CN101711335A - 用于生产lng的方法和*** - Google Patents
用于生产lng的方法和*** Download PDFInfo
- Publication number
- CN101711335A CN101711335A CN200880021514A CN200880021514A CN101711335A CN 101711335 A CN101711335 A CN 101711335A CN 200880021514 A CN200880021514 A CN 200880021514A CN 200880021514 A CN200880021514 A CN 200880021514A CN 101711335 A CN101711335 A CN 101711335A
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- China
- Prior art keywords
- gas
- heat exchanger
- fractionating column
- cooling
- hydrocarbon
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 64
- 238000001816 cooling Methods 0.000 claims abstract description 54
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 43
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 42
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000009833 condensation Methods 0.000 claims abstract description 27
- 230000005494 condensation Effects 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 239000012530 fluid Substances 0.000 claims abstract description 20
- 238000010992 reflux Methods 0.000 claims abstract description 9
- 238000009434 installation Methods 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 156
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 61
- 239000004215 Carbon black (E152) Substances 0.000 claims description 40
- 239000002826 coolant Substances 0.000 claims description 36
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 21
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 20
- 238000009835 boiling Methods 0.000 claims description 15
- 239000012071 phase Substances 0.000 claims description 13
- 239000001273 butane Substances 0.000 claims description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 238000007789 sealing Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- -1 (5) Substances 0.000 claims description 2
- 230000007704 transition Effects 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 claims 2
- 238000005194 fractionation Methods 0.000 abstract description 8
- 239000003949 liquefied natural gas Substances 0.000 description 31
- 238000005516 engineering process Methods 0.000 description 18
- 239000003915 liquefied petroleum gas Substances 0.000 description 18
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 14
- 238000005057 refrigeration Methods 0.000 description 11
- 239000003345 natural gas Substances 0.000 description 9
- 239000001294 propane Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 238000007906 compression Methods 0.000 description 5
- 230000006835 compression Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000002131 composite material Substances 0.000 description 4
- 239000003570 air Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 230000010354 integration Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- BKIMMITUMNQMOS-UHFFFAOYSA-N nonane Chemical compound CCCCCCCCC BKIMMITUMNQMOS-UHFFFAOYSA-N 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- 206010000060 Abdominal distension Diseases 0.000 description 1
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 208000024330 bloating Diseases 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000004108 freeze drying Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- VLKZOEOYAKHREP-UHFFFAOYSA-N hexane Substances CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
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Abstract
描述了一种用于在在岸或者离岸设施上从进入原料气(1)生产LNG的方法,并且其特征在于以下步骤:1)原料气被引导通过分馏塔(150),在此处它被冷却并且被分离成戊烷(C5)和更重的组分的含量降低的塔顶馏分,和富含更重的烃的塔底馏分,2)来自分馏塔的塔顶馏分被进料到热交换器***(110)中并且经受局部冷凝以形成两相流体,并且两相流在适当的分离器(160)中被分离成富含LPG和戊烷(C3-C5)的液体(5),液体(5)作为冷回流而被再循环到分馏塔(150),而包含较小数量的C5烃和比C5更重的烃的气体(6)被移除以在热交换器***(110)中进行进一步的处理从而液化成具有最大的乙烷和LPG含量的LNG,3)用于在热交换器***中液化气体的冷却回路包括带有至少一个气体膨胀步骤的开放或者封闭膨胀工艺。还描述了一种用于进行该方法的***。
Description
技术领域
如能够由独立权利要求1的前序中可见的,本发明涉及一种用于在固定或者浮动离岸设施上以最佳方式生产LNG的方法。
本发明还涉及一种用于实现该方法的***,包括用于进料原料气的分馏塔、用于冷却并且部分地冷凝分馏塔的塔顶气流的热交换器***、用于分离来自热交换器***的两相物流的分离器、用于将来自分离器的液体返回分馏塔并且将该液体作为回流进料到塔上部的装置,和用于将来自分离器的气体返回到热交换器***从而进一步冷却并且液化成LNG的装置。
发明内容
本发明意在使用封闭气体膨胀工艺以液化天然气,并且其中气体首先被进料通过分馏塔,在此处气体被冷却并且被分离成戊烷(C5)和重质组分的含量降低的塔顶馏分,和富含更重的烃的塔底馏分,此外,其中作为***集成部分产生分馏塔回流以当塔顶气体被部分地冷凝时进行液化。通过进行根据本发明的液化,实现了具有最大乙烷和LPG(液态石油气)含量的液化气的生产,同时气体膨胀工艺的效率增加并且最小化了具有高的乙烷、LPG和戊烷含量的不稳定/挥发性液体副产物。
具体地,本发明包括用于液化来自气田或者来自气田/油田的天然气或者其它烃气体的一种方法和一种***,其中将气体液化是适当的,以便于将气体从气体源输送到市场。对于离岸油田/气田而言,这是特别地合适的。
在本文中,天然气指的是烃的混合物,其中主要部分由甲烷组成。通常通过显著地冷却气体从而使它冷凝并且变成液体而将天然气液化。LPG指的是包括丙烷和丁烷(C4、C4组分)的液态石油气。
本发明的目的在于使得气体液化具有能量效率的同时保持工艺简单,从而使得设备能够离岸使用,并且然后尤其是在浮动装置上使用。在液化期间的冷凝物副产物被最小化并且效率得到最大化(最小化对于燃料气体的需求)。
根据本发明的方法其特征在于以下步骤:
1)原料气被引导通过分馏塔(150),在此处它被冷却并且被分离成戊烷(C5)和更重质组分的含量降低的塔顶馏分,和富含更重质烃的塔底馏分,
2)来自分馏塔的塔顶馏分被进料到热交换器***(110)中并且经受部分冷凝以形成两相流体,并且两相流在适当的分离器(160)中被分离成富含LPG和戊烷(C3-C5)的液体(5)和气体(6),液体(5)作为冷回流而被再循环到分馏塔(150),而包含较小量的C5烃和比C5更重的烃的气体(6)被输送以在热交换器***(110)中进行进一步的处理从而液化成具有最大的乙烷和LPG含量的LNG,和
3)用于在热交换器***中液化气体的冷却回路,其包括带有至少一个气体膨胀步骤的开放或者封闭的膨胀工艺。
在从属权利要求2-10中限定了该方法的优选实施方式。
根据本发明的***其特征在于,用于在热交换器***中冷却、冷凝和液化气体的冷却***包括具有至少一个气体膨胀步骤的开放或者封闭气体膨胀工艺。优选设计并且构造该***以分离原料气,使得该***的塔顶气流将富含大部分的丁烷(C4)和具有比丁烷更低的标准沸点的烃,并且分馏塔的塔底产物将富含大多数C6和具有比C6更高的标准沸点的组分。
背景技术
可通过使用气体膨胀工艺进行天然气液化,其中冷却介质通过基于压缩、冷却、膨胀并且随后与待被冷却的流体进行热交换的处理回路。例如,为了液化天然气,可使用气相的压缩冷却介质,通常为氮气或者甲烷,该冷却介质被预冷却并且随后越过膨胀阀或者透平膨胀机膨胀。气体膨胀产生非常冷的气体或者气体和液体的混合物,其然后被用于液化天然气并且预冷却压缩冷却介质气体。气体膨胀工艺是比较简单的并且因此非常好地适用于离岸设施。然而,该工艺具有比更加先进的工艺诸如混合制冷剂循环工艺稍稍更低的效率,并且因此要求大量的压缩设备和大量的能量。
为了生产LNG,通常需要气体具有较高的甲烷含量。然而,大多数进料气体还将包含一些更重的烃例如乙烷、丙烷、丁烷、戊烷等。通常存在对于在液化气中更重的烃含量的一些要求:
每立方米液化气的比能含量通常必须不超过给定的销售规格。
必须保持戊烷(C5)及以上并且还有液化气的芳香化合物的含量低于规定的极限,以避免在冷却工艺中冻干。
限制在液化气中更重质烃含量的最简单的方式是部分地冷凝该气体,并且然后从被进一步冷却从而被液化的气体分离已经冷凝的液体。通常一般在0℃至-60℃之间的温度下,作为冷却工艺的集成部分进行分离。已被分离的冷凝物能够作为冷却工艺的一部分被再次加热以利用制冷潜力。
在大型陆基LNG设施(所谓的“基本负荷”设施)中,在液化之前或者作为液化的一个部分,通常除去大多数的丙烷和更重质的烃,并且在许多情况下还有除去大部分的乙烷。进行这一点是为了满足销售规格并且能够生产和销售有价值的乙烷、LPG和冷凝物/石脑油。无论作为冷却工艺的一个部分还是作为冷却***外侧的分离单元,低温分馏塔通常使用综合工艺。
然而,对于离岸LNG生产而言,并不期望处理除了液态天然气之外的产物。然而当还产生了油或者冷凝物时,能够允许分离冷凝物以实现稳定并且与另一种油和/或冷凝物一起输出。然而,稳定的冷凝物将主要由具有比较低的戊烷含量和更轻的组分的C6+构成。比C6更轻的烃通常不能在不被冷却或者处于低压下被存储或者被安全地输送。一些分离的烃或者冷凝物能够被用作燃料,但是在此之外期望在LNG产物中保留这些组分。由于较小的LNG体积和在以后掺合到大的LNG体积中的可能性,离岸生产具有显著更高的并且优选地最大含量的更重质烃的液态天然气能够是适当的。
本发明提出了对于离岸应用,特别是在浮动单元上的应用的显著优化,其中利用相对简单和耐用的气体膨胀工艺以液化天然气,并且其中在通过最大化乙烷和LPG的含量而最大化液化气量的同时提高了该工艺的能量效率,同时使在液化工艺中作为副产物被分离出去的、比甲烷更重的烃的量最小化。
从而能够使包括根据本发明***的设施简单地适合于并且被安装在例如其中空间经常是一个限制因素的浮板离岸设施上。
对于已知技术和其它公开的参考,以及与本发明的比较:
首先参考EP-1.715.267,该文献描述了一种方法,包括将天然气冷却并且引导通过分馏塔,在此处它被分离成塔顶馏分和塔底馏分。塔底馏分富含更重质的烃并且被从该***输出。塔顶馏分被冷却并且形成在分离器中被分离的两相流体。液相被再循环到分馏塔而气相被进一步进料到热交换器***。利用独立式冷却器进行塔顶馏分的冷却。从而该EP专利描述了一种经典的并且众所周知的蒸馏工艺。
此外,该装置是在所谓的“基本负荷”LNG设施中的标准实践,其中冷却器5和冷却器11这两者(见EP专利中的图)都是通常作为多步丙烷冷却设施实施的该设备的预冷却设施的部件。然而,在EP专利中的设置并未集成分馏塔和作为本发明目标的下游LNG冷凝工艺。集成在这里指的是两个***被紧密地连接到一起,并且作为一个***发挥功能并且材料流和/或能量流在***之间的路径双向流动。
根据EP-1.715.267的制冷操作将塔顶馏分冷却并且产生到分馏塔的所谓的回流,所述回流根据说明并非来自进行进一步的天然气冷却和冷凝的同一冷却回路,而是显然来自外部冷却工艺。
国际专利申请WO-2005/071333描述了一种被用于液化来自用于LNG的存储罐的蒸发气体的、众所周知的双气体膨胀。在实践中,这种蒸发气体仅仅包含甲烷和氮气。
专利公开US2006/0260355A1和US 6,662,589描述了看起来类似于本发明但是实际上显著地不同于本发明的***。在所参考的公开中的***包括用于同时地液化天然气和回收/分离比甲烷更重质的组分,即乙烷和更重质的组分的工艺,其中乙烷、LPG和更重质的组分被分馏成销售产物并且其中液化气具有含量显著降低的乙烷和更重质组分。这是通过将原料气引导到分馏塔而实现的,在分馏塔处,原料气与富含乙烷的回流接触,使得分馏塔将进料分离成塔顶气体馏分和来自塔底的液体流,其中塔顶气体馏分的比甲烷更重质的组分含量显著降低,液体流显著地富含比甲烷更重质的组分。由于来自分馏塔的气体被部分地冷凝,并且另外通过冷却和冷凝被从分馏***再循环的富含乙烷的物流以分馏来自分馏塔的塔底馏分,从而产生富含乙烷的回流。
专利公开US6,401,486、US6,742,358和WO2006/115597A2描述了用于同时地液化天然气和回收/分离比甲烷更重质的组分,即乙烷和更重质组分的***。该工艺自身也显著地不同于本发明并且比本发明更加复杂,其中除了别的以外,原料气被首先在用于液化气体的热交换器(一个或者多个)中被冷却,并且还通过与急骤膨胀的分离液体和与来自塔底部的流体的热交换而被冷却。此外,在它被引导到分馏塔之前,全部或者部分的原料气流通过透平膨胀机或者Joule-Thompson膨胀阀而膨胀。
因此专利公开US 2006/0260355A1、US专利6,662,589、US专利6,401,486还有US专利6,742,358涉及用于在液化气中最小化乙烷、LPG还有更重质的烃的含量的工艺,而本发明包括用于最大化液化气中的甲烷、乙烷和LPG含量的一种***和一种方法。US专利申请2006/0260355A1、US专利6,662,589、US专利6,401,486或者US专利6,742,358均未描述对于能够对气体膨胀工艺用集成分离塔实现能量效率的增加,其中集成分离塔从用于生产LNG的液化热交换器(一个或者多个)接收富含C3-C5的回流。
在DE专利10205366中描述了一种工艺,用于同时地液化天然气和回收/分离比乙烷更重质的组分,并且其中已被分离的LPG和更重质的组分被分馏成销售产物。这是通过首先在用于液化天然气的冷凝设施中部分地冷却原料气,并且然后通过将已被冷却的原料气引导到分馏塔而实现的,在分馏塔处,已被冷却的原料气与富含乙烷的回流形成接触,从而分馏塔将进料物分离成其中比乙烷更重质的组分的含量显著降低的塔顶气体馏分,和显著地富含比乙烷更重质的组分的、来自塔底的液体流。当来自分馏塔的气体被部分地冷凝并且随后与第二分馏塔中的C4/C5流形成接触时,并且在从用于分馏来自第一分馏塔的塔底产物的分馏塔再循环C4/C5馏分时,产生富含乙烷的回流。换言之,DE专利10.205.366包括一种用于最小化液化气的LPG含量还有更重质烃含量的工艺,而本发明包括用于最大化液化气中的LPG含量的一种***和一种方法。公开DE10.205.366并未描述在气体膨胀工艺中,能够利用从用于生产LNG的液化热交换器(一个或者多个)接收富含C3-C5的回流的集成分离塔而实现能量效率的增加。
在US专利4,690,702中描述了一种LNG工艺,其中原料气首先在用于LNG生产的冷却设施中被预冷却,随后被进料到第一分馏塔,在此处它与已被冷却的富含乙烷的回流形成接触,所述回流被从用于分馏来自第一塔的塔底流的第二分馏塔再循环。该公开并不包括其中通过作为LNG工艺的集成部分部分地冷凝来自分馏塔的塔顶气体产物而实现用于分馏塔的富含C3-C5的回流的***。
US专利7,010,937示出一种用于同时地液化天然气和回收/分离比甲烷更重质的组分的***。根据该公开,原料气被预冷却并且部分地冷凝,从而能够在分离器中分离液体流并且其中该液体流在第一分馏塔中被分馏以产生被冷却以产生用于第二分馏塔的回流的塔顶气体。来自分离器的气流沿着气体膨胀器膨胀并且被进料到第二分馏塔。因此该US专利与如在随后的权利要求中限定的本发明几乎无共同点。
附图说明
现在将参考附图更加详细地描述本发明,其中:
图1示出具有主要构件和主要功能性的主要实施方式。
图2以可替代的实施方式示出本发明。
图3利用可替代的实施方式示出本发明,该实施方式包括进一步稳定被分离出去的更重质的烃(冷凝物)。
图4详细地示出通过使用双气体膨胀工艺进行的本发明。
图5示出通过使用带有气体膨胀圈和液体膨胀圈的混合冷却回路进行的本发明。
图6示出用于传统氮气膨胀循环的热温度曲线和冷温度曲线(复合曲线)的一个实例。
图7示出用于通过使用本发明获得的氮气膨胀循环的热温度曲线和冷温度曲线(复合曲线)的一个实例。
图8示出图6和7所示曲线的比较。
具体实施方式
参考图1,用于优化的气体液化的***至少包括以下主要构件:
-应该被冷却和液化的进入气流1,
-分馏塔150,在其中进入气体被冷却并且被分离成戊烷和更重质组分的含量降低的塔顶馏分2,
-富含更重质的烃组分的塔底馏分3,
-热交换器***110,其中进入气体被冷却并且被部分地冷凝以分离更重质的烃并且被进一步冷却和液化,
-包括已被冷却的液化气体的产物流11,
-主要包括戊烷和更重质的烃的产物流3,和
-用于冷却和液化气体的冷却***,包括气相冷却介质流20、至少一个循环压缩机100、至少一个后冷却器130、至少一个气体膨胀器120。
进入的和清洁的原料气1(例如富甲烷烃气体)首先被进料到分馏塔150,在此处当与更冷的回流流体接触时气体被冷却。在冷却和与更冷的流体逆流接触期间,原料气被分离成其中具有高于戊烷(C5)的分子量的烃的含量降低的塔顶馏分2,和富含C6和具有比C6更高的分子量的烃的塔底馏分3。来自分馏塔的塔顶馏分2然后被引导到热交换器***110,在此处气体被冷却并且被部分地冷凝,从而能够在适当的分离器160中分离所产生的两相流4。在分离器160中被分离的、富含LPG和戊烷(C3-C5)的流体5作为冷回流被再循环到分馏塔150。因为利用冷却而通过冷凝产生该流体,所以回流流体5将具有比原料气1更低的温度。来自分离器160的气体6现在已经进一步降低了它的C5烃和高于C5的烃的含量。该气体然后被引导回热交换器***110以进一步冷却、冷凝和低温冷却。液化气11被可替代地引导通过控制操作压力和通过该***的流量的控制阀140。
在一个优选实施方式中,利用适当的外部冷却介质或者单独的、适当的制冷***/预冷却***预冷却原料气流1,所述外部冷却介质例如可用的空气、水、海水。对于后者的外部冷却方法,经常使用利用丙烷、氨或者其它适当的制冷剂的单独的封闭式机械制冷***。
在一个优选实施方式中,分馏塔150和分离器160在这样的压力和温度下操作,所述的压力和温度使得整个***(分馏塔150和回流分离器160)产生在-120℃和60℃之间的标准沸点区域(NBP)中的组***解/分离点。这例如能够对应于用于分离的轻关键组分是具有在-12℃和0℃之间的标准沸点的丁烷(C4)并且重关键组分是具有在50℃和70℃之间的沸点的C6组分。该***的塔顶气流6然后将富含大部分的丁烷(C4)和具有比丁烷更低的标准沸点的烃。来自分馏塔的塔底产物3将富含大部分C6和具有高于C6的标准沸点的组分,而戊烷(C5,NBP=28-36℃)是分布在该***的气体产物和来自分馏塔的塔底产物中的过渡组分。
在热交换器***110中冷却和冷凝原料气是由封闭的或者开放的气体膨胀工艺提供的。当在的较高压力、优选在3和10MPa之间的压力下,包括气体或者气体混合物(例如纯净氮、甲烷、烃混合物,或者氮气和烃的混合物)的冷却剂21被进料到热交换器***110并且被冷却到在0℃和-120℃之间的温度,但是使得冷却介质流主要是处于支配性压力和温度31下的气体时,冷却工艺开始。被预冷却的冷却介质31然后被引导到气体膨胀器121中,在此处气体膨胀至入口压力的5%-40%之间,但是优选地在入口压力的10%和30%之间的较低压力,并且使得冷却剂主要处于气相中。气体膨胀器通常是膨胀涡轮,还被称为透平膨胀机,但是能够使用用于气体的其它类型的膨胀设备例如阀。被预冷却的冷却剂流在高的等熵效率下在气体膨胀器121中膨胀,使得温度显著地下降。在本发明的特定实施方式中,在这个膨胀中一些液体能够被分离出去,但是对于该工艺而言不要求这一点。冷的冷却剂流32然后被引导回热交换器110,在此处它被用于冷却和可替代地冷凝应该被冷却、冷凝和低温冷却的其它进入的热冷却介质流和气体。
在冷的冷却介质流32在热交换器***110中被加热之后,冷却介质将作为气流51存在,气流51在闭环实施方式中被以适当的方式再次压缩以进行再循环,并且利用外部冷却介质例如空气、水、海水或者适当制冷单元而被冷却。
可替代地,在开放实施方式中的冷却***将使用由从适当的来源例如从将被处理和冷却的原料气接收的、处于较高压力的气体或者气体混合物构成的冷却介质21。此外,开放实施方式包括低压冷却介质流51被用于其它目的或者以适当的方式被再次压缩,从而与将被处理和冷却的原料气混合。
在一个优选实施方式中,返回的冷却介质流51被从热交换器110引导到被膨胀涡轮121驱动的独立的压缩机101。以此方式,膨胀功得以利用,并且该工艺的能量效率得以提高。在压缩机101之后,在冷却介质流在循环压缩机100中被进一步压缩之前,冷却剂在热交换器131中被进一步冷却。循环压缩机100能够是一个或者多个单元,可替代地每单元一级或者多级。循环压缩机还能够在压缩机级之间配备有中间冷却132。然后在适当的外部冷却介质例如空气、水、海水或者适当的独立的制冷循环的帮助下,在后冷却器130中通过热交换而冷却被压缩的冷却介质20,从而在闭环中被再次用作经过压缩的冷却介质21。
在一个优选实施方式中,热交换器***110是在同一单元中包括很多不同的“热”和“冷”流的一个热交换器(所谓的多流热交换器)。
图2示出一个可替代实施方式,其中几个多流热交换器被以如此方式连接到一起,使得在冷和热流之间的必要的热传递能够得以实现。图2示出包括串联的几个热交换器的热交换器***110。然而,本发明并不涉及热交换器的具体类型或者交换器的数目,而是能够在能够处理所需数目的热和冷工艺流的、几种不同类型的热交换器***中进行。
图3示出一个可替代实施方式,其中分馏塔150配备有再沸器135以进一步促进分离(在轻和重组分之间更加剧烈地***),并且还用于减小塔中的塔底馏分的挥发性。这能够被用于直接地生产在环境温度和大气压力下稳定的冷凝物。
图4详细地示出在其中使用双气体膨胀工艺的更加先进的实施方式中应用的本发明。在该实施方式中,经过压缩的冷却介质流21首先被冷却至中间温度。在这个温度下,冷却剂流被划分成两个部分,其中一个部分31被从热交换器取出并且在气体膨胀器121中膨胀成低压气流32。另一部分41被进一步预冷却从而在气体膨胀器122中膨胀至基本等于流32中的压力的压力。膨胀的冷的冷却剂流32、42被返回到热交换器***110上的不同进口位置,并且在这个交换器中被混合成一股物流。经过加热的冷却剂51然后被返回以再次压缩。在图3中***的一个可替代实施方式中,在双气体膨胀回路中的经过压缩的冷却剂流20能够在热交换器110之前被***成两股物流,从而在热交换器110中在分离的流动流道中被冷却至不同的温度。
对于加热已被返回的冷的冷却剂流32、42而言同样如此。该实施方式否则为按照图3的。
图5详细地示出通过使用混合冷却回路进行的本发明,所述混合冷却回路其中使用一种纯气相和纯液相的冷却介质。在该实施方式中封闭冷却回路提供了在热交换器***110中对于原料气的冷却。所述冷却循环利用甲烷或者甲烷和氮气的混合物开始,其中甲烷构成至少50%的体积,被压缩并且被后冷却成经过压缩的冷却介质流21,并且其中这个冷却介质流被预冷却,并且冷却介质流的至少一部分31以气相使用,这是因为它越过气体膨胀器121膨胀并且因为冷却剂流的至少一部分41被冷凝成液体并且越过阀或者液体膨胀器141而膨胀。
需要强调的是,本发明的实施方式不仅仅限于上述冷却工艺,而是能够与用于液化天然气或者其它烃气体的任何气体膨胀冷却工艺一起使用,其中冷却主要是通过使用一个或者多个膨胀气流而得以实现的。
通过根据本发明进行天然气的液化产生了液化气产物,该产物具有最大的甲烷、乙烷和LPG含量,但是同时并不包含大于允许水平的戊烷和具有高于50-60℃的标准沸点的、更重质的烃。同时,最小化或者消除了在用于LNG生产的离岸设施上将难以处理的、具有大量的乙烷、丙烷和丁烷的挥发性烃副产物。同时与不带用于接收来自冷却工艺的冷的和富LPG的回流的分馏塔而构造的类似的冷却循环相比,还将以更低的能量消耗产生更多的液态天然气。
与不带集成的分离塔的类似的冷却工艺相比,使用本发明降低了用于天然气液化的气体膨胀工艺的能量消耗的原因在于几个方面:
必须被分离出去以防止在液化期间结冰的更重质的烃将被冷凝并且在比传统方法显著更高的温度下被分离,因为大量的冷凝发生在分馏塔中。这降低了在冷却工艺中的能量损失,因为冷却负荷被移动到更高的温度范围。
冷却工艺的热交换器***100接收作为物流2(分馏塔中的塔顶气流)将被液化的气体,该气流相对于实际的原料气流1具有降低的温度。气体膨胀工艺的特征在于热和冷冷却曲线由被用作冷却介质的大量气体决定。这些气流形成线性冷却曲线。到热交换器中的降低的进料温度在热冷却曲线(被冷却的物流总和)上产生“断点”,从而在热和冷冷却曲线之间的距离能够实现总体降低。这提供了更好的温度适应,降低了能量损失并且因此降低了用于驱动冷却工艺的能量消耗。
初步分析和比较表明,与传统方法相比,对于根据本发明进行的气体膨胀循环,所产生的每kg液态天然气所需的压缩机功能够降低5-15%。
图6表示对于根据本发明实现的、带有作为冷却***的双氮气膨胀工艺的热交换器***110的热和冷冷却曲线(热和冷复合曲线,即分别是被冷却的全部热流的总和和将被加热的全部冷流的总和)。图7表示对于具有相同的原料但是不带分馏塔的、以传统方式进行的相应冷却工艺,相应的热和冷冷却曲线。曲线似乎看起来是类似的,但是考虑到在同一曲线中示出一段和两个***的图8,能够清楚地看到“断点”和更好的适应。
实施例
在下面的实施例示出将被液化的、按照体积具有90.4%的甲烷的天然气,其中本发明被用于最大化液化气的量并且同时最小化具有高含量的乙烷、丙烷和丁烷的、不稳定的烃液体副产物。物流数据参考图1、2、3、4或者5。
物流编号 | 1 | 2 | 3 | 4 | 5 | 6 | 11 |
气体馏分 | 1.00 | 1.00 | 0.00 | 0.95 | 0.00 | 1.00 | 0.00 |
温度(℃) | 40.0 | 19.2 | 35.9 | -20.0 | -20.0 | -20.0 | -155.0 |
压力(kPaabs) | 2740 | 2738 | 2745 | 2725 | 2730 | 2723 | 2655 |
摩尔流量(kmol/h) | 4232 | 4422 | 44 | 4422 | 235 | 4185 | 4185 |
质量流量(kg/h) | 78980 | 87539 | 3410 | 87539 | 11969 | 75541 | 75541 |
摩尔馏分(%) | |||||||
氮气 | 0.51% | 0.49% | 0.02% | 0.49% | 0.03% | 0.52% | 0.52% |
甲烷 | 90.4% | 87.4% | 11.8% | 87.4% | 19.5% | 91.3% | 91.3% |
乙烷 | 4.38% | 4.53% | 2.58% | 4.53% | 6.84% | 4.40% | 4.40% |
丙烷 | 2.29% | 2.95% | 4.17% | 2.95% | 15.04% | 2.27% | 2.27% |
异丁烷 | 0.68% | 1.25% | 2.80% | 1.25% | 11.92% | 0.65% | 0.65% |
正丁烷 | 0.66% | 1.52% | 3.79% | 1.52% | 17.30% | 0.62% | 0.62% |
异戊烷 | 0.17% | 0.70% | 2.52% | 0.70% | 10.57% | 0.14% | 0.14% |
正戊烷 | 0.17% | 0.79% | 3.61% | 0.79% | 12.49% | 0.12% | 0.12% |
正己烷 | 0.44% | 0.32% | 43.62% | 0.32% | 6.25% | 0.02% | 0.02% |
正庚烷 | 0.19% | 0.00% | 18.29% | 0.00% | 0.02% | 0.00% | 0.00% |
正辛烷 | 0.055% | 0.000% | 5.187% | 0.000% | 0.000% | 0.000% | 0.000% |
正壬烷 | 0.014% | 0.000% | 1.339% | 0.000% | 0.000% | 0.000% | 0.000% |
正癸烷+ | 0.002% | 0.000% | 0.214% | 0.000% | 0.000% | 0.000% | 0.000% |
Claims (12)
1.一种用于在在岸或者离岸设施上由进入原料气(1)生产LNG的方法,其特征在于以下步骤:
1)将所述原料气引导通过分馏塔(150),在此处它被冷却并且被分离成戊烷(C5)和更重质的组分的含量降低的塔顶馏分,和富含更重质的烃的塔底馏分,
2)将所述分馏塔的塔顶馏分引导到热交换器***(110)中并且经受部分冷凝以形成两相流体,并且将该两相流体在适当的分离器(160)中分离成富含LPG和戊烷(C3-C5)的流体(5),流体(5)作为冷回流被再循环到分馏塔(150),而包含较小量的C5烃和比C5更重质的烃的气体(6)被除去以在热交换器***(110)中进行进一步的处理,从而液化成具有最大的乙烷和LPG含量的LNG,
3)用于在所述热交换器***中液化气体的冷却回路包括带有至少一个气体膨胀步骤的开放或者封闭膨胀工艺。
2.根据权利要求1的方法,其特征在于,分馏塔(150)和分离器(160)在这样的压力和温度下操作,所述的压力和温度使得整个***(分馏塔150和回流分离器160)产生在-12℃和60℃之间的标准沸点范围(NBP)内的组分***/分离点。
3.根据权利要求1-2的方法,其特征在于,用于分离的轻关键组分是具有在-12℃和0℃之间的标准沸点的丁烷(C4),并且重关键组分是具有在50℃和70℃之间的沸点的C6组分,由此该***的塔顶气流(6)将包含含量显著降低的正丁烷和具有比正丁烷更低的标准沸点的烃,并且该***的废气流(3)包括大部分的C6和具有高于C6的标准沸点的组分。
4.根据权利要求1-3的方法,其特征在于,如此操作分馏塔(150)和分离器(160),使得戊烷(C5,NBP=28-36℃)是在所述***的塔顶气流(6)和所述***的废气流(3)这两者中分布的过渡组分。
5.根据前述权利要求之一的方法,其特征在于,通过分馏塔(150)降低了原料气的温度,从而当所述气体被进料到热交换器***(110)中时它的温度低于在所述热交换器***的热端处的冷却介质气流的温度(热窄点温度)。
6.根据前述权利要求之一的方法,其特征在于,再沸器(135)被连接到分馏塔(150)以降低所述塔底产物的蒸汽压力。
7.根据前述权利要求之一的方法,其特征在于,用于液化(LNG生产)的热交换器包括一个或者多个多流热交换器。
8.根据前述权利要求之一的方法,其特征在于,该方法是利用带有至少一个氮气膨胀器的封闭气体膨胀工艺进行的。
9.根据前述权利要求之一的方法,其特征在于,该方法是利用具有作为冷却剂的甲烷/氮气的封闭混合冷却工艺进行的,其中使用气相和液相二者的冷却剂,并且其中冷却循环具有至少一个气体膨胀器和至少一个用于膨胀液体冷却剂的装置。
10.根据前述权利要求之一的方法,其特征在于,该方法是利用带有至少一个气体膨胀器的开放气体膨胀工艺进行的,其中处于较高压力的适当的气体被用作冷却气体,并且其中处于较低压力的膨胀气体不被再次压缩以用于再循环而是被用于另一目的。
11.一种用于实现根据权利要求1-10的方法的***,包括用于接收原料气的分馏塔(150)、用于冷却并且部分冷凝所述分馏塔的塔顶气流的热交换器***(110)、用于分离来自所述热交换器***的两相物流的分离器(160)、用于将来自所述分离器的流体再循环到所述分馏塔并且将这个流体作为回流引入所述塔的上部的装置,和用于将来自所述分离器的气体引回所述热交换器***以进一步冷却并且液化成LNG的装置,其特征在于,被用于在热交换器***中冷却、冷凝和液化所述气体的冷却***包括带有至少一个气体膨胀步骤的开放或者封闭气体膨胀工艺。
12.根据权利要求11的***,其特征在于,设计和构造该***以分离所述原料气,从而使得该***的塔顶气流(6)将富含大部分丁烷(C4)和具有比丁烷更低的标准沸点的烃,并且在所述分馏塔中的塔底产物将富含大部分C6和具有高于C6的标准沸点的组分。
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CN105716371A (zh) * | 2016-04-12 | 2016-06-29 | 成都赛普瑞兴科技有限公司 | 一种混合冷剂制冷天然气轻烃回收的方法及装置 |
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US11402152B2 (en) | 2017-07-07 | 2022-08-02 | Tor Christensen | Large scale coastal liquefaction |
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Also Published As
Publication number | Publication date |
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EP2165140A1 (en) | 2010-03-24 |
NO20073245L (no) | 2008-12-23 |
AU2008283102B2 (en) | 2013-02-07 |
MY163902A (en) | 2017-11-15 |
KR101568763B1 (ko) | 2015-11-12 |
CN101711335B (zh) | 2014-10-15 |
NO329177B1 (no) | 2010-09-06 |
US20100132405A1 (en) | 2010-06-03 |
BRPI0813297A2 (pt) | 2014-12-30 |
CA2692213A1 (en) | 2009-02-05 |
AU2008283102A1 (en) | 2009-02-05 |
KR20100039353A (ko) | 2010-04-15 |
WO2009017414A1 (en) | 2009-02-05 |
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