CN102893108B - Method of fractionating a hydrocarbon stream and an apparatus therefor - Google Patents
Method of fractionating a hydrocarbon stream and an apparatus therefor Download PDFInfo
- Publication number
- CN102893108B CN102893108B CN201080043713.6A CN201080043713A CN102893108B CN 102893108 B CN102893108 B CN 102893108B CN 201080043713 A CN201080043713 A CN 201080043713A CN 102893108 B CN102893108 B CN 102893108B
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- CN
- China
- Prior art keywords
- stream
- hydrocarbon component
- hydrocarbon
- cooled
- refrigerant
- 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.)
- Expired - Fee Related
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- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 619
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 618
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 618
- 238000000034 method Methods 0.000 title claims description 49
- 239000003507 refrigerant Substances 0.000 claims abstract description 304
- 238000003860 storage Methods 0.000 claims abstract description 164
- 239000007788 liquid Substances 0.000 claims abstract description 98
- 238000005194 fractionation Methods 0.000 claims abstract description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 238
- 238000001816 cooling Methods 0.000 claims description 195
- 238000010790 dilution Methods 0.000 claims description 40
- 239000012895 dilution Substances 0.000 claims description 40
- 239000007789 gas Substances 0.000 claims description 28
- 239000000203 mixture Substances 0.000 claims description 23
- 239000003345 natural gas Substances 0.000 claims description 22
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical group CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 19
- 239000003795 chemical substances by application Substances 0.000 claims description 18
- 238000005057 refrigeration Methods 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 13
- 239000003949 liquefied natural gas Substances 0.000 claims description 8
- 239000000284 extract Substances 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- 230000009467 reduction Effects 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims 1
- 238000002156 mixing Methods 0.000 description 71
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 34
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 17
- 239000002826 coolant Substances 0.000 description 16
- 239000001294 propane Substances 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 13
- 229910001868 water Inorganic materials 0.000 description 13
- 239000001273 butane Substances 0.000 description 11
- 238000000605 extraction Methods 0.000 description 11
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 4
- 238000007667 floating Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 230000008676 import Effects 0.000 description 4
- 238000005201 scrubbing Methods 0.000 description 4
- 239000013535 sea water Substances 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000000875 corresponding effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- -1 H 2o Chemical class 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 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
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
- F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
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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
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B45/00—Arrangements for charging or discharging refrigerant
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- 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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- 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"
- F25J1/0035—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 gas expansion with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
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- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
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- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0247—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 4 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/64—Propane or propylene
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/66—Butane or mixed butanes
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/22—Compressor driver arrangement, e.g. power supply by motor, gas or steam turbine
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/70—Steam turbine, e.g. used in a Rankine 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/80—Hot exhaust gas turbine combustion engine
- F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
Abstract
A hydrocarbon stream (200) is separated in a first fractionation device (205) to provide an overhead first hydrocarbon component stream (210) and a first hydrocarbon component depleted bottoms stream (300). The overhead first hydrocarbon component stream (210) is liquefied and at least part of it is then cooled against a refrigerant stream (2160) to provide a cooled liquefied first hydrocarbon component reservoir stream (260) and a warmed refrigerant stream (2170). After reducing the pressure of the cooled liquefied first hydrocarbon component reservoir stream (260), it is stored in a liquid first hydrocarbon component reservoir (285) at a first hydrocarbon component storage pressure of at most just above atmospheric pressure, for use as a refrigerant component reservoir make-up consituent. A first hydrocarbon component supply stream (280) may drawn from the liquid first hydrocarbon component reservoir (285) and passed to at least one refrigerant circuit (1000, 2000).
Description
Technical field
The invention provides a kind of method and apparatus for fractionation hydrocarbon stream, described stream comprises at least the first hydrocarbon component, to provide at least the first hydrocarbon component storage device stream.
This hydrocarbon stream obtains by extracting from hydrocarbon feed streams.Natural gas is a kind of common hydrocarbon feed streams.First hydrocarbon component can comprise ethane.
Background technology
Natural gas is a kind of useful fuels sources, and is the source of various hydrocarbon compound.Due to many reasons, be usually desirably in natural gas liquefaction in the source place of natural gas flow or neighbouring liquefied natural gas (LNG) equipment.Such as, natural gas is easy to store and long-distance transportation, this is because it occupies less volume and does not need storage of higher pressures than gaseous form when liquid state more.
In off shore device, offshore liquefaction is carried out to natural gas and proposed a lot of year.This off shore device can be the equipment on floating structure (such as floating platform).These designs are useful, because they are that liquefaction device provides the alternate device of offshore on the bank.These structures or can be anchored in enough dark water at gas field place, to allow LNG product to be unloaded on carrying ship away from seashore or close gas field.They also represent movable assets, and at the end of gas field is close to its productive life, or when economy, environment or political situation need, these assets are reconfigurable to new place.
US Patent No. 4,504,296 disclose and a kind ofly utilize the circulation of two closed type multi-component refrigrants to carry out pre-cooled, liquefaction and subcooled technique to the feed streams (such as natural gas) of methane rich.Refrigerant component supply can be carried out during this process.Ethane, propane and Geng Gao alkyl condensate shift out from feed streams by separated.Ethane, propane and butane can be stored, to use in the multi-component refrigrant synthetic that first is pre-cooled and second is main.Methane supply for the second main cooling refrigeration agent synthetic can be extracted from the heating coil bundle of the main liquefaction heat exchanger of coiled coil (warm bundle).
Refrigerant component supply composition is usually respectively under high pressure (pressure such as, in 10-20bara pressure limit), be stored in tank at the scene at ambient temperature or close to ambient temperature.When needed, refrigerant component supply can flow to closed multi-component refrigrant circulation, to substitute the shortcoming amount of any cold-producing medium from pressure storage tank.
These refrigerant component supply compositions can be inflammable hydrocarbon, can manifest fire and/or explosion danger to make any leakage of hydrocarbon steam.Due to the restriction in space, in offshore installations, these danger are correlated with especially usually.
Summary of the invention
In a first aspect, the invention provides a kind of fractionation and comprise the hydrocarbon stream of at least the first hydrocarbon component to provide the method for at least the first hydrocarbon component storage device stream, described method comprises at least following steps:
-hydrocarbon stream comprising at least the first hydrocarbon component is provided;
-in the first fractionating device, be separated hydrocarbon stream, with the bottom stream of the first hydrocarbon component stream and the first hydrocarbon component dilution that provide top;
The first hydrocarbon component stream at-cooling top, to provide the first hydrocarbon component stream of liquefaction;
A part for first hydrocarbon component stream of-extraction liquefaction, to provide the first hydrocarbon component storage device feed streams of liquefaction;
-rely on the first hydrocarbon component storage device stream of flow of refrigerant to liquefaction to cool, to provide cooling and the first hydrocarbon component storage device stream liquefied and the flow of refrigerant warmed up;
-reduce cooling and the pressure of the first hydrocarbon component storage device stream of liquefaction, to provide the liquid first hydrocarbon component storage device stream reducing pressure;
-the liquid first hydrocarbon component storage device stream reducing pressure is stored in liquid first hydrocarbon component storage device, to be used as the first refrigerant component supply composition at least one refrigerant loop under at the most only higher than the first hydrocarbon component storage pressure of atmospheric pressure.
In one aspect of the method, the invention provides a kind of hydrocarbon stream comprising at least the first hydrocarbon component for fractionation to provide the equipment of at least the first hydrocarbon component storage device stream, described equipment at least comprises:
-the first fractionating device, described first fractionating device is used for from hydrocarbon stream, isolate the first hydrocarbon component, with the bottom stream of the first hydrocarbon component stream and the first hydrocarbon component dilution that provide top;
-the first hydrocarbon component heat exchanger, described first hydrocarbon component heat exchanger for cooling the first hydrocarbon component stream at top, be provided to small part liquefaction the first hydrocarbon component stream;
-the first part flow arrangement, described first part flow arrangement is used for the first hydrocarbon component storage device feed streams distributing liquefaction from the first hydrocarbon component stream of liquefaction at least partly;
-the first hydrocarbon component storage device heat exchanger, described first hydrocarbon component storage device heat exchanger cools for relying on the first hydrocarbon component storage device stream of flow of refrigerant to liquefaction, to provide cooling and the first hydrocarbon component storage device stream liquefied and the flow of refrigerant warmed up;
-the first hydrocarbon component storage device decompressor, described first hydrocarbon component storage device decompressor for reducing cooling and the pressure of the first hydrocarbon component storage device stream of liquefaction, to provide the liquid first hydrocarbon component storage device stream reducing pressure under only storing pressure higher than the first hydrocarbon component of atmospheric pressure at the most;
-liquid first hydrocarbon component storage device, described liquid first hydrocarbon component storage device is communicated with liquid first hydrocarbon component storage device stream fluid;
-at least one refrigerant loop;
-make-up system, described make-up system is arranged to allow fluid between at least one refrigerant loop with liquid first hydrocarbon component storage device to be communicated with.
Accompanying drawing explanation
Embodiments of the invention will be described, in accompanying drawing with reference to appended non-limitative drawings only by citing now:
Fig. 1 and 2 schematically illustrates a kind of equipment for fractionation hydrocarbon stream and method;
Fig. 3 schematically illustrates the Part II main refrigerant effluent being provided for cooling and flows through the first hydrocarbon component storage device heat exchanger; And
Fig. 4 schematically illustrates the single hydrocarbon component supply stream heat exchanger of the embodiment that can be used for Fig. 2.
Fig. 1 and 2 can be considered for supplementing each other: Fig. 1 highlights the details of hydrocarbon product stream, and Fig. 2 highlights the details of refrigerant loop.
In order to the object described, single Reference numeral is by the stream being assigned to pipeline and transmit in pipeline.
Detailed description of the invention
The embodiment of the present invention described herein comprises the method and apparatus for fractionation hydrocarbon stream, it provides the first at least liquid hydrocarbon component storage device stream, to be used as the first refrigerant component supply composition under at the most only higher than the first hydrocarbon component storage pressure of atmospheric pressure.
In the context of the present specification, the situation of the application is only depended at the most higher than the implication of atmospheric pressure, but in any case, be considered to fall into only higher than in the intended scope of atmospheric pressure from atmospheric pressure to the pressure (namely from 0 to about 1barg) higher than the about 1bar of atmospheric pressure.Represent in view of with absolute pressure value, it can represent the pressure being less than about 2bara or the pressure being less than 2bara.
The potential danger relevant to hydrocarbon steam leakage is lowered by following manner: under at the most only higher than the pressure of atmospheric pressure by the first hydrocarbon component and optionally any other hydrocarbon component be stored in reservoir with liquid state, described pressure is such as under the pressure being less than 2bara, preferably from 1bara to not comprising in the scope of 2bara up to 2bara, more preferably in the scope from 1.0bara to 1.2bara, and still more preferably in the scope from 1.0bara to 1.1bara.
The method and equipment are particularly suited for using on offshore hydrocarbon processing facility or in offshore hydrocarbon processing facility, the offshore natural gas liquefaction device on all floating structures in this way (such as floating platform) of described offshore hydrocarbon processing facility.In this offshore installations, space is normally limited, and may to by flammable hydrocarbons steam light caused fire and/or blast needs extra safety precaution.
In a preferred embodiment, wherein hydrocarbon stream also comprises the second hydrocarbon component, and described method also can comprise the following steps:
-in after-fractionating device, be separated the bottom stream of the first hydrocarbon component dilution, to provide the bottom stream of the second hydrocarbon component stream at top and the second hydrocarbon component dilution;
The second hydrocarbon component stream at-cooling top, to provide the second hydrocarbon component stream of liquefaction;
A part for second hydrocarbon component stream of-extraction liquefaction, to provide the second hydrocarbon component storage device stream of liquefaction;
-rely on the second hydrocarbon component storage device stream of flow of refrigerant to liquefaction to cool, to provide cooling and the second hydrocarbon component storage device stream liquefied and the flow of refrigerant warmed up;
-reduce cooling and the pressure of the second hydrocarbon component storage device stream of liquefaction, to provide the liquid state second hydrocarbon component storage device stream reducing pressure;
-under the second hydrocarbon component being less than 2bar stores pressure, the liquid state second hydrocarbon component storage device stream reducing pressure is stored in liquid second hydrocarbon component storage device, to be used as second refrigerant component supply composition.
In a similar fashion, when hydrocarbon stream also comprises the 3rd hydrocarbon component, described method also optionally comprises the following steps:
-in the 3rd fractionating device, be separated the bottom stream of the second hydrocarbon component dilution, to provide the bottom stream of the 3rd hydrocarbon component stream at top and the 3rd hydrocarbon component dilution;
The 3rd hydrocarbon component stream at-cooling top, to provide the 3rd hydrocarbon component stream of liquefaction;
A part for 3rd hydrocarbon component stream of-extraction liquefaction, to provide the 3rd hydrocarbon component storage device stream of liquefaction;
-rely on the three hydrocarbon component storage device stream of flow of refrigerant to liquefaction to cool, to provide cooling and the 3rd hydrocarbon component storage device stream liquefied and the flow of refrigerant warmed up;
-reduce cooling and the pressure of the 3rd hydrocarbon component storage device stream of liquefaction, to provide liquid state the 3rd hydrocarbon component storage device stream reducing pressure;
-under the 3rd hydrocarbon component being less than 2bara stores pressure, liquid state the 3rd hydrocarbon component storage device stream reducing pressure is stored in liquid 3rd hydrocarbon component storage device, as the 3rd refrigerant component supply composition.
In preferred at one, extract from least one refrigerant loop for the one or more strands of flow of refrigerant cooled the first hydrocarbon component storage device stream of liquefaction and the hydrocarbon component storage device stream of any other liquefaction.Distribute according to demand with this integrated of at least one refrigerant loop, to be provided for the refrigerant special loop cooling one or more hydrocarbon component storage device streams, which save capital expenditure (CAPEX).Such as, can be the first refrigerant component reservoir stream from the pre-cooled or main refrigerant circuit for the hydrocarbon stream that liquefies (such as natural gas flow) provides cooling load (duty) to produce LNG with any other refrigerant component reservoir stream.
In one group of embodiment, at least one refrigerant loop comprises pre-cooled refrigerant loop and/or main cooling refrigeration agent loop.
This main coolant circuit can comprise the main cooling refrigeration agent of the main refrigerant form in mixing.In one embodiment, cooling load (cooling duty) is supplied to the first hydrocarbon component storage device heat exchanger by flow of refrigerant, to cool the first hydrocarbon component storage device stream of liquefaction, this flow of refrigerant comes from main refrigerant or its part of mixing.This cooling load can be provided, to cool the first hydrocarbon component storage device stream of liquefaction at lower than the temperature of surrounding environment.
In another embodiment, pre-cooled refrigerant loop can comprise pre-cooled cold-producing medium.Useful especially when this pre-cooled cold-producing medium is the cold-producing medium synthetic of mixing, because the cold-producing medium of this pre-cooled mixing can provide under different temperature and pressures, to make the heating curves of the cold-producing medium of pre-cooled mixing match with the cooling curve of the hydrocarbon component that will cool, thus increase treatment effeciency.
Such as, have than the more hyperbaric second hydrocarbon component storage device stream of the first hydrocarbon component storage device stream and/or the 3rd hydrocarbon component storage device stream if method and apparatus disclosed herein additionally provides, then they can rely on the cold-producing medium of pre-cooled mixing and be cooled, and this is usually optimised better for extracting at than the higher temperature of main refrigerant of cooling heat.
On the other hand, the cooling of the stream except hydrocarbon component storage device stream provides by this at least one refrigerant loop.
In one embodiment, at least one refrigerant loop can comprise pre-cooled refrigerant loop, and this pre-cooled refrigerant loop comprises the cold-producing medium of pre-cooled mixing.The first hydrocarbon component stream at top by carrying out heat exchange with the pre-cooled cold-producing medium mixed or its part and be cooled, to provide the first hydrocarbon component stream of liquefaction at lower than the temperature of surrounding environment.The cold-producing medium of this pre-cooled mixing in the refrigerant loop of pre-cooled mixing can be obtained under multiple pressure, in this case, can select according to cooling curve the suitable stress level being used for this heat exchange.
This equipment comprises make-up system, and this make-up system is arranged to allow fluid between at least one refrigerant loop with liquid first hydrocarbon component storage device to be communicated with.When the liquid first hydrocarbon component storage device stream of stored reduction pressure needs to be used as the first refrigerant component supply composition, it form of the first hydrocarbon component supply stream can flow at least one refrigerant loop from liquid first hydrocarbon component storage device via make-up system.
This make-up system can comprise one or more hydrocarbon component supply stream heat exchanger, preferably, per share hydrocarbon component supply stream at least one.Make the first hydrocarbon component supply stream flow at least one refrigerant loop from liquid first hydrocarbon component storage device to comprise the following steps:
-in this hydrocarbon component supply stream heat exchanger, heat the first hydrocarbon component stream, to provide the first hydrocarbon component stream warmed up;
-the first hydrocarbon component stream of making this warm up flows at least one refrigerant loop via the first hydrocarbon component flow control valve warmed up alternatively.
A kind of similar method can be used for making any second refrigerant component supply stream and/or the 3rd refrigerant component supply stream flow at least one refrigerant loop.
In a preferred embodiment, the hydrocarbon component stream warmed up is liquid stream.They can be used as the liquid refrigerant component supply thing of the cold-producing medium synthetic for mixing.Such as after coolant compressor stroke (trip), because a part for refrigerant loop reduces pressure, a large amount of liquid hydrocarbon components for cold-producing medium synthetic may be needed.The fine setting of this cold-producing medium synthetic realizes by using the steam at the top from the first hydrocarbon component gas/liquid separation and any second hydrocarbon component gas/liquid separation and/or the 3rd hydrocarbon component gas/liquid separation.
Fig. 1 is the schematic diagram of the equipment 1 for fractionation hydrocarbon stream 200.Hydrocarbon stream 200 comprises at least the first hydrocarbon component.Preferably, hydrocarbon stream 200 comprises the first hydrocarbon component, the second hydrocarbon component, the 3rd hydrocarbon component, the 4th hydrocarbon component and other hydrocarbon components.4th hydrocarbon component can have the molecular weight higher than the 3rd hydrocarbon component and thus have higher boiling point, 3rd hydrocarbon component can have the molecular weight higher than the second hydrocarbon component and thus have higher boiling point, and the second hydrocarbon component can have the molecular weight higher than the first hydrocarbon component and thus have higher boiling point.
In a preferred embodiment, hydrocarbon stream 200 can comprise one or more in the hydrocarbon component limited as follows:
-the first component: ethane;
-second component: propane;
-three components: butane; And
-Four composition: condensate.
Hydrocarbon stream 200 preferably extracts from natural gas, and this natural gas obtains from natural gas reservoirs or petroleum reservoir, but alternately can obtain from another source, and this another source comprises synthesis source, such as Fischer-Tropsch reaction.As described in more detail below, hydrocarbon stream 200 can be such as pretreated result in pre-cooled and extraction unit.
Hydrocarbon stream 200 can be pressurized stream, and this pressurized stream has the pressure being greater than 2bara.Hydrocarbon stream 200 can flow to the first fractionating device 205, and hydrocarbon stream is separated in this first fractionating device, with the bottom stream 300 of the first hydrocarbon component stream 210 and the first hydrocarbon component dilution that provide top.In one embodiment, the first hydrocarbon component can be ethane, and the first fractionating device 205 can be dethanizer, and to make the first hydrocarbon component stream 210 at this top be rich ethane stream, and the bottom stream 300 of this first hydrocarbon component dilution is the stream of ethane dilution.
The first hydrocarbon component stream 210 at top can flow to the first hydrocarbon component heat exchanger 215, and it is cooled in the first hydrocarbon component heat exchanger, to be provided to the first hydrocarbon component stream 220 of small part liquefaction.In a preferred embodiment, the first hydrocarbon component stream 210 at top relies in the loop of pre-cooled mix refrigerant the flow of refrigerant of the pre-cooled mixing circulated or its part and is cooled.For simplicity, the refrigerant loop of pre-cooled mixing is not shown in Figure 1, but has carried out more detailed discussion relatively with the embodiment of Fig. 2.
First hydrocarbon component stream 220 of at least part of liquefaction can flow to the first hydrocarbon component gas/liquid separation 225, to be provided as the first hydrocarbon component stream 230a of the liquefaction of bottom stream and to provide the first hydrocarbon Component vapor stream 227 at top.The first hydrocarbon Component vapor stream 227 at top can be used as fuel gas, or is used as the first refrigerant component supply thing of the vaporous in the refrigerant loop of mixing.
It is apparent that adjust the amount of the first hydrocarbon Component vapor stream 227 by changing the top of producing to the cooling load of the first hydrocarbon component heat exchanger 215.Such as, if this cooling load is lowered, then by the more first hydrocarbon Component vapor stream 227 at top of production and the first hydrocarbon component stream 230a of less liquefaction.The latter can be implemented when needing the first refrigerant component supply thing of vaporous.
First hydrocarbon component stream 230a of liquefaction can flow to optional first hydrocarbon component pump 235, is supplied to the first hydrocarbon component part flow arrangement 245 with the first hydrocarbon component stream 230b that (will be pumped) liquefaction.The first hydrocarbon component stream 230 that this first hydrocarbon component part flow arrangement 245 (can be pumped) liquefaction is divided into two parts: the first hydrocarbon component backflow stream 240a of liquefaction and the first hydrocarbon component storage device stream 250 of liquefaction.
First hydrocarbon component backflow stream 240a of liquefaction can flow through the first hydrocarbon component backflow decompressor 255 (such as Joule-Thomson valve), to provide the first hydrocarbon component backflow stream 240b of expansion.The the first hydrocarbon component backflow stream 240b expanded can flow to the first fractionating device 205, to improve the separation in the first fractionating device.Preferably, the first hydrocarbon component backflow stream 240b of expansion is added in the first fractionating device 205 in the position of gravimetric height higher than hydrocarbon stream 200.
Then first hydrocarbon component storage device stream 250 of liquefaction flow to the first hydrocarbon component storage device heat exchanger 265, and it carries out heat exchange with flow of refrigerant in this first hydrocarbon component storage device heat exchanger.First hydrocarbon component storage device heat exchanger 265 provides cooling and the first hydrocarbon component storage device stream 260 of liquefaction and the flow of refrigerant warmed up.In a preferred embodiment, flow of refrigerant carrys out main refrigerant or its part of the mixing in autonomous cooling refrigeration agent loop.For simplicity, this main cooling refrigeration agent loop is not shown in Figure 1, but has carried out more detailed discussion relatively with the embodiment of Fig. 2.
Cooling and liquefaction the first hydrocarbon component storage device stream 260 can be that there is the pressurized stream being greater than 2bara pressure.Before storing, this cooling and the first hydrocarbon component storage device stream 260 of liquefaction can flow to the first hydrocarbon component storage device decompressor 275 (such as Joule-Thomson valve), reduces the liquid first hydrocarbon component storage device stream 270 of pressure to provide.This first hydrocarbon component storage device decompressor 275 is preferably by this cooling and the pressure of the first hydrocarbon component storage device stream 260 of liquefaction is reduced to storage pressure close to being less than 2bara.
Clearly, substantially be in liquid degree for the temperature of stream 250 being reduced to when the first hydrocarbon component expands in the first hydrocarbon component storage device decompressor 275 by keeping, the first hydrocarbon component storage device stream 250 cooling this liquefaction in the first hydrocarbon component storage device heat exchanger 265 is very important.In practice, this means this cooling and liquefaction the first hydrocarbon component storage device stream 260 be in overcooled state.
Then the liquid first hydrocarbon component storage device stream 270 reducing pressure can flow to liquid first hydrocarbon reservoir 285, for storing under the pressure being less than 2bara.Liquid first hydrocarbon reservoir 285 can be cryogenic storage tank.Preferably, the scope interior (namely in the scope of 30-70mbarg) that pressure is in the above 30-70mbar of atmospheric pressure is stored.In an example, storing pressure is about 50mbarg.When the first hydrocarbon component is ethane, storing temperature will lower than-89 DEG C, to make the gasification of liquid minimum.
Any boil-off gas from liquid first hydrocarbon reservoir 285 can be used as the first hydrocarbon component evaporative air 290 and is moved out of.If necessary, after optional heating, the first hydrocarbon component evaporative air 290 can flow at least one refrigerant loop, is used as the first refrigerant component supply thing of the vaporous of the cold-producing medium synthetic of mixing.
First hydrocarbon component supply stream 280 is liquid stream, it can extract (alternatively from liquid first hydrocarbon reservoir 285, assisted by the first submerged pump be arranged in the first hydrocarbon reservoir 285), and preferably flow in liquid form at least one refrigerant loop, as the first refrigerant component supply thing of the cold-producing medium synthetic for mixing.Optional delivery pump 283 can be arranged in the first hydrocarbon component supply stream 280.The embodiment of this and Fig. 2 has carried out more detailed discussion relatively.
The bottom stream 300 getting back to this first fractionating device 205, first hydrocarbon dilution can be pressurized stream, and this pressurized stream has the pressure being greater than 2bara.300 dilution first hydrocarbon components are flowed in the bottom of the first hydrocarbon dilution, and are rich at least the second hydrocarbon component, and are preferably rich in the 3rd hydrocarbon component, the 4th hydrocarbon component and other hydrocarbon components.
The bottom stream 300 of the first hydrocarbon dilution can flow to after-fractionating device 305, and it is separated in this after-fractionating device, with the bottom stream 400 of the second hydrocarbon component stream 310 and the second hydrocarbon component dilution that provide top.In one embodiment, second hydrocarbon component can be propane, and after-fractionating device 305 can be depropanizer, to make the second hydrocarbon component stream 310 at top be rich propane stream, and the bottom of the second hydrocarbon component dilution stream 400 is the stream of propane (and ethane) dilution.
The second hydrocarbon component stream 310 at top can flow to the second hydrocarbon component heat exchanger 315, and it is cooled in this second hydrocarbon component heat exchanger, to be provided to the second hydrocarbon component stream 320 of small part liquefaction.By cooling water (such as seawater), cooling load is supplied to the second hydrocarbon component heat exchanger 315.
Second hydrocarbon component stream 320 of at least part of liquefaction can flow to the second hydrocarbon component gas/or liquid/gas separator 325, to be provided as the second hydrocarbon component stream 330a of the liquefaction of bottom stream, and provides the second hydrocarbon Component vapor stream 327 at top.The second hydrocarbon Component vapor stream 327 at top can be used as fuel gas, or is used as the steam supply thing of the second hydrocarbon component in the refrigerant loop of mixing.
Second hydrocarbon component stream 330a of liquefaction can flow to optional second hydrocarbon component pump 335, is provided to the second hydrocarbon component part flow arrangement 345 with the second hydrocarbon component stream 330b that (will be pumped) liquefaction.The the second hydrocarbon component stream 330b being somebody's turn to do (being pumped) liquefaction can be divided into two parts by this second hydrocarbon component part flow arrangement 345: the second hydrocarbon component backflow stream 340a of liquefaction and the second hydrocarbon component storage device stream 350 of liquefaction.
Second hydrocarbon component backflow stream 340a of liquefaction can flow through the second hydrocarbon component backflow decompressor 355 (such as Joule-Thomson valve), to provide the second hydrocarbon component backflow stream 340b of expansion.Second hydrocarbon component backflow stream 340b of this expansion can flow to this after-fractionating device 305, to improve the separation in after-fractionating device.Preferably, the second hydrocarbon component backflow stream 340b of expansion flows the high position of 300 gravimetric height in the bottom than the first hydrocarbon component dilution and is added in after-fractionating device 305.
Then second hydrocarbon component storage device stream 350 of liquefaction flow to the second hydrocarbon component storage device heat exchanger 365, and it carries out heat exchange with flow of refrigerant in this second hydrocarbon component storage device heat exchanger.Second hydrocarbon component storage device heat exchanger 365 provides cooling and the second hydrocarbon component storage device stream 360 of liquefaction and the flow of refrigerant warmed up.In a preferred embodiment, flow of refrigerant is from the cold-producing medium of the pre-cooled mixing in pre-cooled refrigerant loop or its part.Preferably, the second hydrocarbon component storage device stream 350 carries out heat exchange with the pre-cooled cold-producing medium mixed or its part at lower than the temperature of environment temperature.For simplicity, this pre-cooled refrigerant loop is not shown in Figure 1, but has carried out more detailed discussion relatively with the embodiment of Fig. 2.
Cooling and liquefaction the second hydrocarbon component storage device stream 360 can be pressurized stream, this pressurized stream has the pressure being greater than 2bara.Before storing, cooling and the second hydrocarbon component storage device stream 360 of liquefaction can flow to the second hydrocarbon component storage device decompressor 375 (such as Joule-Thomson valve), reduces the liquid state second hydrocarbon component storage device stream 370 of pressure to provide.Second hydrocarbon component storage device decompressor 375 preferably will cool and the pressure of the second hydrocarbon component storage device stream 360 of liquefaction is reduced to the close storage pressure being less than 2bara.
Clearly, substantially be in liquid degree for when the temperature of stream 350 being reduced to and making the second hydrocarbon component expand in the second hydrocarbon component storage device decompressor 375 by keeping, it is very important for cooling the second hydrocarbon component storage device stream 350 of liquefaction in the second hydrocarbon component storage device heat exchanger 365.In fact, this means cool and liquefaction the second hydrocarbon component storage device stream 360 be in supercooling state.
Then the liquid state second hydrocarbon component storage device stream 370 reducing pressure can flow to for carrying out the liquid state second hydrocarbon reservoir 385 stored under the pressure being less than 2bara.Liquid second hydrocarbon reservoir 385 can be cryogenic storage tank.Preferably, pressure is stored in the scope of the above 30-70mbar of atmospheric pressure.In an example, storing pressure is about 50mbarg.When the second hydrocarbon component is propane, storing temperature will lower than-43 DEG C, to make the gasification of liquid minimum.
Any boil-off gas from liquid second hydrocarbon reservoir 385 can be used as the second hydrocarbon component evaporative air 390 and is moved out of.If necessary, after optional heating, the second hydrocarbon component evaporative air 390 can flow at least one refrigerant loop, as the second refrigerant component supply thing of the vaporous of the cold-producing medium synthetic for mixing.
Second hydrocarbon component supply stream 380 is liquid stream, and can extract (alternatively from liquid second hydrocarbon reservoir 385, assisted by the second submerged pump be arranged in the second hydrocarbon reservoir 385), and preferably flow at least one refrigerant loop in liquid form, as the second refrigerant component supply thing of the cold-producing medium synthetic for mixing.Optional delivery pump 383 can be arranged in the second hydrocarbon component supply stream 380.The embodiment of this and Fig. 2 has carried out more detailed discussion relatively.
The bottom stream 400 getting back to after-fractionating device 305, second hydrocarbon dilution can be pressurized stream, and this pressurized stream has the pressure being greater than 2bara.400 dilution first hydrocarbon components and the second hydrocarbon component are flowed in the bottom of the second hydrocarbon dilution, and are rich at least the 3rd hydrocarbon component, and are preferably rich in the 4th hydrocarbon component and other hydrocarbon components.
The bottom stream 400 of the second hydrocarbon dilution can flow to the 3rd fractionating device 405, and it is separated in the 3rd fractionating device, with the bottom stream 500 of the 3rd hydrocarbon component stream 410 and the 3rd hydrocarbon component dilution that provide top.In one embodiment, 3rd hydrocarbon component can be butane, and the 3rd fractionating device 405 can be debutanizer, to make the 3rd hydrocarbon component stream 410 at top be methane-rich stream, and the bottom of the 3rd hydrocarbon component dilution stream 500 is the stream of butane (propane and ethane) dilution.
The bottom stream 500 of the 3rd hydrocarbon component dilution can be liquid stream, and flows to the 3rd hydrocarbon component lower heat exchanger 510, and it is cooled in the 3rd hydrocarbon component lower heat exchanger, to provide cooling and the stream 520 of the 3rd hydrocarbon component dilution of liquid state.The bottom stream 500 of the 3rd hydrocarbon component dilution can rely on freezing cooling water flow and be cooled in the 3rd hydrocarbon component lower heat exchanger 510.
Cooling the and then stream 520 of the 3rd hydrocarbon component dilution of liquid state can flow to the reservoir decompressor 525 (such as Joule-Thomson valve) of the 3rd hydrocarbon component dilution, to provide the reservoir stream 530 of liquid state the 3rd hydrocarbon component dilution reducing pressure.The reservoir decompressor 525 of the 3rd hydrocarbon component dilution preferably will cool and the pressure of the stream 520 of the 3rd hydrocarbon component dilution of liquid state is reduced to the close storage pressure being less than 2bara.
Then the stream 530 of liquid state the 3rd hydrocarbon component dilution of reduction pressure flow to the reservoir 535 for carrying out liquid state the 3rd hydrocarbon component dilution stored under the pressure being less than 2bara.The reservoir 535 of this liquid state the 3rd hydrocarbon component dilution can be storage tank.Preferably, pressure is stored in the scope of the above 30-70mbar of atmospheric pressure.The stream of this liquid state the 3rd hydrocarbon component dilution can be hydrocarbon condensate, thus the reservoir 535 of liquid 3rd hydrocarbon component dilution can be condensate reservoir.
The 3rd hydrocarbon component stream 410 at top can flow to the 3rd hydrocarbon component heat exchanger 415, and it is cooled in the 3rd hydrocarbon component heat exchanger, to be provided to the 3rd hydrocarbon component stream 420 of small part liquefaction.By cooling water (such as seawater), cooling load is supplied to the 3rd hydrocarbon component heat exchanger 415.
3rd hydrocarbon component stream 420 of at least part of liquefaction can flow to the 3rd hydrocarbon component gas/or liquid/gas separator 425, to be provided as the 3rd hydrocarbon component stream 430 of the liquefaction of bottom stream, and provides the 3rd hydrocarbon Component vapor stream 427 at top.The 3rd hydrocarbon Component vapor stream 427 at this top can be used as fuel gas.
3rd hydrocarbon component stream 430a of liquefaction can flow to optional 3rd hydrocarbon component pump 435, is supplied to the 3rd hydrocarbon component part flow arrangement 445 with the 3rd hydrocarbon component stream 430b that (will be pumped) liquefaction.The 3rd hydrocarbon component stream 430b that 3rd hydrocarbon component part flow arrangement 445 (can be pumped) liquefaction is divided into two parts: the 3rd hydrocarbon component backflow stream 440a of liquefaction and the 3rd hydrocarbon component storage device stream 450 of liquefaction.
3rd hydrocarbon component backflow stream 440a of liquefaction can flow to the 3rd hydrocarbon component backflow decompressor 455 (such as Joule-Thomson valve), to provide the 3rd hydrocarbon component backflow stream 440b of expansion.3rd hydrocarbon component backflow stream 440b of this expansion can flow to the 3rd fractionating device 405, to improve the separation in the 3rd fractionating device.Preferably, the 3rd hydrocarbon component backflow stream 440b of expansion flows the high position of 400 gravimetric height in the bottom than the second hydrocarbon component dilution and is added in the 3rd fractionating device 405.
Then 3rd hydrocarbon component storage device stream 450 of liquefaction flow to the 3rd hydrocarbon component storage device heat exchanger 465, and it carries out heat exchange with flow of refrigerant in the 3rd hydrocarbon component storage device heat exchanger.3rd hydrocarbon component storage device heat exchanger 465 provides cooling and the 3rd hydrocarbon component storage device stream 460 of liquefaction and the flow of refrigerant warmed up.In a preferred embodiment, this flow of refrigerant is from the cold-producing medium of the pre-cooled mixing in pre-cooled refrigerant loop or its part.Preferably, the 3rd hydrocarbon component storage device stream 450 carries out heat exchange with the pre-cooled cold-producing medium mixed or its part at lower than the temperature of environment temperature.For simplicity, this pre-cooled refrigerant loop is not shown in Figure 1, but has carried out more detailed discussion relatively with the embodiment of Fig. 2.
Cooling and liquefaction the 3rd hydrocarbon component storage device stream 460 can be pressurized stream, this pressurized stream has the pressure being greater than 2bara.Before storing, cooling and the 3rd hydrocarbon component storage device stream 460 of liquefaction can flow to the 3rd hydrocarbon component storage device decompressor 475 (such as Joule-Thomson valve), reduces liquid state the 3rd hydrocarbon component storage device stream 470 of pressure to provide.3rd hydrocarbon component storage device decompressor 475 preferably will cool and the pressure of the 3rd hydrocarbon component storage device stream 460 of liquefaction is reduced to the close storage pressure being less than 2bara.
Clearly, substantially be in liquid degree for when the temperature of stream 450 being reduced to and making the 3rd hydrocarbon component expand in the 3rd hydrocarbon component storage device decompressor 475 by keeping, it is very important for cooling the second hydrocarbon component storage device stream 450 of liquefaction in the 3rd hydrocarbon component storage device heat exchanger 465.In fact, this means cool and liquefaction the 3rd hydrocarbon component storage device stream 460 be in supercooled state under.
Then liquid state the 3rd hydrocarbon component storage device stream 470 reducing pressure flow to for carrying out liquid state the 3rd hydrocarbon reservoir 485 stored under the pressure being less than 2bara.Liquid 3rd hydrocarbon reservoir 485 can be cryogenic storage tank.Preferably, pressure is stored in the scope of the above 30-70mbar of atmospheric pressure.In an example, storing pressure is about 50mbarg.When the 3rd hydrocarbon component is butane, storing temperature will lower than 0 DEG C, to make the gasification of liquid minimum.
3rd hydrocarbon component supply stream 480 can extract (alternatively from liquid 3rd hydrocarbon component storage device 485, assisted by the 3rd submerged pump be arranged in the 3rd hydrocarbon reservoir 485), and preferably flow at least one refrigerant loop (1000,2000) in liquid form, as the 3rd refrigerant component supply supply stream.Optional delivery pump 483 can be arranged in the 3rd hydrocarbon component supply stream 480.
In a preferred embodiment, method and apparatus disclosed herein can be used as a part for the cooling processing (process of preferably liquefying) for hydrocarbon feed streams 40.Fig. 1 additionally provides the schematic diagram for the treatment of the equipment 1 with cooling (especially liquefying) hydrocarbon feed streams 40.Hydrocarbon stream 200 is prepared by hydrocarbon feed streams 40 in pre-cooled and extraction unit 10.And pre-cooled and extraction unit 10 produces pre-cooled methane-rich stream 170 by hydrocarbon feed streams 40.This pre-cooled methane-rich stream 170 is liquefied subsequently at least one main heat exchanger 175, to be provided to the hydrocarbon stream 180 that small part (preferably whole) liquefies.
There is many known structure for this pre-cooled and extraction unit 10 in the prior art, this pre-cooled and extraction unit prepares hydrocarbon stream 200 (form such as in natural gas liquids stream) and pre-cooled methane-rich stream, and usual this unit comprises at least separating step and cooling step.For example, a kind of structure is like this illustrated in greater detail in FIG.This will further describe hereinafter.
Hydrocarbon feed streams 40 can be any suitable gas flow that will be cooled and liquefy, but normally natural gas flow.Usually, natural gas flow is the hydrocarbon synthetic mainly comprising methane.Preferably, hydrocarbon feed streams 40 comprises the methane of at least 50mol%, more preferably comprises the methane of at least 80mol%.
Hydrocarbon synthetic (such as natural gas) also can comprise non-hydrocarbons, such as H
2o, N
2, CO
2, Hg, H
2s and other sulfide etc.If desired, natural gas can carry out pretreatment before carrying out cooling and any liquefaction.This pretreatment can comprise reduction and/or remove less desirable component (such as CO
2and H
2s) step or other steps (such as cool in early days, precharge or similar step).Because these steps are known to those skilled in the art, their mechanism is discussed no longer further at this.
Thus, term " hydrocarbon feed streams " 40 also can be included in the synthetic before any process (this process comprises purification), and has been processed partly, substantially or fully to reduce and/or to remove any synthetic of at least one compound or material (including but not limited to sulphur, sulfide, carbon dioxide, water and mercury).
According to source, natural gas can comprise the heavy hydrocarbon of the ratio methane of different amount, especially ethane, propane and butane, and may the pentane of less amount and aromatic hydrocarbons.This synthetic changes according to the type of gas and place.
Normally, due to multiple reason, these hydrocarbon heavier than methane were removed to some extent before any significant cooling from hydrocarbon feed streams, this multiple reason is such as have different freezing or condensing temperature, and what these were different freeze or condensing temperature can make their block each several part of methane liquefaction equipment or provide the specification of expectation for liquiefied product.By domethanizing column, C
2+ hydrocarbon can be isolated from hydrocarbon feed streams, or their content in hydrocarbon feed streams reduces, and this comprises C by what provide the hydrocarbon stream of the methane rich at top and bottom
2the poor methane stream of+hydrocarbon.
Bottom comprise C
2the poor methane stream of+hydrocarbon is preferred hydrocarbon stream 200 used herein.The stream of the poor methane of bottom flows to other above-mentioned separators, to provide independent hydrocarbon component and condensate.
After releasing, methane-rich stream is cooled.Methane-rich stream flows against at least one flow of refrigerant at least one refrigerant loop.This refrigerant loop can comprise at least one coolant compressor, to be compressed to the flow of refrigerant of small part evaporation, thus provides the flow of refrigerant of compression.Then the flow of refrigerant of compression can be cooled, to provide flow of refrigerant in cooler (such as aerial cooler or water cooler).Coolant compressor is driven by least one turbine or motor.
The cooling of methane-rich stream can be realized at least one stage.Initial cooling (also referred to as pre-cooled or supplement heat rejecter) realizes by using the pre-cooled cold-producing medium of pre-cooled refrigerant loop (cold-producing medium of such as unitary system cryogen or mixing), to provide pre-cooled methane-rich stream at least one pre-cooled heat exchanger.Pre-cooled methane-rich stream preferably such as at lower than the temperature of 0 DEG C by partial liquefaction.
Preferably, these pre-cooled heat exchangers can comprise the pre-cooled stage, wherein any cooling is subsequently carried out at least one main heat exchanger, a part for pre-cooled methane-rich stream to be liquefied at least one main cooling stage and/or secondary cooling stage.
Thus, can comprise two or more cooling stages, each stage has at least one step, part etc.Such as, each cooling stage can comprise one to five heat exchanger.Be rich in the hydrocarbon of methane and/or cold-producing medium or their part and can not flow through all heat exchangers of cooling stage and/or all identical heat exchangers.
In one embodiment, hydrocarbon can be cooled and liquefy in the method comprising two or three cooling stages.The pre-cooled stage is preferably tending towards the temperature of methane-rich stream to be reduced to lower than 0 DEG C, is usually in the scope of-20 DEG C to-70 DEG C.
Heat exchanger as two or more pre-cooled heat exchangers is known in the art.These pre-cooled heat exchangers are preferably shell-and-tube heat exchanger.
Main cooling stage preferably with this pre-cooled stage separate.That is, main cooling stage comprises at least one independently main heat exchanger.This main cooling stage be preferably tending towards by hydrocarbon (normally by the pre-cooled stage cool be rich in methane at least partially) temperature be reduced to less than-100 DEG C.
At least one in any main heat exchanger is preferably wound tube heat exchanger or shell-and-tube heat exchanger.Alternatively, this main heat exchanger can comprise more than two cooling end sections in its enclosure interior, and each cooling end section can be considered to a cooling stage or be considered to relative to another cool position independently " heat exchanger ".
In another embodiment, one or two in pre-cooled flow of refrigerant and any main refrigerant stream can flow through at least one heat exchanger, preferably flows through the heat exchanger that two or more are pre-cooled and main, to provide the flow of refrigerant of cooling.
If cold-producing medium is the cold-producing medium of the mixing in the refrigerant loop (in such as any pre-cooled refrigerant loop and any main refrigerant circuit one or two) of mixing, the cold-producing medium then mixed can be formed by the mixture of two or more components be selected from following group, and this group comprises following component: nitrogen, methane, ethane, ethene, propane, propylene, butane, pentane etc.At least one other cold-producing medium can be used in the refrigerant loop or other cooling circuits of independent or overlap.
Any pre-cooled refrigerant loop can comprise the pre-cooled cold-producing medium of mixing.The cold-producing medium of any cooling mainly can comprise the main refrigerant of mixing.As the cold-producing medium of the mixing pointed by this or the flow of refrigerant of mixing comprise the different component of two kinds of at least 5mol%.More preferably, the cold-producing medium of mixing comprises two or more in following group, and this group comprises: nitrogen, methane, ethane, ethene, propane, propylene, butane and pentane.
Common synthetic for pre-cooled mix refrigerant can be:
Methane (C1) 0-20mol%;
Ethane (C2) 5-80mol%;
Propane (C3) 5-80mol%;
Butane (C4) 0-15mol%;
Assembly divides and comprises 100mol%.
Common synthetic for main cooling and mixing cold-producing medium can be:
Nitrogen 0-25mol%;
Methane (C1) 20-70mol%;
Ethane (C2) 30-70mol%;
Propane (C3) 0-30mol%;
Butane (C4) 0-15mol%;
Assembly divides and comprises 100mol%.
Preferably, (especially liquefying) methane-rich stream of cooling described herein can be stored at least one storage tank.
In another preferred embodiment, if hydrocarbon feed streams 40 comes from natural gas, then (the preferably liquefying) methane-rich stream cooled can be liquefied natural gas (LNG) stream.
For the treatment of with liquefaction hydrocarbon stream many methods be known in the prior art.Fig. 1 provides a kind of such illustrative methods.
A kind of hydrocarbon feed streams 40 (such as coming from the stream of natural gas) is now provided.Hydrocarbon feed streams 40 preferably includes methane and at least the first hydrocarbon component and optional second hydrocarbon component and the 3rd hydrocarbon component, (such as ethane, propane and butane), as mentioned above.Hydrocarbon feed streams 40 preferably in be suitable for cool form, with make its can pretreated thus reduce and/or remove less desirable component (such as CO
2and H
2s).
Hydrocarbon feed streams 40 is preferably pressurized stream, and it can flow to pre-cooled and extraction unit 10.In the example depicted in fig. 1, first hydrocarbon feed streams 40 flow in hydrocarbon feed separator 75, and this hydrocarbon feed separator is included in pre-cooled and extraction unit.This hydrocarbon feed separator can be the gas/liquid separation of any type.This hydrocarbon feed separator 75 provides hydrocarbon feed steam stream 80 and the hydrocarbon feed liquid bottom stream 90 at top.
Hydrocarbon feed steam stream 80 can be inflated in overhead hydrocarbon vapors stream expansion gear 95 (such as turbine expansion device), to provide the top hydrocarbon feed streams 100 of expansion.The top hydrocarbon feed streams 100 of this expansion can flow to feed fractionating device 115 (such as scrubbing tower or domethanizing column), to provide overhead stream 120 and the hydrocarbon stream 200 of methane rich.Hydrocarbon stream 200 is according to disclosed in this and method as above and by further fractionation.
The hydrocarbon feed liquid bottom stream 90 coming from hydrocarbon feed separator 75 can be inflated in bottom feed stream expansion gear 105 (such as Joule-Thomson valve), to provide the bottom hydrocarbon feed streams 110 of expansion.The bottom hydrocarbon feed streams 110 expanded can flow to feed fractionating device 115, to improve the separation of hydrocarbon component in feed fractionating device.Preferably, the bottom hydrocarbon feed streams 90 of expansion flows in feed fractionating device 115 in the position lower than top hydrocarbon feed streams 100 gravimetric height expanded.
The overhead stream 120 being rich in methane from feed fractionating device 115 can flow at least one methane-rich stream compressor 125,135.In the embodiment shown in fig. 1, arrange the first methane-rich stream compressor 125, this first methane-rich stream compressor carries out Mechanical Driven by overhead hydrocarbon vapors stream expansion gear 95 via axle 97.First methane-rich stream compressor 125 provides the overhead stream 130 of the methane rich of the first compression.Then the overhead stream 130 of the methane rich of this first compression is compressed by the second methane-rich stream compressor 135, and this second methane-rich stream compressor carries out Mechanical Driven by methane-rich stream compressor drive 137.Methane-rich stream compressor drive 137 can be selected from gas turbine, steam turbine and motor.
Second methane-rich stream compressor 135 provides methane-rich stream 140.Methane-rich stream 140 can flow at least one pre-cooled heat exchanger 145,155,165, and wherein, methane-rich stream relies on pre-cooled cold-producing medium to be cooled.This pre-cooled cold-producing medium can be the pre-cooled cold-producing medium of mixing.Fig. 1 respectively illustrates the first pre-cooled heat exchanger 155 of pre-cooled heat exchanger 145, second and the 3rd pre-cooled heat exchanger 165, the methane-rich stream 160 that the methane-rich stream 150, second that they each provide the first cooling cools and pre-cooled methane-rich stream.Preferably, multiple pre-cooled heat exchanger 145,155,165 uses, under the pre-cooled cold-producing medium of this mixing can be arranged in and be in different pressure in each pre-cooled heat exchanger 145,155,165 (description as relevant to the embodiment of Fig. 2) together with the pre-cooled cold-producing medium of mixing.
At least one pre-cooled heat exchanger 145,155,165 ultimately provides the hydrocarbon stream 170 of pre-cooled methane rich.The hydrocarbon stream 170 of pre-cooled methane rich can flow in main heat exchanger 175, for cooling and being preferably used for liquefaction.Main heat exchanger 175 can be shell-and-tube heat exchanger or wound tube heat exchanger.
The hydrocarbon stream 170 of pre-cooled methane rich can rely on the main refrigerant in main refrigerant circuit and cooled and be preferably liquefied in main heat exchanger 175, thus is provided to the hydrocarbon stream 180 that small part (preferably whole) liquefies, such as LNG.
In an alternative embodiment, in the alternative pre-cooled and extraction unit do not described in detail in FIG, flow through for before being separated in scrubbing tower at hydrocarbon feed streams, hydrocarbon feed streams can rely on pre-cooled cold-producing medium and be pre-cooled.Scrubbing tower provides the overhead stream of hydrocarbon stream and methane rich, and this hydrocarbon stream can carry out fractionation according to method and apparatus disclosed herein.The overhead stream of methane rich can flow to overhead stream heat exchanger, and it is cooled in this overhead stream heat exchanger, to provide the overhead stream of the methane rich of cooling.Then the overhead stream of the methane rich of this cooling flows to overhead stream collector, and this overhead stream collector provides bottom the collector overhead stream of methane rich and overhead stream collector and flows, and bottom this overhead stream collector, stream can be used as backflow and turns back to scrubbing tower.The collector overhead stream of methane rich can flow to main heat exchanger, for relying on main cooling refrigeration agent to carry out cooling and preferably liquefying, to be provided to the hydrocarbon stream 180 that small part (preferably whole) liquefies.
Fig. 1 does not illustrate the pre-cooled and main cooling refrigeration agent loop that can use in equipment described herein and method.Fig. 2 provides the n-lustrative scheme of the equipment for the methane-rich stream 140a that liquefies and preferably liquefy, and shows exemplary pre-cooled refrigerant loop 1000 (comprising the pre-cooled cold-producing medium of mixing) and exemplary main cooling refrigeration agent loop 2000 (comprising the main cooling refrigeration agent of mixing).
Methane-rich stream 140a is by carrying out compression to provide to the overhead stream of the methane rich from feed fractionating device as above.Methane-rich stream 140a can flow to the first pre-cooled heat exchanger 145a.This first pre-cooled heat exchanger 145a can be the pre-cooled heat exchanger 145a of high pressure.Methane-rich stream 140a is cooled, and carries out indirect heat exchange with the pre-cooled cold-producing medium mixed, the pre-cooled cold-producing medium of this mixing in the shell-side of the pre-cooled heat exchanger 145a of high pressure with high-pressure evaporation.Preferably, methane-rich stream 140a is partly condensed in the pre-cooled heat exchanger 145a of high pressure.
The hydrocarbon of cooling (preferred partial condensation) leaves the pre-cooled heat exchanger 145a of high pressure, as the methane-rich stream 150a of the first cooling.The operation of pre-cooled cold-producing medium will be described in further detail below, this pre-cooled cold-producing medium is in pre-cooled refrigerant loop 1000.
The methane-rich stream 150a of the first cooling can flow to the second pre-cooled heat exchanger 155a.This second pre-cooled heat exchanger 155a can be the pre-cooled heat exchanger 155a of middle pressure.The methane-rich stream 150a of the first cooling is cooled, and carries out indirect heat exchange with the pre-cooled cold-producing medium mixed, and the pre-cooled cold-producing medium of this mixing operates with middle pressure in the shell-side of the pre-cooled heat exchanger 155a of middle pressure.Preferably, if methane-rich stream 140a is not partly condensed in the pre-cooled heat exchanger 145a of high pressure, then the methane-rich stream 150a of the first cooling is partly condensed in the pre-cooled heat exchanger 155a of middle pressure.
(preferred partial condensation) hydrocarbon of cooling leaves middle pressure heat exchanger 155a, as the methane-rich stream 160a of the second cooling.The methane-rich stream 160a of this second cooling can flow to the 3rd pre-cooled heat exchanger 165a.3rd pre-cooled heat exchanger 165a can be the pre-cooled heat exchanger 165a of low pressure.Methane-rich stream 160a of this second cooling is cooled, and carries out indirect heat exchange with the pre-cooled cold-producing medium mixed, the pre-cooled cold-producing medium of this mixing in the shell-side of low pressure pre-cooled heat exchanger 165a with low voltage operated.Preferably, if the methane-rich stream 150a of the first cooling is not partly condensed in the pre-cooled heat exchanger 155a of middle pressure, then the methane-rich stream 160a of the second cooling is partly condensed in the pre-cooled heat exchanger 165a of low pressure.
(preferred partial condensation) hydrocarbon of cooling leaves the pre-cooled heat exchanger 165a of low pressure, as pre-cooled methane-rich stream 170a.The term " high pressure ", " middle pressure " and " low pressure " that describe pre-cooled heat exchanger use with relative meaning.That is, the shell pressure of low pressure pre-cooled heat exchanger 165a is less than the shell pressure of the pre-cooled heat exchanger 155a of middle pressure.The shell pressure of middle pressure pre-cooled heat exchanger 155a is less than the shell pressure of the pre-cooled heat exchanger 145a of high pressure.These pressure can change according to the pre-cooled refrigerant composition of mixing and the composition of stream that will be pre-cooled.Suitable operating pressure is known to those skilled in the art.
In these figures in a unshowned alternate embodiments, two and not three pre-cooled heat exchangers can be set, use for together with the pre-cooled cold-producing medium of mixing.Such as, can use the pre-cooled heat exchanger of high pressure and the pre-cooled heat exchanger of low pressure, wherein the pre-cooled heat exchanger of this high pressure operates under the shell pressure higher than the pre-cooled heat exchanger of low pressure.
Pre-cooled methane-rich stream 170a can flow to optionally main heat exchanger knock-out drum (knock out drum) 185 before leading to main heat exchanger 175a.This main heat exchanger knock-out drum 185 provides the steam stream 190 of pre-cooled methane rich at top.
The steam stream 190 of pre-cooled methane rich can flow to main heat exchanger 175a, at this place, it relies on the main refrigerant of mixing and is liquefied by least part of (preferably whole), to be provided to the hydrocarbon stream 180a that small part (preferably whole) liquefies.
The equipment of Fig. 2 also discloses convection current in the first pre-cooled heat exchanger 145a, the second pre-cooled heat exchanger 155a and the 3rd pre-cooled heat exchanger 165a and cools.Method disclosed herein is useful especially for the cooling of the main refrigerant of mixing, and the main refrigerant of this mixing is used for carrying out cooling further and liquefaction at least partly to the steam stream 190 of pre-cooled methane rich in main heat exchanger 175a.
The main refrigerant of mixing is preferably cooled and is more preferably partly condensed in four-stage.The main refrigerant of mixing can flow through one or more main refrigerant cooler 2015, and in the pre-cooled stage, flow through high pressure pre-cooled heat exchanger 145a, middle pressure pre-cooled heat exchanger 155a and the pre-cooled heat exchanger 165a of low pressure.
Main refrigerant stream 2010 can be the compressive flow provided by least one main cooling refrigeration agent compressor 2225, it flows to one or more cooler 2015 (such as aerial cooler or water cooler), to provide the main refrigerant stream 2020 of the mixing of the first cooling.
The main refrigerant stream 2020 of this first cooling can flow to the pre-cooled refrigerant heat exchanger 145a of high pressure.The cold-producing medium of this mixing is cooled by carrying out indirect heat exchange with the pre-cooled cold-producing medium mixed, and the pre-cooled cold-producing medium of this mixing under high pressure evaporates in the shell-side of the pre-cooled heat exchanger 145a of high pressure.The main refrigerant of the mixing of cooling leaves the pre-cooled heat exchanger 145a of high pressure, as the main refrigerant stream 2030 of the second cooling.
The main refrigerant stream 2030 of this second cooling can flow to the pre-cooled refrigerant heat exchanger 155a of middle pressure.The cold-producing medium of this mixing is cooled by carrying out indirect heat exchange with the pre-cooled cold-producing medium mixed, and the pre-cooled cold-producing medium of this mixing evaporates in the shell-side of the pre-cooled heat exchanger 155a of middle pressure under middle pressure.The main refrigerant of the mixing of cooling leaves the pre-cooled heat exchanger 155a of middle pressure, as the main refrigerant stream 2040 of the 3rd cooling.
The main flow of refrigerant 2040 of the 3rd cooling can flow to the pre-cooled heat exchanger 165a of low pressure.The cold-producing medium of this mixing is cooled by carrying out indirect heat exchange with pre-cooled cold-producing medium and is preferably partly condensed, and this pre-cooled cold-producing medium under low pressure evaporates in the shell-side of the pre-cooled heat exchanger 165a of low pressure.The main refrigerant of the mixing of this cooling leaves the pre-cooled heat exchanger 165a of low pressure, as the main refrigerant stream 2050 of pre-cooled mixing.
The main refrigerant stream 2050 of this pre-cooled mixing can flow to main refrigerant separator 2055 (such as gas/liquid separation).This main refrigerant separator 2055 provides and flows to Part I main refrigerant stream 2060 in main heat exchanger 175a and Part II main refrigerant stream 2110 respectively.The steam stream that Part I main refrigerant stream 2060 preferably takes out from main refrigerant separator 2055 at top.The liquid flow that this Part II main refrigerant stream 2110 preferably takes out from the bottom of main refrigerant separator 2055.
This Part I main refrigerant stream 2060 and Part II main refrigerant stream 2110 are automatically cooled in main heat exchanger 175a, be inflated and flow to the shell-side of this heat exchanger, to provide cooling.
Especially, Part I main refrigerant stream 2060 relies on the main refrigerant of mixing and is cooled in main heat exchanger 175a, is preferably liquefied at least partly, and discharges from heat exchanger, to provide the Part I main refrigerant stream 2070 of cooling.Then the Part I main refrigerant stream 2070 of this cooling can flow at least one Part I main refrigerant expansion gear (such as Joule-Thomson valve), to provide the Part I main refrigerant stream 2080 of expansion.Then the Part I main refrigerant stream 2080 of this expansion can flow to the shell-side of main heat exchanger 175a, to provide cooling.
This Part II main refrigerant stream 2110 relies on the main refrigerant of mixing and is cooled in main heat exchanger 175a, and discharges from this heat exchanger, to provide the Part II main refrigerant stream 2120 of cooling.The Part II main refrigerant stream 2120 of this cooling can be shunted in the Part II part flow arrangement 2125 of cooling, thus provide the Part II main refrigerant of cooling to continue the Part II main refrigerant effluent 2160 of stream 2130 and cooling, using as flow of refrigerant.
The Part II main refrigerant Continuous Flow 2130 of this cooling can expand, to provide the Part II main refrigerant stream 2140 of expansion at least one Part II main refrigerant expansion gear 2135 (such as Joule-Thomson valve).The Part II main refrigerant stream 2140 of this expansion can be as described below combined in the combination unit 2145 of Part II stream with the Part II main refrigerant effluent 2180 of expansion, to provide the Part II main refrigerant stream 2150 of the expansion of combination.Then the Part II main refrigerant stream 2080 of the expansion of this combination can flow to the shell-side of main heat exchanger 175a, to provide cooling.
The Part II main refrigerant effluent 2160 of cooling can be used for cooling load being supplied to the first hydrocarbon component storage device heat exchanger 265a.In such embodiments, the Part II main refrigerant effluent 2160 of cooling carries out heat exchange with the first hydrocarbon component storage device stream (in Fig. 1 250) of liquefaction, and provides the Part II main refrigerant effluent 2170 (flow of refrigerant as warming up) and cooling and the first hydrocarbon component storage device stream (in Fig. 1 260) of liquefaction that warm up.
The steam stream 190 of main refrigerant and pre-cooled methane rich and Part I main refrigerant stream 2060 and Part II main refrigerant stream 2110 carry out indirect heat exchange, to cool these streams and to warm up this main refrigerant.This main refrigerant warmed up is discharged near the bottom place of main heat exchanger 175a or its, as the main refrigerant stream 2210 warmed up.
The main refrigerant stream 2210 that this warms up flows to main refrigerant compressor knock-out drum 2215.This main refrigerant compressor knock-out drum 2215 provides main refrigerant compressor feed streams 2220.This main refrigerant compressor feed streams 2220 is gaseous state substantially.
Main refrigerant compressor feed streams 2220 can flow to main cooling refrigeration agent compressor 2225, and wherein, it is compressed to be provided as the main refrigerant stream 2010 of compressive flow.This main cooling refrigeration agent compressor 2225 is mechanically driven via main refrigerant compressor drive shaft 2245 by main refrigerant compressor drive 2235 (such as gas or steam turbine or motor).
Fig. 2 shows a mode easily, and the Part II main refrigerant effluent 2170 wherein warmed up can turn back to main cooling refrigeration agent loop 2000.The Part II main refrigerant effluent 2170 warmed up can flow at least one Part II main refrigerant expansion gear 2175 warmed up, to provide the Part II main refrigerant effluent 2180 of expansion.The Part II main refrigerant effluent 2180 expanded can be combined with the Part II main refrigerant stream 2140 expanded, and flow to main heat exchanger 175a, as combining and the Part II main refrigerant stream 2150 (as mentioned above) expanded.
Alternately, as illustrated in figure 3, the Part II main refrigerant effluent 2160 of cooling flow through the Part II main refrigerant expansion gear 2176 (form preferably in Joule-Thomson valve) of at least one cooling before being fed into the first hydrocarbon component storage device heat exchanger 265a.In this case, the Part II main refrigerant effluent 2170 warmed up turns back to main cooling refrigeration agent loop 2000 by it being directly supplied in main refrigerant compressor knock-out drum 2215.Therefore, the temperature of the first hydrocarbon component storage device stream 260 can be controlled by handling the Part II main refrigerant expansion gear 2176 of cooling in the exit of the first hydrocarbon component storage device heat exchanger 265a.Alternatively, the Part II main refrigerant effluent 2170 warmed up also can flow to the Part II main refrigerant expansion gear 2175 warmed up, and matches with the pressure of the main refrigerant stream 2210 warmed up to make its pressure.
Still alternately (not shown), the Part II main refrigerant effluent 2160 of cooling can take out from the Part II main refrigerant stream 2140 expanded.
Get back to pre-cooled refrigerant loop 1000 as shown in Figure 2, the pre-cooled flow of refrigerant 1010 of the pre-cooled cold-producing medium of mixing is provided as compressive flow by pre-cooled coolant compressor 1505.Pre-cooled coolant compressor 1505 is mechanically driven via pre-cooled coolant compressor driving shaft 1525 by pre-cooled coolant compressor driver 1515 (such as gas or steam turbine or motor).This pre-cooled flow of refrigerant 1010 preferably provides at very high pressures.
Pre-cooled flow of refrigerant 1010 can be cooled, to provide the pre-cooled flow of refrigerant 1020 of the first cooling in one or more pre-cooled refrigerant cooler 1015 (such as aerial cooler or water cooler).The pre-cooled flow of refrigerant 1020 of this first cooling can flow to the pre-cooled combination unit 1025 of the first cooling, this combination unit is connected to make-up system 600, and this make-up system is arranged and to be communicated with the fluid between one or more in the first hydrocarbon component storage device 285 or higher hydrocarbon component storage device 385 for setting up pre-cooled refrigerant loop 1000.In the embodiment of fig. 2, make-up system 600 provides pre-cooled cold-producing medium supply stream 630, and its pre-cooled flow of refrigerant 1020 that can cool with first in combination unit 1025 is combined, to provide pre-cooled cold-producing medium memory feed streams 1030.
Pre-cooled cold-producing medium supply stream 630 can comprise in this first hydrocarbon component and the second hydrocarbon component one or both.Such as, the first hydrocarbon component supply stream 280 is the liquid stream from liquid first hydrocarbon component supply reservoir, and can flow to the first hydrocarbon component supply stream heat exchanger 605.First hydrocarbon component stream 280 warms up by the first hydrocarbon component supply stream heat exchanger 605, to provide the first hydrocarbon component stream 610 (it can be liquid stream) warmed up.First hydrocarbon component stream 280 is by carrying out heat exchange with any suitable heat medium 606 (such as water/glycol flow, seawater stream or propane stream) and warmed up, and this depends on design preferences.
Alternately, heat medium 606 provides with the form of steam stream under selected pressure, to make steam condensation under the impact warming up the first hydrocarbon component stream 280.Condensing steam stream is utilized to be as the benefit of heat medium: to carry out the solidification danger of freezing caused heat medium than lower when using liquid or distillation steam owing to relying on the first cold hydrocarbon component supply stream 280.In addition, if allow steam condensation during itself and the first cold hydrocarbon component supply stream 280 carry out heat exchange, then the heat medium of per unit mass can increase higher heat with latent heat form.
The good example of suitable steam stream is water vapour stream.Water vapour can (such as in burning boiler or in heat recovery boiler) produce in any known fashion.This heat recovery boiler is heated by the hot gas gas turbine exhaust stream from gas turbine.Suitably, it can be gas turbine, this gas turbine can be used as the compressor drive (compressor drive 137 of such as pre-cooled coolant compressor driver 1515, main refrigerant compressor drive 2235 or methane-rich stream) in method and apparatus described herein, and/or is used as the driver produced for the generator of the one or more electric energy in these compressor drives.
Preferably, this water vapour stream is under the pressure of 2bara to 10bara.The advantage of the water vapour that employing is under quite low pressure is: steam can come from the waste steam stream of the unit (such as steam turbine) using high-pressure steam stream.Suitably, it can be steam turbine, steam turbine can be used as the compressor drive (compressor drive 137 of such as pre-cooled coolant compressor driver 1515, main refrigerant compressor drive 2235 or methane-rich stream) in method and apparatus described herein, and/or is used as the driver produced for the generator of the one or more electric energy in these compressor drives.
And, utilize low pressure water vapor stream (such as having the pressure of 10bara) Billy to use high-pressure water vapor stream, be easier to meet the pressure vessel specification for the first hydrocarbon component supply stream heat exchanger 605.
The the first hydrocarbon component stream 610 warmed up can flow through the first hydrocarbon stream control valve 615 warmed up, to provide in check first hydrocarbon component stream 620.This in check first hydrocarbon component stream 620 flows to pre-cooled cold-producing medium supply stream 630 by hydrocarbon component stream combination unit 625.
The pressure of the first hydrocarbon component stream 610 warmed up can at more than 30bara, such as between 30bara and 55bara, preferably just over the refrigerant pressure at least one refrigerant loop, in this refrigerant loop, the first hydrocarbon component stream 610 warmed up is injected into.Temperature is from 5 DEG C within the scope of 35 DEG C.In an example, the pressure in the first hydrocarbon component stream 610 warmed up is 41bara, and its temperature is 25 DEG C.In another example, the pressure in the first hydrocarbon component stream 610 warmed up is 41bara, and its temperature is 10 DEG C.
Second hydrocarbon component supply stream 380 is the liquid stream coming from liquid second hydrocarbon component supply reservoir, can flow to the second hydrocarbon component supply stream heat exchanger 635.Second hydrocarbon component supply stream heat exchanger 635 warms up the second hydrocarbon component stream 380, and to provide the second hydrocarbon component stream 640 warmed up, this second hydrocarbon component stream warmed up is liquid stream.Second hydrocarbon component stream 380 can rely on any suitable heat medium 636 (such as above for described in this first hydrocarbon component supply stream heat exchanger 605, as water/glycol flow, seawater stream, propane stream or water vapour stream) and warmed up, this depends on design preferences.
The the second hydrocarbon component stream 640 warmed up can flow through the second hydrocarbon component flow control valve 645 warmed up, to provide in check second hydrocarbon component stream 650.In check second hydrocarbon component stream 650 flows to pre-cooled cold-producing medium supply stream 630 by hydrocarbon component stream combination unit 625.
The pressure of the second hydrocarbon component stream 640 warmed up can at more than 30bara, such as, between 30bara to 55bara.Temperature can be in 5 DEG C within the scope of 35 DEG C.In an example, the pressure in the second hydrocarbon component stream 640 warmed up is 41bara, and its temperature is 25 DEG C.In another example, the pressure in the second hydrocarbon component stream 640 warmed up is 41bara, and its temperature is 10 DEG C.
Pre-cooled cold-producing medium memory feed streams 1030 can flow to pre-cooled cold-producing medium collector 1035.This pre-cooled cold-producing medium can be discharged, as pre-cooled cold-producing medium supply stream 1040 from this pre-cooled cold-producing medium collector 1035.This pre-cooled cold-producing medium supply stream 1040 can flow to the pre-cooled heat exchanger 145a of high pressure.The pre-cooled cold-producing medium of this very mixing of high pressure is cooled automatically by carrying out indirect heat exchange with the pre-cooled cold-producing medium mixed, and the pre-cooled cold-producing medium of this mixing under high pressure evaporates in the shell-side of the pre-cooled heat exchanger 145a of high pressure.Cooling and the pre-cooled cold-producing medium of mixing leaves the pre-cooled heat exchanger 145a of high pressure, as the pre-cooled flow of refrigerant 1050 of the first cooling.
The pre-cooled flow of refrigerant 1050 of the first cooling can flow to the pre-cooled cold-producing medium separator 1055 of the first cooling, the pre-cooled flow of refrigerant 1110 cooled to provide continuous print first and the pre-cooled refrigerant branches stream 1060 of the first cooling.
The pre-cooled refrigerant branches stream 1060 of the first cooling flows to the pre-cooled refrigerant expansion device 1065 (such as Joule-Thomson valve) of the first cooling, to provide high pressure pre-cooled flow of refrigerant 1070.The pre-cooled refrigerant branches stream 1060 of the first cooling is expanded to the operating pressure of the pre-cooled heat exchanger 145a shell-side of high pressure.
Then the pre-cooled flow of refrigerant of high pressure 1070 flows to the shell-side of the pre-cooled heat exchanger 145a of high pressure, provides cooling with the main refrigerant stream 2020 of the mixing to pre-cooled cold-producing medium supply stream 1040, methane-rich stream 140a and first cooling.The pre-cooled cold-producing medium of high pressure is warmed up and is evaporated at least partly in the pre-cooled heat exchanger 145a of high pressure.This warms up and the pre-cooled cold-producing medium of high pressure of evaporation is at least partly discharged from the pre-cooled refrigerant heat exchanger 145a of high pressure, returns stream 1080 as the pre-cooled cold-producing medium of high pressure.
The pre-cooled cold-producing medium of high pressure returns stream 1080 can flow to the pre-cooled cold-producing medium knock-out drum 1085 of high pressure, to remove any liquid phase making the pre-cooled cold-producing medium of high pressure return before stream 1090 flows to pre-cooled coolant compressor 1505 as the pre-cooled refrigerant vapour of high pressure.
The pre-cooled flow of refrigerant 1110 that the continuous print first provided by the pre-cooled cold-producing medium separator 1055 of the first cooling cools can flow to the pre-cooled refrigerant heat exchanger 155a of middle pressure.The pre-cooled cold-producing medium of high pressure mixing is cooled automatically by carrying out indirect heat exchange with the pre-cooled cold-producing medium mixed, and the pre-cooled cold-producing medium of this mixing evaporates in the shell-side of the pre-cooled heat exchanger 155a of middle pressure under middle pressure.The pre-cooled cold-producing medium of mixing of cooling leaves the pre-cooled refrigerant heat exchanger 155a of middle pressure, as the pre-cooled flow of refrigerant 1120 of the second cooling.
The pre-cooled flow of refrigerant 1120 of the second cooling can flow to the pre-cooled cold-producing medium separator 1125 of the second cooling, the pre-cooled flow of refrigerant 1210 cooled to provide continuous print second and the pre-cooled refrigerant branches stream 1130 of the second cooling.
The pre-cooled refrigerant branches stream 1130 of the second cooling can flow to the pre-cooled refrigerant expansion device 1135 (such as Joule-Thomson valve) of the second cooling, to provide the pre-cooled flow of refrigerant 1140 of middle pressure.The pre-cooled refrigerant branches stream 1130 of the second cooling is expanded to the operating pressure of the pre-cooled heat exchanger 155a shell-side of middle pressure.
Then the pre-cooled flow of refrigerant of middle pressure 1140 can flow to the shell-side of the pre-cooled heat exchanger 155a of middle pressure, provides cooling with the main refrigerant stream 2030 of the mixing of methane-rich stream 150a and second cooling of the pre-cooled flow of refrigerant 1110, first cooled continuous print first cooling.The pre-cooled cold-producing medium of middle pressure is warmed up and is evaporated at least partly in the pre-cooled heat exchanger 155a of middle pressure.To warm up and the pre-cooled cold-producing medium of middle pressure of at least partly evaporation is discharged from the pre-cooled refrigerant heat exchanger 155a of middle pressure, return stream 1150 as the pre-cooled cold-producing medium of middle pressure.
The pre-cooled cold-producing medium of middle pressure returns stream 1150 can be combined with the middle pressure the warmed up pre-cooled cold-producing medium effluent 1260 of combination as described by the refrigerant compositions device 1155 using middle pressure pre-cooled, returns stream 1160 to provide the pre-cooled cold-producing medium of the middle pressure of combination.
The pre-cooled cold-producing medium of middle pressure of combination returns stream 1160 and can flow to the pre-cooled cold-producing medium knock-out drum 1165 of middle pressure, to remove any liquid phase being returned before stream 1170 flows to pre-cooled coolant compressor 1505 as the pre-cooled refrigerant vapour of middle pressure by pre-cooled for middle pressure cold-producing medium.
The pre-cooled flow of refrigerant 1210 that the continuous print second provided by the pre-cooled cold-producing medium separator 1125 of the second cooling cools can flow to the pre-cooled cold-producing medium separator 1215 that continuous print second cools.The pre-cooled cold-producing medium separator 1215 that continuous print second cools provides the pre-cooled flow of refrigerant 1310 of another continuous print second cooling and the pre-cooled cold-producing medium effluent 1220 of the second cooling.
The pre-cooled cold-producing medium effluent 1220 of the second cooling flows to the pre-cooled refrigerant side flow splitting device 1225 of the second cooling, the pre-cooled cold-producing medium effluent 1230b that the pre-cooled cold-producing medium effluent 1230a cooled to provide Part I second respectively and Part II second cool.The pre-cooled cold-producing medium effluent 1230a that Part I second cools and the pre-cooled cold-producing medium effluent 1230b that Part II second cools flows to Part I second pre-cooled refrigerant expansion device 1235a and the pre-cooled refrigerant expansion device 1235b of Part II second, to provide Part I middle pressure pre-cooled cold-producing medium effluent 1240a and Part II middle pressure pre-cooled cold-producing medium effluent 1240b respectively.The pre-cooled cold-producing medium effluent 1230a that Part I second cools and the pre-cooled cold-producing medium effluent 1230b that Part II second cools can be expanded to the middle pressure of middle pressure pre-cooled heat exchanger 155a shell-side.
Cooling load can be supplied to the first hydrocarbon heat exchanger 215a by Part I middle pressure pre-cooled cold-producing medium effluent 1240a.Part I middle pressure pre-cooled cold-producing medium effluent 1240a can carry out heat exchange with the first hydrocarbon component stream (210 in Fig. 1) at top, to provide the first hydrocarbon component stream (220 in Fig. 1) of Part I middle pressure pre-cooled cold-producing medium effluent 1250a and the liquefaction at least partly warmed up.
Cooling load can be supplied to the 3rd hydrocarbon component storage device heat exchanger 465a by Part II middle pressure pre-cooled cold-producing medium effluent 1240b.Part II middle pressure pre-cooled cold-producing medium effluent 1240b can carry out heat exchange (450 in Fig. 1) with the 3rd hydrocarbon component storage device stream of liquefaction, to provide the Part II middle pressure pre-cooled cold-producing medium effluent 1250b and cooling and the 3rd hydrocarbon component storage device stream (460 in Fig. 1) of liquefaction that warm up.
The Part I middle pressure pre-cooled cold-producing medium effluent 1250a warmed up and Part II middle pressure pre-cooled cold-producing medium effluent 1250b can be mixed in pre-cooled cold-producing medium effluent combination unit 1255 at the middle pressure warmed up, to provide the middle pressure warmed up of combination pre-cooled cold-producing medium effluent 1260.
The pre-cooled flow of refrigerant 1310 that another continuous print second that the pre-cooled cold-producing medium separator 1215 cooled by continuous print second provides cools can flow to the pre-cooled refrigerant heat exchanger 165a of low pressure.The pre-cooled cold-producing medium of mixing of middle pressure is cooled automatically by carrying out indirect heat exchange with the pre-cooled cold-producing medium mixed, and the pre-cooled cold-producing medium of this mixing under low pressure evaporates in the shell-side of the pre-cooled heat exchanger 165a of low pressure.The pre-cooled cold-producing medium of mixing of cooling leaves the pre-cooled refrigerant heat exchanger 165a of low pressure, as the pre-cooled flow of refrigerant 1320 of the 3rd cooling.
The pre-cooled flow of refrigerant 1320 of the 3rd cooling can flow to the pre-cooled refrigerant branches stream 1330 of the pre-cooled cold-producing medium separator 1325 of the 3rd cooling, the pre-cooled flow of refrigerant 1410 cooled to provide continuous print the 3rd and the 3rd cooling.
The pre-cooled refrigerant branches stream 1330 of the 3rd cooling can flow to the pre-cooled refrigerant expansion device 1335 (such as Joule-Thomson valve) of the 3rd cooling, to provide low pressure pre-cooled flow of refrigerant 1340.The pre-cooled refrigerant branches stream 1330 of the 3rd cooling is expanded to the operating pressure of low pressure pre-cooled heat exchanger 165a shell-side.
Then the pre-cooled flow of refrigerant of low pressure 1340 flows to the shell-side of the pre-cooled heat exchanger 165a of low pressure, provides cooling with the mixing main refrigerant stream 2040 of methane-rich stream 160a and the 3rd cooling of the pre-cooled flow of refrigerant 1310, second cooled another continuous print second cooling.The pre-cooled cold-producing medium of low pressure is warmed up and is evaporated at least partly in the pre-cooled heat exchanger 165a of low pressure.This warms up and the pre-cooled cold-producing medium of low pressure of evaporation is at least partly discharged from the pre-cooled refrigerant heat exchanger 165a of low pressure, returns stream 1350 as the pre-cooled cold-producing medium of low pressure.
The pre-cooled cold-producing medium of low pressure returns stream 1350 and can mix mutually with the pre-cooled cold-producing medium Continuous Flow 1450 of the low pressure warmed up of combination as described by using low pressure pre-cooled refrigerant compositions device 1355, returns stream 1360 to provide the pre-cooled cold-producing medium of the low pressure of combination.
The pre-cooled cold-producing medium of low pressure of combination returns stream 1360 and can flow to the pre-cooled cold-producing medium knock-out drum 1365 of low pressure, to remove any liquid phase being returned before stream 1370 flows to pre-cooled coolant compressor 1505 as the pre-cooled refrigerant vapour of low pressure by pre-cooled for low pressure cold-producing medium.
The pre-cooled flow of refrigerant 1410 that the continuous print the 3rd provided by the pre-cooled cold-producing medium separator 1325 of the 3rd cooling cools can flow to the pre-cooled cold-producing medium Continuous Flow separator 1415 of the 3rd cooling, the pre-cooled cold-producing medium Continuous Flow 1420b that the pre-cooled cold-producing medium Continuous Flow 1420a cooled to provide Part I the 3rd respectively and Part II the 3rd cool.The pre-cooled cold-producing medium Continuous Flow 1420b that the pre-cooled cold-producing medium Continuous Flow 1420a of the 3rd cooling of Part I and Part II the 3rd cool can flow to the pre-cooled refrigerant expansion device 1425a of Part I the 3rd and pre-cooled refrigerant expansion device 1425b of Part II the 3rd, to provide Part I low pressure pre-cooled cold-producing medium Continuous Flow 1430a and the pre-cooled cold-producing medium Continuous Flow 1430b of Part II low pressure respectively.The pre-cooled cold-producing medium Continuous Flow 1420b that the pre-cooled cold-producing medium Continuous Flow 1420a of the 3rd cooling of Part I and Part II the 3rd cool can be expanded to the low pressure of low pressure pre-cooled heat exchanger 165a shell-side.
The pre-cooled cold-producing medium Continuous Flow 1430 of Part I low pressure can provide cooling load to hydrocarbon feed streams heat exchanger 65a.The pre-cooled cold-producing medium Continuous Flow 1430a of Part I low pressure can carry out heat exchange with hydrocarbon feed streams (40 in Fig. 1), to provide the hydrocarbon feed streams of the pre-cooled cold-producing medium Continuous Flow 1440a of the Part I low pressure warmed up and cooling.The hydrocarbon feed streams of cooling can flow to hydrocarbon feed separator (75 in Fig. 1).
Part II low pressure pre-cooled cold-producing medium effluent 1430b can provide cooling load to the second hydrocarbon component storage device heat exchanger 365a.The pre-cooled cold-producing medium Continuous Flow 1430b of Part II low pressure can carry out heat exchange with the second hydrocarbon component storage device stream (350 in Fig. 1) of liquefaction, to provide the pre-cooled cold-producing medium Continuous Flow 1440b of the Part II low pressure warmed up and cooling and the second hydrocarbon component storage device stream (360 in Fig. 1) of liquefaction.
The Part I low pressure pre-cooled cold-producing medium Continuous Flow 1440a warmed up can mix in pre-cooled cold-producing medium effluent combination unit 1445 in the low pressure warmed up mutually with Part II low pressure pre-cooled cold-producing medium Continuous Flow 1440b, to provide the low pressure warmed up of combination pre-cooled cold-producing medium Continuous Flow 1450.
In the embodiment of fig. 2, main refrigerant compressor 1505 is shown as compound compressor.The pre-cooled refrigerant vapour of high pressure returns the high pressure section that stream 1090 can flow to pre-cooled coolant compressor 1505.The pre-cooled refrigerant vapour of middle pressure returns the middle pressure level that stream 1170 can flow to pre-cooled coolant compressor 1505.The pre-cooled refrigerant vapour of low pressure returns the low-pressure stage that stream 1370 can flow to pre-cooled coolant compressor 1505.These streams can be compressed, to provide the pre-cooled flow of refrigerant 1010 be under very high pressure.
Alternately, main refrigerant compressor can be the one or more main refrigerant compressor of series connection, and they have high pressure suction grade, middle pressure suction grade and low-pressure suction grade.
In a preferred embodiment, as shown in Figure 4, the second hydrocarbon component supply stream heat exchanger 635 of Fig. 2 and the second hydrocarbon component supply stream heat exchanger 635 provide with the form of single hydrocarbon component supply stream heat exchanger 1600.Single hydrocarbon supply stream heat exchanger 1600 is arranged in the manifold of pipeline, and this pipeline installing has selector valve 1601a, 1601b, 1601c, 1601d, so as selective by these hydrocarbon component supply streams only one flow through single hydrocarbon supply stream heat exchanger 1600.Other streams one or more strands of except the first hydrocarbon component supply stream and the second hydrocarbon component supply stream can be optionally made to flow through this single hydrocarbon supply stream heat exchanger 1600 for it should be understood that person of ordinary skill in the field that this manifold may extend into alternatively.Heat medium 1606 can be any one in the above-mentioned type.
Fig. 4 also illustrates the first available submerged pump 284 and the second submerged pump 384, and they can be convenient to extract corresponding hydrocarbon component supply stream from corresponding liquid second hydrocarbon reservoir.These submerged pumps are not shown in Figure 2, although they also can be present in that embodiment.
Single hydrocarbon supply stream heat exchanger 1600 or the independently first hydrocarbon supply stream heat exchanger 605 and the second hydrocarbon supply stream heat exchanger 635 can be any suitable types, comprise plate-fin heat exchanger, printed circuit type heat exchanger and shell-and-tube heat exchanger.Shell-and-tube heat exchanger is preferred, and thus, preferably, hydrocarbon supply stream flows through the pipe side of hydrocarbon supply stream heat exchanger, and heat medium flows through shell-side.
Typically, the pressure of hydrocarbon supply stream 280,380 can between 35bara to 60bara in the import department of adopted hydrocarbon supply stream heat exchanger.In an example, this pressure can be about 43bara.When using low-pressure steam stream as heat medium, in an example, the pressure of the import department of the hydrocarbon supply stream heat exchanger adopted is 4bara, is 5bara in another example.The temperature of the import department of the hydrocarbon supply stream heat exchanger adopted preferably is being in more than the condensation temperature under main pressure, such as, more than between 10 DEG C to 100 DEG C.Under the pressure of 4.3bara, the condensation temperature of this water vapour is close to 146 DEG C.In this case, the temperature of import department can be about 198 DEG C.
It will be understood by those skilled in the art that without departing from the scope of the appended claims, the present invention can be realized in many different ways.Such as, the present invention is applicable to a lot of methods except above-mentioned specific arrangements.The method may be used on such as US Patent No. .4, and 404, the AP-X liquefaction process described in 008, as US Patent No. 4,404, the C described in 008
3mR method, and as US Patent No. 6,370, double-mixed refrigerant (DMR) method described in 910.
In the mode similar with the layout of Fig. 2, the first hydrocarbon component and any second hydrocarbon component can be used as and be added in main refrigerant stream after the compression of these liquefaction processes and cooling the supply thing of main mix refrigerant.Preferably, cold-producing medium supply hydrocarbon component can be added before main refrigerant collector or main refrigerant itself.
Claims (15)
1. fractionation comprises the hydrocarbon stream of at least the first hydrocarbon component to provide a method at least the first hydrocarbon component storage device stream, and described method comprises at least following steps:
-hydrocarbon stream comprising at least the first hydrocarbon component is provided;
-in the first fractionating device, be separated described hydrocarbon stream, with the bottom stream of the first hydrocarbon component stream and the first hydrocarbon component dilution that provide top;
-cool the first hydrocarbon component stream at described top, to provide the first hydrocarbon component stream of liquefaction;
-extract the part of the first hydrocarbon component stream of described liquefaction, to provide the first hydrocarbon component storage device stream of liquefaction;
-rely on flow of refrigerant to cool the first hydrocarbon component storage device stream of described liquefaction, to provide cooling and the first hydrocarbon component storage device stream liquefied and the flow of refrigerant warmed up;
-reduce described cooling and the pressure of the first hydrocarbon component storage device stream of liquefaction, to provide the liquid first hydrocarbon component storage device stream reducing pressure;
-store pressure with lucky the first hydrocarbon component higher than atmospheric pressure at the most the liquid first hydrocarbon component storage device stream of described reduction pressure to be stored in liquid first hydrocarbon component storage device, to be used as the first refrigerant component supply composition at least one refrigerant loop.
2. method according to claim 1, wherein, described method also comprises makes the first hydrocarbon component supply stream flow at least one refrigerant loop described from described liquid first hydrocarbon component storage device.
3. method according to claim 1, wherein, the described flow of refrigerant for the first hydrocarbon component storage device stream cooling described liquefaction extracts from least one refrigerant loop described.
4. method according to claim 1, wherein, at least one refrigerant loop described comprises pre-cooled refrigerant loop, described pre-cooled refrigerant loop comprises pre-cooled mix refrigerant, wherein, the first hydrocarbon component stream cooling described top comprises with the step of the first hydrocarbon component stream providing liquefaction makes the first hydrocarbon component stream be in lower than the pre-cooled mix refrigerant at the temperature of ambient temperature or its part and described top carry out heat exchange.
5. method according to claim 1, wherein, the step making the first hydrocarbon component stream flow at least one refrigerant loop described from described liquid first hydrocarbon component storage device comprises:
-heat the first hydrocarbon component stream, to provide the first hydrocarbon component stream warmed up;
-described the first hydrocarbon component stream warmed up is flow at least one refrigerant loop described via the first hydrocarbon component flow control valve warmed up alternatively.
6. method according to claim 1, wherein, described hydrocarbon stream comes from natural gas, and/or the first hydrocarbon component is ethane.
7. method according to claim 1, wherein, the first hydrocarbon component stream cooling described top comprises the following steps with the step of the first hydrocarbon component stream providing liquefaction:
-cool the first hydrocarbon component stream at described top, to be provided to the hydrocarbon component stream of small part liquefaction;
-in hydrocarbon component gas/liquid separation, be separated the hydrocarbon component stream of described at least part of liquefaction, to provide the hydrocarbon component stream of liquefaction.
8. the method according to any one of the claims, described method is further comprising the steps of:
-the hydrocarbon feed streams comprising methane and at least the first hydrocarbon component is provided;
-from hydrocarbon feed streams, prepare hydrocarbon stream and pre-cooled methane-rich stream comprises separating step and cooling step;
-to liquefy at least in part described pre-cooled methane-rich stream by carrying out indirect heat exchange with the main cooling refrigeration agent in main cooling refrigeration agent loop at least one main heat exchanger, to be provided to the hydrocarbon stream of small part liquefaction.
9. method according to claim 8, wherein, described at least part of liquefaction of described pre-cooled methane-rich stream comprises the described pre-cooled methane-rich stream that liquefies completely, to provide the hydrocarbon stream liquefied completely, and comprise following subsequent step: the hydrocarbon stream liquefied completely is reduced pressure, with obtain be in lucky higher than the liquefaction hydrocarbon stream under the pressure of atmospheric pressure at the most.
10. method according to claim 8, wherein, described hydrocarbon feed streams comes from natural gas, and the hydrocarbon stream of described at least part of liquefaction is liquefied natural gas stream.
11. methods according to claim 8, wherein, at least one refrigerant loop described comprises described main cooling refrigeration agent loop, described main refrigerant circuit comprises the main cooling refrigeration agent in main mix refrigerant form, wherein, at the first hydrocarbon component storage device stream relying on flow of refrigerant to cool described liquefaction with in the first hydrocarbon component storage device stream providing cooling and the step of flow of refrigerant warmed up, flow of refrigerant comes from main mix refrigerant or its part.
12. methods according to claim 9, wherein saidly prepare hydrocarbon stream and described pre-cooled methane-rich stream comprises:
-be separated described hydrocarbon feed streams, to provide hydrocarbon stream and methane-rich stream;
-at least one pre-cooled heat exchanger, rely on pre-cooled cold-producing medium to cool described methane-rich stream, to provide pre-cooled methane-rich stream.
13. 1 kinds of fractionation comprise the hydrocarbon stream of at least the first hydrocarbon component for the equipment providing at least the first hydrocarbon component storage device stream, and described equipment at least comprises:
-the first fractionating device, described first fractionating device is used for from hydrocarbon stream, isolate the first hydrocarbon component, with the bottom stream of the first hydrocarbon component stream and the first hydrocarbon component dilution that provide top;
-the first hydrocarbon component heat exchanger, described first hydrocarbon component heat exchanger for cooling the first hydrocarbon component stream at described top, be provided to small part liquefaction the first hydrocarbon component stream;
-the first part flow arrangement, described first part flow arrangement is used for the first hydrocarbon component storage device stream distributing liquefaction from the first hydrocarbon component stream of described at least part of liquefaction;
-the first hydrocarbon component storage device heat exchanger, described first hydrocarbon component storage device heat exchanger, for relying on flow of refrigerant to cool the first hydrocarbon component storage device stream of described liquefaction, cools and the first hydrocarbon component storage device stream liquefied and the flow of refrigerant warmed up to provide;
-the first hydrocarbon component storage device decompressor, described first hydrocarbon component storage device decompressor for reducing described cooling and the pressure of the first hydrocarbon component storage device stream of liquefaction, is in lucky the first hydrocarbon component higher than atmospheric pressure at the most stores the liquid first hydrocarbon component storage device stream of the reduction pressure under pressure to provide;
-liquid first hydrocarbon component storage device, described liquid first hydrocarbon component storage device is communicated with described liquid first hydrocarbon component storage device stream fluid;
-at least one refrigerant loop;
-make-up system, described make-up system be arranged to allow described between at least one refrigerant loop with described liquid first hydrocarbon component storage device fluid be communicated with.
14. equipment according to claim 13, wherein, described first part flow arrangement comprises hydrocarbon component gas/liquid separation and is arranged in the first hydrocarbon component part flow arrangement of the first hydrocarbon component stream of liquefaction, described hydrocarbon component gas/liquid separation is for separating of the first hydrocarbon component stream going out described at least part of liquefaction, to provide the first hydrocarbon component stream of liquefaction, described first hydrocarbon component part flow arrangement is used for the first hydrocarbon component storage device stream extracting described liquefaction from the first hydrocarbon component stream of liquefaction.
15. equipment according to claim 13 or 14, wherein, described make-up system comprises the first hydrocarbon component supply stream heat exchanger, described first hydrocarbon component supply stream heat exchanger is arranged in described between at least one refrigerant loop and described liquid first hydrocarbon component storage device, arrange and be used for heat being fed to described first hydrocarbon component, to provide the first hydrocarbon component stream warmed up in the upstream of at least one refrigerant loop described.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP09171722.3 | 2009-09-30 | ||
| EP09171722 | 2009-09-30 | ||
| PCT/EP2010/064496 WO2011039279A2 (en) | 2009-09-30 | 2010-09-29 | Method of fractionating a hydrocarbon stream and an apparatus therefor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102893108A CN102893108A (en) | 2013-01-23 |
| CN102893108B true CN102893108B (en) | 2014-12-24 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201080043713.6A Expired - Fee Related CN102893108B (en) | 2009-09-30 | 2010-09-29 | Method of fractionating a hydrocarbon stream and an apparatus therefor |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP2483615B1 (en) |
| KR (1) | KR20120081602A (en) |
| CN (1) | CN102893108B (en) |
| AP (1) | AP3423A (en) |
| AU (1) | AU2010302667B2 (en) |
| BR (1) | BR112012007167B1 (en) |
| CY (1) | CY1121417T1 (en) |
| WO (1) | WO2011039279A2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2749830A1 (en) * | 2012-12-27 | 2014-07-02 | Shell Internationale Research Maatschappij B.V. | Method for the manufacture of conditioned ethane and an apparatus therefor |
| US9759480B2 (en) * | 2014-10-10 | 2017-09-12 | Air Products And Chemicals, Inc. | Refrigerant recovery in natural gas liquefaction processes |
| FR3061277B1 (en) | 2016-12-22 | 2019-05-24 | Engie | DEVICE AND METHOD FOR LIQUEFACTING A NATURAL GAS AND SHIP COMPRISING SUCH A DEVICE |
| RU2640969C1 (en) * | 2017-03-16 | 2018-01-12 | Публичное акционерное общество "Газпром" | Method for extraction of liquefied hydrocarbon gases from natural gas of main gas pipelines and plant for its implementation |
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- 2010-09-29 CN CN201080043713.6A patent/CN102893108B/en not_active Expired - Fee Related
- 2010-09-29 EP EP10759659.5A patent/EP2483615B1/en not_active Not-in-force
- 2010-09-29 KR KR1020127009755A patent/KR20120081602A/en not_active Application Discontinuation
- 2010-09-29 AU AU2010302667A patent/AU2010302667B2/en active Active
- 2010-09-29 WO PCT/EP2010/064496 patent/WO2011039279A2/en active Application Filing
- 2010-09-29 AP AP2012006144A patent/AP3423A/en active
- 2010-09-29 BR BR112012007167-0A patent/BR112012007167B1/en active IP Right Grant
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2019
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Also Published As
| Publication number | Publication date |
|---|---|
| KR20120081602A (en) | 2012-07-19 |
| AU2010302667A1 (en) | 2012-03-29 |
| AU2010302667B2 (en) | 2013-12-05 |
| BR112012007167A2 (en) | 2016-03-29 |
| AP2012006144A0 (en) | 2012-04-30 |
| CY1121417T1 (en) | 2020-05-29 |
| AP3423A (en) | 2015-09-30 |
| EP2483615A2 (en) | 2012-08-08 |
| WO2011039279A3 (en) | 2014-05-08 |
| BR112012007167B1 (en) | 2020-10-27 |
| CN102893108A (en) | 2013-01-23 |
| WO2011039279A2 (en) | 2011-04-07 |
| EP2483615B1 (en) | 2019-01-23 |
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