO)船只上。
#34. 根据#26的***,其中该制冷剂流是氮气流。
#35. 根据#26的***,其中第一热交换器和第二热交换器是单个热交换器。
#36. 根据#27的***,其中第三热交换器和过冷器交换器是单个热交换器。
#37. 根据#26的***,其中第一热交换器和第二热交换器是板翅钎焊铝(芯)型热交换器。
#38. 根据#27的***,其中第三热交换器和过冷器交换器112是缠绕盘管式热交换器。
#39. 根据#28的***,还包括补充制冷***,其流体地联接到高压制冷剂压缩机且适于自高压制冷剂压缩机接受压缩气态制冷剂流。
#40. 根据#26的***,还包括补充制冷***,其流体地联接到第三热交换器且适于接受该进料气流。
#41. 根据#28的***,还包括第三膨胀器,其流体地联接到高压制冷剂压缩机且适于自高压制冷剂压缩机接受压缩气态制冷剂流的一部分。
#42. 根据#27的***,还包括:
阀,其流体地联接到过冷器交换器,适于自过冷器交换器接受进料气流;
相分离器,其流体地联接到所述阀且适于将进料气流分离成液体产物和闪蒸汽。
#43. 根据#26的***,还包括:
第一低压制冷剂压缩机,其流体地联接到第一热交换器;以及,
第二低压制冷剂压缩机,其流体地联接到第三热交换器。
#44. 一种使用具有至少两个膨胀器的闭环蒸汽膨胀循环来液化气态进料的方法,其中,第二膨胀器的排放压力低于第一膨胀器的排放压力,且其中第一膨胀器提供液化气态进料所需制冷的至少一部分。
#45. 根据#44的方法,其中气态进料包括天然气。
#46. 根据#44的方法,其中自第二膨胀器所得的膨胀流被温热到接近环境温度,被压缩,且与自第一膨胀器的温热的所得膨胀流合并。
#47. 根据#46的方法,其中自第一膨胀器和第二膨胀器的合并流被进一步压缩且然后冷却用于进一步膨胀。
#48. 根据#44的方法,其中使自第一膨胀器的所得膨胀流分流使得所得膨胀流的第一部分用于通过间接热交换而冷却该气态进料且所得膨胀流的第二部分用于提供热交换器中的冷却。
实例
参看图3,将在113℉(45℃)和180psia(1.24MPa)下的含大约92%甲烷、1.6%氮气、3.4%乙烷、2%丙烷和1%更重组分的3,160 lbmol/h(1,433kgmol/h)天然气(流100)由制冷***320预冷至大约-31.6℉(-35.3℃),制冷***320包括利用R134A制冷剂(C2H2F4)汽化的3个釜。制冷剂在3级压缩机中压缩,如图6所示。制冷剂压缩机吸入压力大约为0.5巴(50kPa)绝对值。保持吸入压力在真空,允许过冷至更低温度。使用不易燃的制冷剂,保证安全操作。
所得到的流301在液化器热交换器310中冷却至-136℉(-93℃),在此点,流102全都是液体。其然后在过冷器交换器112中过冷到-261℉(-163℃),提供所得到的流104。
自高压制冷剂压缩机132的排放的气态氮气146在104℉(40℃)和1,200 psia(8.27MPa)。流146然后被分成进入制冷***220的21,495 lbmol/h(9,750kgmol/h)g和进入合并热交换器214、216的196,230 lbmol/h(89,008kgmol/h)。
自合并流249和250得到的流150在-49℉(-45℃)和164,634 lbmol/h(74,677kgmol/h)的流率进入膨胀器136。其在-141℉(-96℃)膨胀至大约475psia(3.28MPa)且分成在141,326 lbmol/h(64,104kgmol/h)进入液化器热交换器310的流154和进入合并热交换器214、116的流160。
流356在-54.4℉(-48℃)离开液化器热交换器310。其然后与流162合并,在合并热交换器214、116中温热至97.5℉(36.4℃),且以164,634 lbmol/h(74,677kgmol/h)的流率引入于低压制冷剂压缩机130与高压制冷剂压缩机132之间(流166)。
流170在-136℉(-93℃)且以53,091 lbmol/h(24,082kgmol/h)的流率进入膨胀器138。流170在-165℉(-109℃)膨胀至大约192psia(1.32MPa)(流172)且然后进入过冷器交换器112。
流174在大约-140℉(-96℃)离开过冷器交换器112。流174然后在合并热交换器214、116中温热至97.5℉(36.4℃)且进入低压制冷剂压缩机130的吸入(流140)。
虽然结合各个附图的优选实施例描述了本发明的多方面,应了解在不偏离本发明的情况下可使用其它类似实施例或者可对所描述的实施例做出修改和添加以执行本发明的相同功能。因此,所要求保护的本发明不应限于任何单个实施例,而是应根据所附权利要求书的幅度和范围来解释。附图标记提供于权利要求中只是辅助理解且并不限制权利要求的范围。
Claims (16)
1.一种使用闭环制冷***的利用气体制冷剂的基本上等熵膨胀的液化方法,所述方法包括以下步骤:
(a)在至少一个压缩机(132)中压缩气态制冷剂流(144);
(b)在第一热交换器(114)中冷却压缩气态制冷剂流(144)的至少一部分;
(c)在第一膨胀器(136)中使来自第一热交换器(114)的冷却的压缩气态制冷剂流(148)的至少第一部分(150)膨胀以提供第一膨胀气态制冷剂流(152);
(d)冷却且基本上液化进料气流(100)以在第二热交换器(110)中通过与来自第一膨胀器(136)的第一膨胀气态制冷剂流(152)的至少第一部分(154)进行间接热交换而形成基本上液化的进料气流(102);以及
(e)从第二热交换器(110)的中间位置抽取所述第一膨胀气态制冷剂流(152)的所述至少第一部分(154)的一部分(156),以平衡所述第二热交换器的预冷部段,使得在预冷部段的第一膨胀气态制冷剂流的所述至少第一部分(154)的质量流小于进入所述第二热交换器的第一膨胀气态制冷剂流(152)的所述至少第一部分(154)的质量流,
其中,离开所述第一膨胀器(136)的所述第一膨胀气态制冷剂流(152)基本上为蒸汽。
2.根据权利要求1所述的方法,其特征在于还包括在过冷器交换器(112)中与离开第二膨胀器(138)的第二膨胀气态制冷剂流(172)进行间接热交换而过冷冷却且基本上液化的进料气流(102)。
3.根据权利要求2所述的方法,其特征在于,离开所述第二膨胀器(138)的所述第二膨胀气态制冷剂流(172)基本上为蒸汽。
4.根据权利要求3所述的方法,其特征在于,离开所述过冷器交换器(112)的第二膨胀气态制冷剂流(174)在低压压缩机(130)中压缩;至少与离开所述第二热交换器(110)的所述第一膨胀气态制冷剂流(158)合并;以及,混合流(144)在高压压缩机(132)中被进一步压缩。
5.根据权利要求2所述的方法,其特征在于,所述第二膨胀气态制冷剂流是来自所述第一热交换器(114)的冷却的压缩气态制冷剂流的第二部分(168)得到。
6.根据权利要求5所述的方法,其特征在于,所述冷却的压缩气态制冷剂流(148)的第二部分(168)在第三热交换器(116)中通过与来自所述第一膨胀器(136)的第一膨胀气态制冷剂流(152)的至少第二部分(160)进行间接热交换而进一步冷却且被进给到所述第二膨胀器(138)来提供所述第二膨胀气态制冷剂流(172)。
7.根据权利要求2所述的方法,其特征在于,所述第二膨胀气态制冷剂流是从所述第一膨胀气态制冷剂流(152)的一部分(570)得到。
8.根据权利要求7所述的方法,其特征在于,所述第一膨胀气态制冷剂流(152)的所述一部分(570)在所述膨胀(138)之前通过与从离开所述过冷器交换器(112)的基本上液化的进料气流分离出来的压缩蒸汽进行热交换(116)而被温热。
9.根据权利要求1所述的方法,其特征在于在所述第一热交换器(116)中所述第一膨胀气态制冷剂流(152)的所述至少第一部分(154)的所述一部分(156)从所述第二热交换器(110)的中间位置抽取。
10.根据权利要求1所述的方法,其特征在于,进行液化的进料气流是天然气流。
11.根据权利要求1所述的方法,其特征在于,所述气态制冷剂流是氮气流。
12.根据权利要求1所述的方法,其特征在于还包括:在第三热交换器(116)和所述第一热交换器(114)中温热离开所述第一膨胀器(136)的第一膨胀气态制冷剂流(152)的第二部分(160)以形成温热的气态制冷剂流(166),以及合并所述温热的气态制冷剂流(166)与离开所述第二热交换器(110)的第一膨胀气态制冷剂流(158)。
13.根据权利要求1所述的方法,其特征在于还包括:将离开所述至少一个压缩机(132)的所述压缩气态制冷剂流(146)分成第一部分(247)和第二部分(246);在包括至少一级汽化液态制冷剂的补充制冷***(220)中冷却所述第一部分(247);在权利要求1的步骤(b)中在所述第一热交换器(214)中冷却所述第二部分;以及,在权利要求1的步骤(c)中合并所述冷却的第一部分(249)与所述冷却的第二部分(248)的至少一部分(250)以在所述第一膨胀器(136)中膨胀。
14.根据权利要求1所述的方法,其特征在于还包括将离开所述至少一个压缩机(132)的所述压缩气态制冷剂流(146)分成第一部分(447)和第二部分(446);在第三膨胀器(434)中使所述第一部分(447)膨胀,在所述第一热交换器(214)中温热所得膨胀的第一部分(449),且然后合并所得温热的膨胀的第一部分(166)与离开所述第二热交换器(110)的气态制冷剂流(158),以及,在权利要求1的步骤(b)中在所述第一热交换器(114)中冷却所述第二部分(446)。
15.一种利用权利要求2所述的方法进行液化的闭环***,包括:
制冷回路,所述制冷回路包括:
第一热交换器(114);
第一膨胀器(136),其流体地联接到所述第一热交换器(114)且适于接受来自所述第一热交换器(114)的气态制冷剂流(150);
第二热交换器(110),其流体地联接到所述第一膨胀器(136)且适于(i)接受来自所述第一膨胀器(136)的第一膨胀气态制冷剂流(154)和进料气流(100),以及(ii)从第二热交换器(110)的中间位置抽取所述第一膨胀气态制冷剂流(152)的一部分(156),以平衡所述第二热交换器的预冷部段,使得在预冷部段的所述 第一膨胀气态制冷剂流的质量流小于进入所述第二热交换器的第一膨胀气态制冷剂流(152)的质量流;
第三热交换器(116),其流体地联接到所述第一热交换器(114);
第二膨胀器(138),其流体地联接到所述第三热交换器(116)且适于接受来自所述第三热交换器(116)的气态制冷剂流(170);以及
过冷器交换器(112),其流体地联接到所述第二热交换器(110)和所述第二膨胀器(138)且适于接受来自所述第二热交换器(110)的进料气流(102)。
16.根据权利要求15所述的***,其适用于利用权利要求3至14中任一项所述的方法进行液化的闭环***。
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