CN109631492A - 一种采用混合冷剂级联的天然气液化装置及方法 - Google Patents
一种采用混合冷剂级联的天然气液化装置及方法 Download PDFInfo
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 118
- 239000003345 natural gas Substances 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 194
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 30
- 239000003507 refrigerant Substances 0.000 claims abstract description 24
- 239000007791 liquid phase Substances 0.000 claims abstract description 17
- 230000001105 regulatory effect Effects 0.000 claims abstract description 13
- 239000012071 phase Substances 0.000 claims abstract description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 10
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 9
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 48
- 238000010992 reflux Methods 0.000 claims description 36
- CHHHXKFHOYLYRE-STWYSWDKSA-M potassium sorbate Chemical compound [K+].C\C=C\C=C\C([O-])=O CHHHXKFHOYLYRE-STWYSWDKSA-M 0.000 claims description 24
- OGMADIBCHLQMIP-UHFFFAOYSA-N 2-aminoethanethiol;hydron;chloride Chemical compound Cl.NCCS OGMADIBCHLQMIP-UHFFFAOYSA-N 0.000 claims description 22
- QUWSDLYBOVGOCW-UHFFFAOYSA-N Tetrasul Chemical compound C1=CC(Cl)=CC=C1SC1=CC(Cl)=C(Cl)C=C1Cl QUWSDLYBOVGOCW-UHFFFAOYSA-N 0.000 claims description 21
- TYNLGDBUJLVSMA-UHFFFAOYSA-N 4,5-diacetyloxy-9,10-dioxo-2-anthracenecarboxylic acid Chemical compound O=C1C2=CC(C(O)=O)=CC(OC(C)=O)=C2C(=O)C2=C1C=CC=C2OC(=O)C TYNLGDBUJLVSMA-UHFFFAOYSA-N 0.000 claims description 19
- SUBDBMMJDZJVOS-UHFFFAOYSA-N 5-methoxy-2-{[(4-methoxy-3,5-dimethylpyridin-2-yl)methyl]sulfinyl}-1H-benzimidazole Chemical compound N=1C2=CC(OC)=CC=C2NC=1S(=O)CC1=NC=C(C)C(OC)=C1C SUBDBMMJDZJVOS-UHFFFAOYSA-N 0.000 claims description 19
- PPASLZSBLFJQEF-RXSVEWSESA-M sodium-L-ascorbate Chemical compound [Na+].OC[C@H](O)[C@H]1OC(=O)C(O)=C1[O-] PPASLZSBLFJQEF-RXSVEWSESA-M 0.000 claims description 19
- VSJKWCGYPAHWDS-FQEVSTJZSA-N camptothecin Chemical compound C1=CC=C2C=C(CN3C4=CC5=C(C3=O)COC(=O)[C@]5(O)CC)C4=NC2=C1 VSJKWCGYPAHWDS-FQEVSTJZSA-N 0.000 claims description 17
- 239000002826 coolant Substances 0.000 claims description 14
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- 239000004302 potassium sorbate Substances 0.000 claims description 12
- 239000004283 Sodium sorbate Substances 0.000 claims description 11
- 239000000661 sodium alginate Substances 0.000 claims description 10
- PPASLZSBLFJQEF-RKJRWTFHSA-M sodium ascorbate Substances [Na+].OC[C@@H](O)[C@H]1OC(=O)C(O)=C1[O-] PPASLZSBLFJQEF-RKJRWTFHSA-M 0.000 claims description 10
- 230000006835 compression Effects 0.000 claims description 9
- 238000007906 compression Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 9
- 239000007792 gaseous phase Substances 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims 1
- 239000002737 fuel gas Substances 0.000 abstract description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 5
- 239000001294 propane Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
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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
- F25J1/0002—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
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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
- F25J1/003—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
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- 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
- F25J1/0212—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 as a single flow MCR cycle
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- 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
- F25J1/0217—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 as at least a three level refrigeration cascade with at least one MCR cycle
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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
- 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
- F25J1/0262—Details of the cold heat exchange system
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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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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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
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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Abstract
一种采用混合冷剂级联的天然气液化装置及方法,首先将通过预处理单元的高压天然气进入预冷板翅式换热器,与预冷混合制冷剂循环换热,冷却至‑50℃~‑55℃;再进入重烃分离罐,脱出天然气中的重烃组分;再进入液化板翅式换热器,与液化混合制冷剂循环换热,冷却至‑118℃~‑122℃;再进入深冷板翅式换热器,与深冷混合制冷剂循环换热,冷却至‑155℃~‑160℃;再经节流阀节流降压至150kPa,进入分离器,气相作为厂区的燃料气,液相为液化天然气(LNG)产品进入LNG储罐;本发明将预处理后的天然气和3种混合制冷剂在冷箱中的板翅式换热器中换热,既可以实现对环境低温的充分利用,也能最大限度提高驱动机功率的利用率。
Description
技术领域
本发明涉及天然气液化技术领域,特别涉及一种采用混合冷剂级联的天然气液化装置及方法,主要针对基本负荷型LNG工厂的天然气液化。
背景技术
国内对于天然气的需求迅速增长,但国内天然气用户与资源分布极不均匀。中国的天然气资源大多分布在中西部地区和海上,很多天然气用户市场的资源供应严重缺乏,因此要实现天然气资源的合理利用,首要任务是从根本上解决运输与利用之间的矛盾。液化天然气技术的出现使天然气的远距离运输得以实现。
在整个LNG产业链中,天然气液化是其中资金、技术最为密集的关键环节,其费用大约为整个LNG产业链的30~40%。天然气液化技术是一项科技含量很高的系统工程,其工业链由净化、液化、储存、运输、接收一系列环节组成。
近年来,大型天然气液化工艺技术呈现多样化。混合制冷剂液化天然气流程因其低能耗的优点,已被广泛采用于大型LNG液化工厂。主要应用于工业的混合冷剂流程有:单混合冷剂工艺(SMR)、丙烷预冷混合冷剂工艺(C3MR)、AP-X膨胀工艺等。SMR流程无预冷循环,采用一种混合制冷剂,效率较低,流程能耗很高。C3MR,AP-X流程预冷段都采用丙烷冷剂制冷,预冷的最低温度受丙烷沸点的限制。
发明内容
为了克服上述现有技术的缺陷,本发明的目的在于提供一种采用混合冷剂级联的天然气液化装置及方法,将通过预处理单元的高压天然气(NG)和三种混合制冷剂在冷箱换热器中换热,将天然气液化为液化天然气,既可以实现对环境低温的充分利用,也能最大限度提高驱动机功率的利用率。
为了达到上述目的,本发明的技术方案为:
一种采用混合冷剂级联的天然气液化装置,包括天然气液化回路装置、预冷混合冷剂循环装置、液化混合冷剂循环装置和深冷混合冷剂循环装置;
所述的天然气液化回路装置包括预冷板翅式换热器ET-101(17)、分离器V-101(9)、液化板翅式换热器ET-201(16)、深冷板翅式换热器ET-301(15)、节流阀S-101(11)、分离器V-102(12)和LNG储罐V-103(13);预冷板翅式换热器ET-101(17)的天然气入口与预处理后的天然气管线连通,预冷板翅式换热器ET-101(17)的天然气出口与分离器V-101(9)的入口连通,分离器V-101(9)的气相出口与液化板翅式换热器ET-201(16)的天然气入口连通,液化板翅式换热器ET-201(16)的天然气出口与深冷板翅式换热器ET-301(15)的天然气入口连通,深冷板翅式换热器ET-301(15)的天然气出口经节流阀S-101(11)与分离器V-102(12)的入口连通,分离器V-102(12)的液相出口与LNG储罐V-103(13)的入口连通;
所述的预冷混合冷剂循环装置包括节流阀S-201(8)、压缩机C-201(7)、空冷器AC-201(6)、水冷器E-201(5)、分离器V-201(4)、压缩机C-202(3)、离心泵P-201(24)、空冷器AC-202(2)和水冷器E-202(1);水冷器E-202(1)的出口与预冷板翅式换热器ET-101(17)的预冷混合冷剂入口连通,预冷板翅式换热器ET-101(17)的预冷混合冷剂出口经节流阀S-201(8)与预冷板翅式换热器ET-101(17)的预冷混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的预冷混合冷剂反流出口与压缩机C-201(7)的入口连通,压缩机C-201(7)的出口与空冷器AC-201(6)的入口连通,空冷器AC-201(6)的出口与水冷器E-201(5)的入口连通,水冷器E-201(5)的出口与分离器V-201(4)的入口连通,分离器V-201(4)的气相出口与压缩机C-202(3)的入口连通,分离器V-201(4)的液相出口与离心泵P-201(24)的入口连通,压缩机C-202(3)的出口和离心泵P-201(24)的出口与空冷器AC-202(2)的入口连通,空冷器AC-202(2)的出口与水冷器E-202(1)的入口连通;
所述的液化混合冷剂循环装置包括液化板翅式换热器ET-201(16)、节流阀S-301(10)、压缩机C-301(21)、空冷器AC-301(22)和水冷器E-301(23);水冷器E-301(23)的出口与预冷板翅式换热器ET-101(17)的液化混合冷剂入口连通,预冷板翅式换热器ET-101(17)的液化混合冷剂出口与液化板翅式换热器ET-201(16)的液化混合冷剂入口连通,液化板翅式换热器ET-201(16)的液化混合冷剂出口经节流阀S-301(10)与液化板翅式换热器ET-201(16)的液化混合冷剂反流入口连通,液化板翅式换热器ET-201(16)的液化混合冷剂反流出口与预冷板翅式换热器ET-101(17)的液化混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的液化混合冷剂反流出口与压缩机C-301(21)的入口连通,压缩机C-301(21)的出口与空冷器AC-301(22)的入口连通,空冷器AC-301(22)的出口与水冷器E-301(23)的入口连通;
所述的深冷混合冷剂循环装置包括液化板翅式换热器ET-201(16)、深冷板翅式换热器ET-301(15)、节流阀S-401(14)、压缩机C-401(18)、空冷器AC-401(19)和水冷器E-401(20);水冷器E-401(20)的出口与预冷板翅式换热器ET-101(17)的深冷混合冷剂入口连通,预冷板翅式换热器ET-101(17)的深冷混合冷剂出口与液化板翅式换热器ET-201(16)的深冷混合冷剂入口连通,液化板翅式换热器ET-201(16)的深冷混合冷剂出口与深冷板翅式换热器ET-301(15)的深冷混合冷剂入口连通,深冷板翅式换热器ET-301(15)的深冷混合冷剂出口与节流阀S-401(14)的入口连通,节流阀S-401(14)的出口与深冷板翅式换热器ET-301(15)的深冷混合冷剂反流入口连通,深冷板翅式换热器ET-301(15)的深冷混合冷剂反流出口与液化板翅式换热器ET-201(16)的深冷混合冷剂反流入口连通,液化板翅式换热器ET-201(16)的深冷混合冷剂反流出口与预冷板翅式换热器ET-101(17)的深冷混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的深冷混合冷剂反流出口与压缩机C-401(18)的入口连通,压缩机C-401(18)的出口与空冷器AC-401(19)的入口连通,空冷器AC-401(19)的出口与水冷器E-401(20)的入口连通。
基于上述装置的一种采用混合冷剂级联的天然气液化方法,包括如下步骤:
(1)天然气液化回路:
首先将通过预处理单元的高压天然气NG进入预冷板翅式换热器ET-101(17),冷却至-50℃~-55℃;
再进入重烃分离罐V-101(9),脱出天然气中的重烃组分;
再进入液化板翅式换热器ET-201(16),冷却至-118℃~-122℃;
再进入深冷板翅式换热器ET-301(15),冷却至-155℃~-160℃;
再经节流阀S-101(11)节流降压至150KPa,进入分离器V-102(12),气相作为厂区的燃料气,液相为液化天然气LNG产品进入LNG储罐V-103(13)。
(2)预冷混合冷剂循环:
1.8MPa~2.2MPa高压的预冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再经过节流阀S-201(8)节流降压至0.17MPa~0.24MPa,重新进入预冷板翅式换热器ET-101(17)汽化为冷却天然气、预冷剂高压部分、液化冷剂和深冷剂提供冷量;
然后预冷剂经低压压缩机C-201(7)压缩后依次进入级间空冷器AC-201(6)和水冷器E-201(5)冷却,此时会凝析出部分液相,需要经分离器V-201(4)分离,气相部分进入高压压缩机C-202(3)加压,液相部分进入液体离心泵P-201(24)加压,再将气、液两相混合后,最后再依次进入级间空冷器AC-202(2)和水冷器E-202(1)冷却,恢复为至初始状态的预冷剂,完成预冷循环。
(3)液化混合制冷剂循环:
2.1MPa~2.5MPa的高压的液化混合制冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再进入液化板翅式换热器ET-201(16)冷却至-118℃~-122℃;
通过节流阀S-301(10)节流降压至0.22MPa~0.27MPa,重新依次进入液化板翅式换热器ET-201(16)和预冷板翅式换热器ET-101(17)汽化为液化天然气、液化冷剂高压部分和深冷剂提供冷量;
然后液化冷剂经压缩机C-301(21)压缩后依次进入空冷器AC-301(22)和水冷器E-301(23)冷却,恢复为至初始状态的液化冷剂,完成液化循环。
(4)深冷混合制冷剂循环:
2.8MPa~3.2MPa高压的深冷混合制冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再进入液化板翅式换热器ET-201(16)冷却至-118℃~-122℃;
再进入深冷板翅式换热器ET-301(15)冷却至-155℃~-160℃;
通过节流阀S-401(14)节流降压0.35MPa~0.42MPa,重新依次进入深冷板翅式换热器ET-301(15)、液化板翅式换热器ET-201(16)和预冷板翅式换热器ET-101(17)汽化为深冷天然气、深冷剂高压部分和液化冷剂提供冷量;
然后深冷剂经压缩机C-401(18)压缩后依次进入空冷器AC-401(19)和水冷器E-401(20)冷却,恢复为至初始状态的深冷剂,完成深冷循环。
本发明混合冷剂级联流程克服了丙烷预冷固有的局限性,具有更多可调参数来优化处于设计点外的流程性能。根据不同原料气条件和季节气温变化,可将液化循环的部分制冷量转移到预冷部分,从而更好地平衡制冷负荷,既可以实现对环境低温的充分利用,也能最大限度提高驱动机功率的利用率,并使压缩机在宽温度范围内保持较高效率点运行。提高了流程对原料天然气和外界条件的适应性;液化过程中天然气与混合冷剂在换热器内的传热温差均匀,效率高,流程能耗更低。
附图说明
图1是本发明的结构示意图。
具体实施方式
下面结合附图对本发明做详细叙述。
参照图1,一种采用混合冷剂级联的天然气液化装置,包括天然气液化回路装置、预冷混合冷剂循环装置、液化混合冷剂循环装置和深冷混合冷剂循环装置;
所述的天然气液化回路装置包括预冷板翅式换热器ET-101(17)、分离器V-101(9)、液化板翅式换热器ET-201(16)、深冷板翅式换热器ET-301(15)、节流阀S-101(11)、分离器V-102(12)和LNG储罐V-103(13);预冷板翅式换热器ET-101(17)的天然气入口与预处理后的天然气管线连通,预冷板翅式换热器ET-101(17)的天然气出口与分离器V-101(9)的入口连通,分离器V-101(9)的气相出口与液化板翅式换热器ET-201(16)的天然气入口连通,液化板翅式换热器ET-201(16)的天然气出口与深冷板翅式换热器ET-301(15)的天然气入口连通,深冷板翅式换热器ET-301(15)的天然气出口经节流阀S-101(11)与分离器V-102(12)的入口连通,分离器V-102(12)的液相出口与LNG储罐V-103(13)的入口连通;
所述的预冷混合冷剂循环装置包括节流阀S-201(8)、压缩机C-201(7)、空冷器AC-201(6)、水冷器E-201(5)、分离器V-201(4)、压缩机C-202(3)、离心泵P-201(24)、空冷器AC-202(2)和水冷器E-202(1);水冷器E-202(1)的出口与预冷板翅式换热器ET-101(17)的预冷混合冷剂入口连通,预冷板翅式换热器ET-101(17)的预冷混合冷剂出口经节流阀S-201(8)与预冷板翅式换热器ET-101(17)的预冷混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的预冷混合冷剂反流出口与压缩机C-201(7)的入口连通,压缩机C-201(7)的出口与空冷器AC-201(6)的入口连通,空冷器AC-201(6)的出口与水冷器E-201(5)的入口连通,水冷器E-201(5)的出口与分离器V-201(4)的入口连通,分离器V-201(4)的气相出口与压缩机C-202(3)的入口连通,分离器V-201(4)的液相出口与离心泵P-201(24)的入口连通,压缩机C-202(3)的出口和离心泵P-201(24)的出口与空冷器AC-202(2)的入口连通,空冷器AC-202(2)的出口与水冷器E-202(1)的入口连通;
所述的液化混合冷剂循环装置包括液化板翅式换热器ET-201(16)、节流阀S-301(10)、压缩机C-301(21)、空冷器AC-301(22)和水冷器E-301(23);水冷器E-301(23)的出口与预冷板翅式换热器ET-101(17)的液化混合冷剂入口连通,预冷板翅式换热器ET-101(17)的液化混合冷剂出口与液化板翅式换热器ET-201(16)的液化混合冷剂入口连通,液化板翅式换热器ET-201(16)的液化混合冷剂出口经节流阀S-301(10)与液化板翅式换热器ET-201(16)的液化混合冷剂反流入口连通,液化板翅式换热器ET-201(16)的液化混合冷剂反流出口与预冷板翅式换热器ET-101(17)的液化混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的液化混合冷剂反流出口与压缩机C-301(21)的入口连通,压缩机C-301(21)的出口与空冷器AC-301(22)的入口连通,空冷器AC-301(22)的出口与水冷器E-301(23)的入口连通;
所述的深冷混合冷剂循环装置包括液化板翅式换热器ET-201(16)、深冷板翅式换热器ET-301(15)、节流阀S-401(14)、压缩机C-401(18)、空冷器AC-401(19)和水冷器E-401(20);水冷器E-401(20)的出口与预冷板翅式换热器ET-101(17)的深冷混合冷剂入口连通,预冷板翅式换热器ET-101(17)的深冷混合冷剂出口与液化板翅式换热器ET-201(16)的深冷混合冷剂入口连通,液化板翅式换热器ET-201(16)的深冷混合冷剂出口与深冷板翅式换热器ET-301(15)的深冷混合冷剂入口连通,深冷板翅式换热器ET-301(15)的深冷混合冷剂出口与节流阀S-401(14)的入口连通,节流阀S-401(14)的出口与深冷板翅式换热器ET-301(15)的深冷混合冷剂反流入口连通,深冷板翅式换热器ET-301(15)的深冷混合冷剂反流出口与液化板翅式换热器ET-201(16)的深冷混合冷剂反流入口连通,液化板翅式换热器ET-201(16)的深冷混合冷剂反流出口与预冷板翅式换热器ET-101(17)的深冷混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的深冷混合冷剂反流出口与压缩机C-401(18)的入口连通,压缩机C-401(18)的出口与空冷器AC-401(19)的入口连通,空冷器AC-401(19)的出口与水冷器E-401(20)的入口连通。
基于上述装置的一种采用混合冷剂级联的天然气液化方法,包括如下步骤:
(1)天然气液化回路:
首先将通过预处理单元的高压天然气NG进入预冷板翅式换热器ET-101(17),冷却至-50℃~-55℃;
再进入重烃分离罐V-101(9),脱出天然气中的重烃组分;
再进入液化板翅式换热器ET-201(16),冷却至-118℃~-122℃;
再进入深冷板翅式换热器ET-301(15),冷却至-155℃~-160℃;
再经节流阀S-101(11)节流降压至150KPa,进入分离器V-102(12),气相作为厂区的燃料气,液相为液化天然气LNG产品进入LNG储罐V-103(13)。
(2)预冷混合冷剂循环:
1.8MPa~2.2MPa高压的预冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再经过节流阀S-201(8)节流降压至0.17MPa~0.24MPa,重新进入预冷板翅式换热器ET-101(17)汽化为冷却天然气、预冷剂高压部分、液化冷剂和深冷剂提供冷量;
然后预冷剂经低压压缩机C-201(7)压缩后依次进入级间空冷器AC-201(6)和水冷器E-201(5)冷却,此时会凝析出部分液相,需要经分离器V-201(4)分离,气相部分进入高压压缩机C-202(3)加压,液相部分进入液体离心泵P-201(24)加压,再将气、液两相混合后,最后再依次进入级间空冷器AC-202(2)和水冷器E-202(1)冷却,恢复为至初始状态的预冷剂,完成预冷循环。
(3)液化混合制冷剂循环:
2.1MPa~2.5MPa的高压的液化混合制冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再进入液化板翅式换热器ET-201(16)冷却至-118℃~-122℃;
通过节流阀S-301(10)节流降压至0.22MPa~0.27MPa,重新依次进入液化板翅式换热器ET-201(16)和预冷板翅式换热器ET-101(17)汽化为液化天然气、液化冷剂高压部分和深冷剂提供冷量;
然后液化冷剂经压缩机C-301(21)压缩后依次进入空冷器AC-301(22)和水冷器E-301(23)冷却,恢复为至初始状态的液化冷剂,完成液化循环。
(4)深冷混合制冷剂循环:
2.8MPa~3.2MPa高压的深冷混合制冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再进入液化板翅式换热器ET-201(16)冷却至-118℃~-122℃;
再进入深冷板翅式换热器ET-301(15)冷却至-155℃~-160℃;
通过节流阀S-401(14)节流降压0.35MPa~0.42MPa,重新依次进入深冷板翅式换热器ET-301(15)、液化板翅式换热器ET-201(16)和预冷板翅式换热器ET-101(17)汽化为深冷天然气、深冷剂高压部分和液化冷剂提供冷量;
然后深冷剂经压缩机C-401(18)压缩后依次进入空冷器AC-401(19)和水冷器E-401(20)冷却,恢复为至初始状态的深冷剂,完成深冷循环。
本发明首先将通过预处理单元的高压天然气(NG)进入预冷板翅式换热器,与预冷混合制冷剂循环换热,冷却至-50℃~-55℃;再进入重烃分离罐,脱出天然气中的重烃组分;再进入液化板翅式换热器,与液化混合制冷剂循环换热,冷却至-118℃~-122℃;再进入深冷板翅式换热器,与深冷混合制冷剂循环换热,冷却至-155℃~-160℃;再经节流阀节流降压至150kPa,进入分离器,气相作为厂区的燃料气,液相为液化天然气(LNG)产品进入LNG储罐。将预处理后的天然气和3种混合制冷剂在冷箱中的板翅式换热器中换热,天然气液化为液化天然气,既可以实现对环境低温的充分利用,也能最大限度提高驱动机功率的利用率。
Claims (2)
1.一种采用混合冷剂级联的天然气液化装置,其特征在于,包括天然气液化回路装置、预冷混合冷剂循环装置、液化混合冷剂循环装置和深冷混合冷剂循环装置;
所述的天然气液化回路装置包括预冷板翅式换热器ET-101(17)、分离器V-101(9)、液化板翅式换热器ET-201(16)、深冷板翅式换热器ET-301(15)、节流阀S-101(11)、分离器V-102(12)和LNG储罐V-103(13);预冷板翅式换热器ET-101(17)的天然气入口与预处理后的天然气管线连通,预冷板翅式换热器ET-101(17)的天然气出口与分离器V-101(9)的入口连通,分离器V-101(9)的气相出口与液化板翅式换热器ET-201(16)的天然气入口连通,液化板翅式换热器ET-201(16)的天然气出口与深冷板翅式换热器ET-301(15)的天然气入口连通,深冷板翅式换热器ET-301(15)的天然气出口经节流阀S-101(11)与分离器V-102(12)的入口连通,分离器V-102(12)的液相出口与LNG储罐V-103(13)的入口连通;
所述的预冷混合冷剂循环装置包括节流阀S-201(8)、压缩机C-201(7)、空冷器AC-201(6)、水冷器E-201(5)、分离器V-201(4)、压缩机C-202(3)、离心泵P-201(24)、空冷器AC-202(2)和水冷器E-202(1);水冷器E-202(1)的出口与预冷板翅式换热器ET-101(17)的预冷混合冷剂入口连通,预冷板翅式换热器ET-101(17)的预冷混合冷剂出口经节流阀S-201(8)与预冷板翅式换热器ET-101(17)的预冷混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的预冷混合冷剂反流出口与压缩机C-201(7)的入口连通,压缩机C-201(7)的出口与空冷器AC-201(6)的入口连通,空冷器AC-201(6)的出口与水冷器E-201(5)的入口连通,水冷器E-201(5)的出口与分离器V-201(4)的入口连通,分离器V-201(4)的气相出口与压缩机C-202(3)的入口连通,分离器V-201(4)的液相出口与离心泵P-201(24)的入口连通,压缩机C-202(3)的出口和离心泵P-201(24)的出口与空冷器AC-202(2)的入口连通,空冷器AC-202(2)的出口与水冷器E-202(1)的入口连通;
所述的液化混合冷剂循环装置包括液化板翅式换热器ET-201(16)、节流阀S-301(10)、压缩机C-301(21)、空冷器AC-301(22)和水冷器E-301(23);水冷器E-301(23)的出口与预冷板翅式换热器ET-101(17)的液化混合冷剂入口连通,预冷板翅式换热器ET-101(17)的液化混合冷剂出口与液化板翅式换热器ET-201(16)的液化混合冷剂入口连通,液化板翅式换热器ET-201(16)的液化混合冷剂出口经节流阀S-301(10)与液化板翅式换热器ET-201(16)的液化混合冷剂反流入口连通,液化板翅式换热器ET-201(16)的液化混合冷剂反流出口与预冷板翅式换热器ET-101(17)的液化混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的液化混合冷剂反流出口与压缩机C-301(21)的入口连通,压缩机C-301(21)的出口与空冷器AC-301(22)的入口连通,空冷器AC-301(22)的出口与水冷器E-301(23)的入口连通;
所述的深冷混合冷剂循环装置包括液化板翅式换热器ET-201(16)、深冷板翅式换热器ET-301(15)、节流阀S-401(14)、压缩机C-401(18)、空冷器AC-401(19)和水冷器E-401(20);水冷器E-401(20)的出口与预冷板翅式换热器ET-101(17)的深冷混合冷剂入口连通,预冷板翅式换热器ET-101(17)的深冷混合冷剂出口与液化板翅式换热器ET-201(16)的深冷混合冷剂入口连通,液化板翅式换热器ET-201(16)的深冷混合冷剂出口与深冷板翅式换热器ET-301(15)的深冷混合冷剂入口连通,深冷板翅式换热器ET-301(15)的深冷混合冷剂出口与节流阀S-401(14)的入口连通,节流阀S-401(14)的出口与深冷板翅式换热器ET-301(15)的深冷混合冷剂反流入口连通,深冷板翅式换热器ET-301(15)的深冷混合冷剂反流出口与液化板翅式换热器ET-201(16)的深冷混合冷剂反流入口连通,液化板翅式换热器ET-201(16)的深冷混合冷剂反流出口与预冷板翅式换热器ET-101(17)的深冷混合冷剂反流入口连通,预冷板翅式换热器ET-101(17)的深冷混合冷剂反流出口与压缩机C-401(18)的入口连通,压缩机C-401(18)的出口与空冷器AC-401(19)的入口连通,空冷器AC-401(19)的出口与水冷器E-401(20)的入口连通。
2.基于上述装置的一种采用混合冷剂级联的天然气液化方法,其特征在于,包括如下步骤:
(1)天然气液化回路:
首先将通过预处理单元的高压天然气NG进入预冷板翅式换热器ET-101(17),冷却至-50℃~-55℃;
再进入重烃分离罐V-101(9),脱出天然气中的重烃组分;
再进入液化板翅式换热器ET-201(16),冷却至-118℃~-122℃;
再进入深冷板翅式换热器ET-301(15),冷却至-155℃~-160℃;
再经节流阀S-101(11)节流降压至150KPa,进入分离器V-102(12),气相作为厂区的燃料气,液相为液化天然气LNG产品进入LNG储罐V-103(13)。
(2)预冷混合冷剂循环:
1.8MPa~2.2MPa高压的预冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再经过节流阀S-201(8)节流降压至0.17MPa~0.24MPa,重新进入预冷板翅式换热器ET-101(17)汽化为冷却天然气、预冷剂高压部分、液化冷剂和深冷剂提供冷量;
然后预冷剂经低压压缩机C-201(7)压缩后依次进入级间空冷器AC-201(6)和水冷器E-201(5)冷却,此时会凝析出部分液相,需要经分离器V-201(4)分离,气相部分进入高压压缩机C-202(3)加压,液相部分进入液体离心泵P-201(24)加压,再将气、液两相混合后,最后再依次进入级间空冷器AC-202(2)和水冷器E-202(1)冷却,恢复为至初始状态的预冷剂,完成预冷循环。
(3)液化混合制冷剂循环:
2.1MPa~2.5MPa的高压的液化混合制冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再进入液化板翅式换热器ET-201(16)冷却至-118℃~-122℃;
通过节流阀S-301(10)节流降压至0.22MPa~0.27MPa,重新依次进入液化板翅式换热器ET-201(16)和预冷板翅式换热器ET-101(17)汽化为液化天然气、液化冷剂高压部分和深冷剂提供冷量;
然后液化冷剂经压缩机C-301(21)压缩后依次进入空冷器AC-301(22)和水冷器E-301(23)冷却,恢复为至初始状态的液化冷剂,完成液化循环。
(4)深冷混合制冷剂循环:
2.8MPa~3.2MPa高压的深冷混合制冷剂进入预冷板翅式换热器ET-101(17)预冷到-50℃~-55℃;
再进入液化板翅式换热器ET-201(16)冷却至-118℃~-122℃;
再进入深冷板翅式换热器ET-301(15)冷却至-155℃~-160℃;
通过节流阀S-401(14)节流降压0.35MPa~0.42MPa,重新依次进入深冷板翅式换热器ET-301(15)、液化板翅式换热器ET-201(16)和预冷板翅式换热器ET-101(17)汽化为深冷天然气、深冷剂高压部分和液化冷剂提供冷量;
然后深冷剂经压缩机C-401(18)压缩后依次进入空冷器AC-401(19)和水冷器E-401(20)冷却,恢复为至初始状态的深冷剂,完成深冷循环。
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