CN107166871A - 采用双级混合制冷剂循环的液化天然气蒸发气再液化*** - Google Patents
采用双级混合制冷剂循环的液化天然气蒸发气再液化*** Download PDFInfo
- Publication number
- CN107166871A CN107166871A CN201710404719.5A CN201710404719A CN107166871A CN 107166871 A CN107166871 A CN 107166871A CN 201710404719 A CN201710404719 A CN 201710404719A CN 107166871 A CN107166871 A CN 107166871A
- Authority
- CN
- China
- Prior art keywords
- entrance
- heat exchanger
- outlet
- bog
- cooler
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003507 refrigerant Substances 0.000 title claims abstract description 102
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 239000007789 gas Substances 0.000 title claims abstract description 21
- 239000003345 natural gas Substances 0.000 title claims abstract description 19
- 238000009834 vaporization Methods 0.000 title claims abstract description 12
- 230000008016 vaporization Effects 0.000 title claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 230000004087 circulation Effects 0.000 claims abstract description 14
- 238000005057 refrigeration Methods 0.000 claims abstract description 12
- 230000006835 compression Effects 0.000 claims abstract description 9
- 238000007906 compression Methods 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims description 30
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 12
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 8
- 239000001294 propane Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000001282 iso-butane Substances 0.000 claims description 4
- 235000013847 iso-butane Nutrition 0.000 claims description 4
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 2
- 230000002427 irreversible effect Effects 0.000 abstract description 2
- 230000002265 prevention Effects 0.000 abstract description 2
- 239000003949 liquefied natural gas Substances 0.000 description 16
- 238000001816 cooling Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 7
- 238000005096 rolling process Methods 0.000 description 5
- 238000002309 gasification Methods 0.000 description 3
- 230000009102 absorption Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Classifications
-
- 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
- F25J1/0211—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 using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0219—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 using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
-
- 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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
-
- 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
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
-
- 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
- F25J1/003—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
- 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"
- F25J1/004—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" by flash gas recovery
-
- 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
- F25J1/003—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
- F25J1/0047—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
- F25J1/0052—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 vaporising a liquid refrigerant stream
-
- 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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
采用双级混合制冷剂循环的液化天然气蒸发气再液化***,包括高温区混合制冷剂(MR2)循环、低温区混合制冷剂(MR1)循环和BOG喷射制冷液化循环,采用带喷射器的双级混合制冷剂***,两级混合制冷剂制冷循环通过合理的组分配比、压力和温度设定,以较小的耗功量使压缩后的BOG再液化;同时引入喷射器,利用高压液态天然气引射储罐中的BOG,减小了节流过程中的不可逆损失,节省了耗功,进一步降低了***的单位液化耗功量,节能效果显著。
Description
技术领域
本发明属于液化天然气技术领域,具体涉及采用双级混合制冷剂循环的液化天然气蒸发气再液化***。
背景技术
液化天然气(liquefied natural gas,LNG)是一种常压贮存于-162℃的低温液体燃料,其主要成分是甲烷,体积为气态时的1/625,便于长途运输和贮存。由于LNG的常压贮存温度为-162℃,在其输运及贮存过程中,难免有热量从环境漏入,使部分LNG汽化产生蒸发气(boil-off gas,BOG),并使容器压力升高,当压力高于安全压力时,BOG将被排放至大气中,不仅造成温室气体排放,经济损失也十分可观,因此如何合理回收BOG成为LNG贮存环节亟待解决的热点问题。
目前,BOG的处理工艺多为再冷凝工艺,该工艺结合LNG外输,利用高压过冷的LNG使压缩后的BOG冷凝,之后再泵送至汽化器,回收了LNG的冷量,大大节省了BOG加压的耗功。然而,当LNG储罐外输负荷较小或长时间无LNG外输时,不断产生的BOG将被火炬排空,以维持***运行的安全压力。因此,该工艺无法从根本上有效的解决BOG的处理问题,需考虑采用独立的低温制冷***将BOG再液化后送回储罐中。
发明内容
为了克服上述现有技术的缺点,本发明的目的在于提供了采用双级混合制冷剂循环的液化天然气蒸发气再液化***,使其单位液体产品能耗更低,可以有效降低BOG再液化的耗功。
为了实现上述目的,本发明采取如下技术方案:
采用双级混合制冷剂循环的液化天然气蒸发气再液化***,包括换热器HX1,换热器HX1的出口c与第一级高温制冷剂压缩机C6入口连接,第一级高温制冷剂压缩机C6出口和第五冷却器5入口连接,第五冷却器5出口和第二级高温制冷剂压缩机C7入口连接,第二级高温制冷剂压缩机C7出口与第六冷却器6入口连接,第六冷却器6出口与换热器HX1的入口e连接,和入口e连通的换热器HX1的出口f与高温制冷剂节流阀V2入口相连,高温制冷剂节流阀V2出口与换热器HX1的入口d连接,入口d和出口c连通,构成高温区混合制冷剂(MR2)循环;
换热器HX1的出口a与第一级低温制冷剂压缩机C4入口连接,第一级低温制冷剂压缩机C4出口与第三冷却器3入口连接,第三冷却器3出口与第二级低温制冷剂压缩机C5入口连接,第二级低温制冷剂压缩机C5出口和第四冷却器4入口连接,第四冷却器4出口与换热器HX1的入口g连接,和入口g连通的换热器HX1的出口h与换热器HX2的入口m连接,和入口m连通的换热器HX2的出口n与低温制冷剂节流阀V1入口连接,低温制冷剂节流阀V1出口与换热器HX2的入口l连接,和入口l连通的换热器HX2的出口k与换热器HX1的入口b连接,入口b和换热器HX1的出口a连通,构成低温区混合制冷剂(MR1)循环;
换热器HX1的出口j与换热器HX2的入口o连接,和入口o连通的换热器HX2的出口p与过冷器HX3的入口s连接,和入口s连通的过冷器HX3的出口t和喷射器E0主流体入口u连接,喷射器E0的被引射流体入口v与储罐BOG出口相连,喷射器E0的出口w与气液分离器S0入口x连接,气液分离器S0的液相出口y与BOG节流阀V0入口相连,BOG节流阀V0出口与LNG储罐连接;气液分离器的气相出口z和过冷器HX3的入口r连接,和入口r连通的过冷器HX3的出口q与第一级BOG压缩机C1入口连接,第一级BOG压缩机C1出口与第二级BOG压缩机C2的入口相连,第二级BOG压缩机C2的出口和第一冷却器1的入口连接,第一冷却器1的出口与第三级BOG压缩机C3入口连接,第三级BOG压缩机C3出口与第二冷却器2入口连接,第二冷却器2出口与换热器HX1的入口i相连,入口i和换热器HX1的出口j连通,至此构成BOG喷射制冷液化循环。
所述的高温区混合制冷剂包含异丁烷、丙烷和乙烷,所述低温区混合制冷剂包含丙烷、乙烯和甲烷。
所述的高温区混合制冷剂(MR2)循环进入换热器HX1前实现全部冷凝,所述的低温区混合制冷剂(MR1)循环进入换热器HX2前实现部分冷凝。
所述的BOG喷射制冷液化循环在进入过冷器HX3前实现全部液化。
本发明的有益效果为:
本发明用于对储罐中的BOG再液化回收处理,采用一种带喷射器的双级混合制冷剂***,其优点在于两级混合制冷剂制冷循环通过合理的组分配比、压力和温度设定,以较小的耗功量使压缩后的BOG再液化。同时,该***引入喷射器,利用高压液态天然气引射储罐中的BOG,减小了节流过程中的不可逆损失,节省了耗功,进一步降低了***的单位液化耗功量,节能效果显著。
附图说明
图1为本发明实施例的结构示意图。
具体实施方式
下面结合附图和实施例对本发明做进一步详细描述:
参照图1,采用双级混合制冷剂循环的液化天然气蒸发气再液化***,包括换热器HX1,换热器HX1的出口c与第一级高温制冷剂压缩机C6入口连接,第一级高温制冷剂压缩机C6出口和第五冷却器5入口连接,第五冷却器5出口和第二级高温制冷剂压缩机C7入口连接,第二级高温制冷剂压缩机C7出口与第六冷却器6入口连接,第六冷却器6出口与换热器HX1的入口e连接,和入口e连通的换热器HX1的出口f与高温制冷剂节流阀V2入口相连,高温制冷剂节流阀V2出口与换热器HX1的入口d连接,入口d和出口c连通,构成高温区混合制冷剂(MR2)循环。
第一级高温制冷剂压缩机C6吸入从换热器HX1排出的低压制冷剂蒸气MR2-1后,压缩后进入第五冷却器5中间冷却后进入第二级高温制冷剂压缩机C7压缩至最高压力,随后高压的制冷剂MR2-4进入第六冷却器6中被冷却至环境温度,之后高压的制冷剂MR2-5流入换热器HX1被过冷至状态MR2-6后在高温制冷剂节流阀V2中节流,并返流回换热器HX1为其提供冷量;在换热器HX1中吸收高压天然气、高压低温混合制冷剂MR1及自身冷却过程释放的热量,并被气化复温后,低压的制冷剂MR2-1被第一级高温制冷剂压缩机C6吸入,进入下一次MR2循环。
换热器HX1的出口a与第一级低温制冷剂压缩机C4入口连接,第一级低温制冷剂压缩机C4出口与第三冷却器3入口连接,第三冷却器3出口与第二级低温制冷剂压缩机C5入口连接,第二级低温制冷剂压缩机C5出口和第四冷却器4入口连接,第四冷却器4出口与换热器HX1的入口g连接,和入口g连通的换热器HX1的出口h与换热器HX2的入口m连接,和入口m连通的换热器HX2的出口n与低温制冷剂节流阀V1入口连接,低温制冷剂节流阀V1出口与换热器HX2的入口l连接,和入口l连通的换热器HX2的出口k与换热器HX1的入口b连接,入口b和换热器HX1的出口a连通,构成低温区混合制冷剂(MR1)循环。
第一级低温制冷剂压缩机C4吸入由换热器HX1排出的低压制冷剂MR1-1,压缩后MR1-2进入第三冷却器3中冷却后进入第二级低温制冷剂压缩机C5被压缩至最高压力,随后高压的制冷剂MR1-4进入第四冷却器4中被冷却至环境温度,之后进入换热器HX1中被返流的高温区混合制冷剂MR2预冷,再进入换热器HX2中被过冷后在低温制冷剂节流阀V1中节流,并返流依次通过换热器HX2、换热器HX1为其提供冷量;制冷剂在换热器HX1中完全气化复温为MR1-1后被第一级低温制冷剂压缩机C4吸入,进入下一次MR1循环。
换热器HX1的出口j与换热器HX2的入口o连接,和入口o连通的换热器HX2的出口p与过冷器HX3的入口s连接,和入口s连通的过冷器HX3的出口t和喷射器E0主流体入口u连接,喷射器E0的被引射流体入口v与储罐BOG出口相连,喷射器E0的出口w与气液分离器S0入口x连接,气液分离器S0的液相出口y与BOG节流阀V0入口相连,BOG节流阀V0出口与LNG储罐连接;气液分离器的气相出口z和过冷器HX3的入口r连接,和入口r连通的过冷器HX3的出口q与第一级BOG压缩机C1入口连接,第一级BOG压缩机C1出口与第二级BOG压缩机C2的入口相连,第二级BOG压缩机C2的出口和第一冷却器1的入口连接,第一冷却器1的出口与第三级BOG压缩机C3入口连接,第三级BOG压缩机C3出口与第二冷却器2入口连接,第二冷却器2出口与换热器HX1的入口i相连,入口i和换热器HX1的出口j连通,至此构成BOG喷射制冷液化循环。
从过冷器HX3排出的低压BOG M0经多级压缩中间冷却后,成为常温高压天然气M5,随后依次进入换热器HX1、换热器HX2分别被前述MR2循环和MR1循环提供的冷量冷却并液化,之后进入过冷器HX3被来自气液分离器S0的返流低温BOG M10过冷后,进入喷射器E0作为主流体M8引射来自储罐中的BOG,在喷射器E0出口产生低温气液两相混合物M9,之后进入气液分离器S0中两相分离,气体部分M10返流进入过冷器HX3过冷前述的高压天然气M7,液体部分在BOG节流阀V0节流调压后返回储罐中。
所述的换热器HX1和换热器HX2为多股流换热器,在换热器HX1中,高温区混合制冷剂、低温区混合制冷剂和BOG的同时进行换热;在换热器HX2中,低温区混合制冷剂和BOG的同时进行换热。
由于液化天然气蒸发气体组分以甲烷(CH4)为主,所述的高温区混合制冷剂(MR2)由异丁烷、丙烷和乙烷组成,所述的低温区混合制冷剂(MR1)由丙烷、乙烯和甲烷组成;所述的冷却器均采用水冷冷却器,各物流流出冷却器的温度均为30℃。所述换热器HX1和HX2为多股流换热器,其热侧和冷侧通道入口端及出口端的各物流温度应保持一致。
高温区混合制冷剂(MR2)循环采用两级压缩中间冷却,所述高温区混合制冷剂(MR2)在第六冷却器6中实现全部冷凝,经换热器HX1过冷后流入高温制冷剂节流阀V2,节流至0.105MPa,获得温度低于-50℃的两相流体,返流回换热器HX1气化吸热。所述高温区混合制冷剂(MR2)在换热器HX1中完全气化并过热至高于20℃后,被第一级高温制冷剂压缩机C6吸入。
低温区混合制冷剂(MR1)循环类似于高温区混合制冷剂循环,同样采用两级压缩中间冷却,所述高压的低温区混合制冷剂(MR1)在第四冷却器4中被冷却至30℃,经换热器HX1预冷至-50℃左右,实现部分冷凝后进入换热器HX2;所述低温区混合制冷剂(MR1)在换热器HX2中实现全部冷凝并过冷后进入低温制冷剂节流阀V1,节流至0.105MPa,获得温度低于-120℃的两相流体,依次返流回换热器HX2和HX1气化吸热,为其提供冷量;所述低温区混合制冷剂(MR1)经换热器HX1过热至高于20℃后,被第一级低温制冷剂压缩机C4吸入。
BOG再液化循环采用三级压缩中间冷却,将BOG压缩至高压,在冷却器被冷却至30℃,经换热器HX1预冷至-50℃左右,在换热器HX2中实现完全冷凝并过冷至-120℃,经过冷器HX3进一步被过冷至-130℃以下;所述低温高压的液相BOG进入喷射器,作为主流体引射来自储罐中的低压BOG;在喷射器出口获得的低温低压的两相流体进入气液分离器,其中气相部分经过冷器HX3回收冷量后被第一级BOG压缩机C1吸入,液相部分经BOG节流阀V0节流至0.107MPa后返回储罐中。
采用流程模拟计算的方法说明图1所示的实施方案,结果列于表1中。假定天然气物流由纯甲烷组成,天然气循环的最高压力为4MPa(即第三级BOG压缩机C3的出口压力),来自LNG储罐的天然气蒸发气(BOG)压力为0.107MP、温度为-125℃;返回储罐的天然气压力为0.107MPa、温度为-160.9℃。高温区混合制冷剂(MR2)由异丁烷、丙烷和乙烷组成,其摩尔分数分别为0.4697、0.3310和0.1993,而低温区混合制冷剂(MR1)由丙烷、乙烯和甲烷组成,其摩尔分数分别为0.1862、0.6906和0.1232。本领域技术人员可确定该闭式混合制冷剂循环中制冷剂的组成,使对于各种不同的原料气组成、压力和温度条件下,液化天然气蒸发气再液化流程所需耗功量最小。计算结果表明,所需高温区和低温区混合制冷剂循环的压力最高不超过2MPa。
该实施例是对本发明所作的进一步详细说明,不能认定本发明的具体实施方式仅限于此,对于本发明所属技术领域的普通技术人员来说,在不脱离本发明构思的前提下,还可以做出若干简单的推演或替换,都应当视为属于本发明由所提交的权利要求书确定专利保护范围。
表1实施例主要参数
Claims (4)
1.采用双级混合制冷剂循环的液化天然气蒸发气再液化***,包括换热器HX1,其特征在于:换热器HX1的出口c与第一级高温制冷剂压缩机C6入口连接,第一级高温制冷剂压缩机C6出口和第五冷却器5入口连接,第五冷却器5出口和第二级高温制冷剂压缩机C7入口连接,第二级高温制冷剂压缩机C7出口与第六冷却器6入口连接,第六冷却器6出口与换热器HX1的入口e连接,和入口e连通的换热器HX1的出口f与高温制冷剂节流阀V2入口相连,高温制冷剂节流阀V2出口与换热器HX1的入口d连接,入口d和出口c连通,构成高温区混合制冷剂(MR2)循环;
换热器HX1的出口a与第一级低温制冷剂压缩机C4入口连接,第一级低温制冷剂压缩机C4出口与第三冷却器3入口连接,第三冷却器3出口与第二级低温制冷剂压缩机C5入口连接,第二级低温制冷剂压缩机C5出口和第四冷却器4入口连接,第四冷却器4出口与换热器HX1的入口g连接,和入口g连通的换热器HX1的出口h与换热器HX2的入口m连接,和入口m连通的换热器HX2的出口n与低温制冷剂节流阀V1入口连接,低温制冷剂节流阀V1出口与换热器HX2的入口l连接,和入口l连通的换热器HX2的出口k与换热器HX1的入口b连接,入口b和换热器HX1的出口a连通,构成低温区混合制冷剂(MR1)循环;
换热器HX1的出口j与换热器HX2的入口o连接,和入口o连通的换热器HX2的出口p与过冷器HX3的入口s连接,和入口s连通的过冷器HX3的出口t和喷射器E0主流体入口u连接,喷射器E0的被引射流体入口v与储罐BOG出口相连,喷射器E0的出口w与气液分离器S0入口x连接,气液分离器S0的液相出口y与BOG节流阀V0入口相连,BOG节流阀V0出口与LNG储罐连接;气液分离器的气相出口z和过冷器HX3的入口r连接,和入口r连通的过冷器HX3的出口q与第一级BOG压缩机C1入口连接,第一级BOG压缩机C1出口与第二级BOG压缩机C2的入口相连,第二BOG压缩机C2的出口和第一冷却器1的入口连接,第一冷却器1的出口与第三级BOG压缩机C3入口连接,第三级BOG压缩机C3出口与第二冷却器2入口连接,第二冷却器2出口与换热器HX1的入口i相连,入口i和换热器HX1的出口j连通,至此构成BOG喷射制冷液化循环。
2.根据权利要求1所述的采用双级混合制冷剂循环的液化天然气蒸发气再液化***,其特征在于:所述的高温区混合制冷剂包含异丁烷、丙烷和乙烷,所述低温区混合制冷剂包含丙烷、乙烯和甲烷。
3.根据权利要求1所述的采用双级混合制冷剂循环的液化天然气蒸发气再液化***,其特征在于:所述的高温区混合制冷剂(MR2)循环进入换热器HX1前实现全部冷凝,所述的低温区混合制冷剂(MR1)循环进入换热器HX2前实现部分冷凝。
4.根据权利要求1所述的采用双级混合制冷剂循环的液化天然气蒸发气再液化***,其特征在于:所述的BOG喷射制冷液化循环在进入过冷器HX3前实现全部液化。
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201710404719.5A CN107166871A (zh) | 2017-06-01 | 2017-06-01 | 采用双级混合制冷剂循环的液化天然气蒸发气再液化*** |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201710404719.5A CN107166871A (zh) | 2017-06-01 | 2017-06-01 | 采用双级混合制冷剂循环的液化天然气蒸发气再液化*** |
Publications (1)
Publication Number | Publication Date |
---|---|
CN107166871A true CN107166871A (zh) | 2017-09-15 |
Family
ID=59821543
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN201710404719.5A Pending CN107166871A (zh) | 2017-06-01 | 2017-06-01 | 采用双级混合制冷剂循环的液化天然气蒸发气再液化*** |
Country Status (1)
Country | Link |
---|---|
CN (1) | CN107166871A (zh) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107726045A (zh) * | 2017-09-29 | 2018-02-23 | 深圳市燃气集团股份有限公司 | 一种液化天然气的bog液化再回收*** |
CN108489133A (zh) * | 2018-03-13 | 2018-09-04 | 中国科学院理化技术研究所 | 多级压缩混合工质制冷/液化*** |
CN109404716A (zh) * | 2018-11-27 | 2019-03-01 | 郑州大学 | 一种加气站bog再液化同轴联动介式*** |
CN111854322A (zh) * | 2020-07-14 | 2020-10-30 | 西安交通大学 | 一种基于丙烷、异丁烷混合预冷的天然气液化*** |
CN113274951A (zh) * | 2021-05-21 | 2021-08-20 | 济南隆凯能源科技有限公司 | 一种双蒸气引射循环烃部分氧化***及方法 |
CN114017988A (zh) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | 一种基于混合工质制冷技术的lng船用bog再液化循环*** |
CN114017989A (zh) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | Lng-bog再液化***及其适用的混合冷剂 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2001132896A (ja) * | 1999-11-08 | 2001-05-18 | Osaka Gas Co Ltd | ボイルオフガスの再液化方法 |
CN1330760A (zh) * | 1998-12-18 | 2002-01-09 | 埃克森美孚上游研究公司 | 用于液化天然气的双多组分制冷循环 |
EP1062466B1 (en) * | 1997-12-16 | 2012-07-25 | Battelle Energy Alliance, LLC | Apparatus and process for the refrigeration, liquefaction and separation of gases with varying levels of purity |
CN106066116A (zh) * | 2015-04-24 | 2016-11-02 | 气体产品与化学公司 | 用于使天然气液化的集成甲烷制冷*** |
CN106766671A (zh) * | 2017-01-15 | 2017-05-31 | 郑州大学 | 一种新型撬装式加气站bog液化*** |
-
2017
- 2017-06-01 CN CN201710404719.5A patent/CN107166871A/zh active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1062466B1 (en) * | 1997-12-16 | 2012-07-25 | Battelle Energy Alliance, LLC | Apparatus and process for the refrigeration, liquefaction and separation of gases with varying levels of purity |
CN1330760A (zh) * | 1998-12-18 | 2002-01-09 | 埃克森美孚上游研究公司 | 用于液化天然气的双多组分制冷循环 |
JP2001132896A (ja) * | 1999-11-08 | 2001-05-18 | Osaka Gas Co Ltd | ボイルオフガスの再液化方法 |
CN106066116A (zh) * | 2015-04-24 | 2016-11-02 | 气体产品与化学公司 | 用于使天然气液化的集成甲烷制冷*** |
CN106766671A (zh) * | 2017-01-15 | 2017-05-31 | 郑州大学 | 一种新型撬装式加气站bog液化*** |
Non-Patent Citations (1)
Title |
---|
HONGBO TAN等: "Enhancement of energy performance in a boil-off gas re-liquefaction system of LNG carriers using ejectors", 《ENERGY CONVERSION AND MANAGEMENT》 * |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107726045A (zh) * | 2017-09-29 | 2018-02-23 | 深圳市燃气集团股份有限公司 | 一种液化天然气的bog液化再回收*** |
CN108489133A (zh) * | 2018-03-13 | 2018-09-04 | 中国科学院理化技术研究所 | 多级压缩混合工质制冷/液化*** |
CN108489133B (zh) * | 2018-03-13 | 2023-10-20 | 中国科学院理化技术研究所 | 多级压缩混合工质制冷/液化*** |
CN109404716A (zh) * | 2018-11-27 | 2019-03-01 | 郑州大学 | 一种加气站bog再液化同轴联动介式*** |
CN109404716B (zh) * | 2018-11-27 | 2024-02-13 | 郑州大学 | 一种加气站bog再液化同轴联动介式*** |
CN111854322A (zh) * | 2020-07-14 | 2020-10-30 | 西安交通大学 | 一种基于丙烷、异丁烷混合预冷的天然气液化*** |
CN113274951A (zh) * | 2021-05-21 | 2021-08-20 | 济南隆凯能源科技有限公司 | 一种双蒸气引射循环烃部分氧化***及方法 |
CN113274951B (zh) * | 2021-05-21 | 2022-12-20 | 济南隆凯能源科技有限公司 | 一种双蒸气引射循环烃部分氧化***及方法 |
CN114017988A (zh) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | 一种基于混合工质制冷技术的lng船用bog再液化循环*** |
CN114017989A (zh) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | Lng-bog再液化***及其适用的混合冷剂 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN107166871A (zh) | 采用双级混合制冷剂循环的液化天然气蒸发气再液化*** | |
CN104321581B (zh) | Lng蒸发气体再冷凝配置和方法 | |
CN105486034B (zh) | 一种天然气液化与轻烃分离一体化集成工艺***及工艺 | |
KR101099079B1 (ko) | 저온 액화 냉동 방법 및 장치 | |
US9506690B2 (en) | Process for the production of a subcooled liquefied natural gas stream from a natural gas feed stream, and associated installation | |
CN103857955B (zh) | 储槽的压力上升抑制装置、抑制***及抑制方法、液化气体运输船及储藏设备 | |
CN105004100B (zh) | 单制冷剂回路、多吸气压力的蒸气压缩制冷/热泵*** | |
CN110345690B (zh) | 用于双温电冰箱的双喷射器增效制冷循环***及工作方法 | |
KR101876974B1 (ko) | 선박용 증발가스 재액화 장치 및 방법 | |
EP1913117A1 (en) | Lng bog reliquefaction apparatus | |
CN103109144A (zh) | 制冷剂成分控制 | |
KR20070011075A (ko) | 작동유체의 유량조절수단을 이용하여 부하 변동 조절이가능한 천연가스 액화장치 | |
CN108106048A (zh) | 一种喷射器膨胀自复叠制冷循环***及工作过程 | |
CN106969557A (zh) | 一种带经济器的双温co2跨临界增压制冷*** | |
CN101410678A (zh) | 冷冻装置 | |
CN206235085U (zh) | 液氧、液氮互换生产装置 | |
KR20070024071A (ko) | Bog 재액화 장치 | |
CN106595220B (zh) | 一种用于液化天然气的液化***及其液化方法 | |
AU2022308303A1 (en) | Facility and method for the liquefaction of hydrogen | |
US20230251030A1 (en) | Facility and method for hydrogen refrigeration | |
CN103148625B (zh) | 一种具有储冷器的混合工质节流循环低温制冷机 | |
CN109612145A (zh) | 一种多喷射器组强化的co2双温制冷*** | |
CN205593289U (zh) | 液化天然气的装置 | |
CN106766671A (zh) | 一种新型撬装式加气站bog液化*** | |
CN106288657A (zh) | 液氧、液氮互换生产装置及生产工艺 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PB01 | Publication | ||
PB01 | Publication | ||
SE01 | Entry into force of request for substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
WD01 | Invention patent application deemed withdrawn after publication | ||
WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170915 |