WO2010012560A2 - Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream - Google Patents
Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream Download PDFInfo
- Publication number
- WO2010012560A2 WO2010012560A2 PCT/EP2009/058323 EP2009058323W WO2010012560A2 WO 2010012560 A2 WO2010012560 A2 WO 2010012560A2 EP 2009058323 W EP2009058323 W EP 2009058323W WO 2010012560 A2 WO2010012560 A2 WO 2010012560A2
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- WO
- WIPO (PCT)
- Prior art keywords
- stream
- compressor
- hydrocarbon
- mixed
- cooling
- Prior art date
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- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 136
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 135
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 119
- 238000001816 cooling Methods 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 42
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 82
- 239000003345 natural gas Substances 0.000 claims abstract description 20
- 239000007789 gas Substances 0.000 claims description 28
- 238000011084 recovery Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 27
- 238000004064 recycling Methods 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 238000004821 distillation Methods 0.000 claims description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 10
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 10
- 239000003949 liquefied natural gas Substances 0.000 description 10
- 230000008901 benefit Effects 0.000 description 7
- 230000008569 process Effects 0.000 description 5
- 239000001294 propane Substances 0.000 description 5
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 3
- 235000013844 butane Nutrition 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical class CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910001868 water Inorganic materials 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 229940112112 capex Drugs 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical class CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- -1 methane Chemical class 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D27/00—Control, e.g. regulation, of pumps, pumping installations or pumping systems specially adapted for elastic fluids
- F04D27/02—Surge control
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D27/00—Control, e.g. regulation, of pumps, pumping installations or pumping systems specially adapted for elastic fluids
- F04D27/02—Surge control
- F04D27/0269—Surge control by changing flow path between different stages or between a plurality of compressors; load distribution between compressors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—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
- 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
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0247—Different modes, i.e. 'runs', of operation; Process control start-up of the process
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0248—Stopping of the process, e.g. defrosting or deriming, maintenance; Back-up mode or systems
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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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- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/0214—Liquefied natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/0238—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 2 carbon atoms or more
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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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
- F25J2230/24—Multiple compressors or compressor stages in parallel
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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
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
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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
- F25J2240/04—Multiple expansion turbines in parallel
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
- F25J2280/00—Control of the process or apparatus
- F25J2280/10—Control for or during start-up and cooling down of the installation
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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
- F25J2280/00—Control of the process or apparatus
- F25J2280/20—Control for stopping, deriming or defrosting after an emergency shut-down of the installation or for back up system
Definitions
- the present invention relates to a method and apparatus for treating a mixed hydrocarbon stream.
- the present invention relates to a method of cooling an initial hydrocarbon stream.
- a common example of a mixed hydrocarbon stream is natural gas, which often consists of multiple components.
- Natural gas is a useful fuel source, as well as being a source of various hydrocarbon compounds. It is often desirable to liquefy natural gas in a liquefied natural gas (LNG) plant at or near the source of a natural gas stream for a number of reasons. As an example, natural gas can be stored and transported over long distances more readily as a liquid than in gaseous form because it occupies a small volume and does not need to be stored at high pressure.
- LNG liquefied natural gas
- natural gas comprising predominantly methane
- the purified gas is processed through a plurality of cooling stages using heat exchangers to progressively reduce its temperature until liquefaction is achieved.
- the liquid natural gas is then further cooled and expanded to final atmospheric pressure suitable for storage and transportation.
- natural gas usually includes some heavier hydrocarbons and impurities, including but not limited to carbon dioxide, sulphur, hydrogen sulphide and other sulphur compounds, nitrogen, helium, water and other non-hydrocarbon acid gases, ethane, propane, butanes, C5+ hydrocarbons and aromatic hydrocarbons.
- hydrocarbons and impurities including but not limited to carbon dioxide, sulphur, hydrogen sulphide and other sulphur compounds, nitrogen, helium, water and other non-hydrocarbon acid gases, ethane, propane, butanes, C5+ hydrocarbons and aromatic hydrocarbons.
- NGLs natural gas liquids
- Hydrocarbons heavier than methane and usually ethane are typically condensed and recovered as natural gas liquids (NGLs) from a natural gas stream.
- NGLs natural gas liquids
- the NGLs are usually fractionated to yield valuable hydrocarbon products, either as products steams per se or for use in liquefaction, for example as a component of a refrigerant .
- methane recovered from the NGL recovery is usually recompressed for use or reuse either in the liquefaction, such as a fuel gas, or being recombined with the main methane stream being liquefied, or it can be provided as a separate stream.
- EP 1 031 803 A2 describes a method and apparatus for maximising the production rate of NGL in a gas processing plant. Natural gas passes through a turboexpander, a recompressor and a booster compressor, each having an antisurge valve and a cold recycle valve. If an operating point of either compressor achieves a set point of its CRIC controller or of the two UIC controllers, specific signals open the cold recycle valve first.
- the present invention provides an apparatus for treating a mixed hydrocarbon feed stream, the apparatus at least comprising an NGL recovery system comprising :
- a first compressor having a first inlet and a first outlet, to compress the light overhead stream and to provide a first compressed light stream
- This apparatus may be comprised in an apparatus, such as a plant or facility, for liquefying a hydrocarbon stream, such as natural gas.
- a liquefying apparatus may further comprise at least one or more cooling stages upstream and/or downstream of the NGL recovery system.
- the liquefying apparatus may further comprise - A -
- a first cooling stage of the one or more cooling stages able to cool an initial hydrocarbon stream to provide a cooled and partly condensed initial hydrocarbon stream
- a separator able to separate the cooled and partly condensed initial hydrocarbon stream to provide the mixed hydrocarbon feed stream and a methane enriched overhead stream
- a second cooling stage of the one or more cooling stages able to cool the overhead stream to provide a combined liquefied hydrocarbon stream.
- the present invention also provides a method of treating a mixed hydrocarbon feed stream, the method at least comprising the steps of: (a) providing a mixed hydrocarbon feed stream;
- the present invention also provides a method of cooling, preferably liquefying, an initial hydrocarbon stream, such as a natural gas stream, comprising at least the steps of:
- cooling preferably liquefying, at least a fraction of the one or more further compressed light streams to provide a cooled, preferably liquefied, hydrocarbon stream.
- Figure 1 is a diagrammatic scheme for a first apparatus and method for treating a mixed hydrocarbon stream according to one embodiment of the present invention
- Figure 2 is a diagrammatic scheme of a method of cooling an initial hydrocarbon stream including embodiments shown in Figure 1;
- Figure 3 is a diagrammatic scheme for a second apparatus and method for cooling an initial hydrocarbon stream including treating a mixed hydrocarbon stream according to a second embodiment of the present invention .
- the methods and apparatus disclosed herein may form part of or be used in a multi-column natural gas liquids (NGL) recovery system and arrangement.
- NNL natural gas liquids
- An advantage of this arrangement is a simplified apparatus and simplified and easier individual compressor control compared with that shown in EP 1 031 803 A2.
- a second advantage of the apparatus disclosed herein is that the or each recycle line around the or each first compressor does not need to be cooled by a cooler, such as an expensive water and/or air cooler, as the or each first recycle line is dedicated to the or each first compressor.
- a cooler such as an expensive water and/or air cooler
- the or each first recycle line is dedicated to the or each first compressor.
- ⁇ recycle line' is meant a branch line from downstream of the or each outlet of the one or more first or second compressors which is connected upstream from the or each inlet of the one or more first or second compressors respectively.
- the one or more first compressor recycle lines may have one or more first recycle line outlets upstream of the one or more first inlets of the one or more first compressors and one or more first recycle line inlets downstream of the one or more first outlets of the one or more first compressors.
- the one or more second compressor recycle lines may have one or more second recycle line outlets upstream of the one or more second inlets of the one or more second compressors and one or more second recycle line inlets downstream of the one or more second outlets of the one or more second compressors. More preferably the one or more second recycle line outlets lie downstream of the one or more first recycle line inlets.
- Figure 1 shows an apparatus and method for treating a mixed hydrocarbon stream 10 such as an NGL recovery system 1
- Figure 2 shows a simplified and first general scheme of a liquefied natural gas plant 2 for a method for cooling an initial hydrocarbon stream 100, including the NGL recovery system 1 of Figure 1.
- An initial hydrocarbon stream 100 may be any suitable hydrocarbon stream such as, but not limited to, a hydrocarbon-containing gas stream able to be cooled.
- a hydrocarbon-containing gas stream able to be cooled.
- One example is a natural gas stream obtained from a natural gas or petroleum reservoir.
- the natural gas stream may also be obtained from another source, also including a synthetic source such as a Fischer-Tropsch process.
- Such an initial hydrocarbon stream is comprised substantially of methane.
- such an initial feed stream comprises at least 50 mol% methane, more preferably at least 80 mol% methane.
- the NGL recovery system 1 usually involves one or more gas/liquid separators 14 such as distillation columns and/or scrub columns to separate the mixed hydrocarbon feed stream 10 into at least a light stream and one or more heavy streams at relatively low pressure, for example in the range of 20 to 35 bar.
- gas/liquid separators 14 such as distillation columns and/or scrub columns to separate the mixed hydrocarbon feed stream 10 into at least a light stream and one or more heavy streams at relatively low pressure, for example in the range of 20 to 35 bar.
- the mixed hydrocarbon feed stream 10 is usually provided from a high pressure initial hydrocarbon stream 100, for example in the range of 40 to 70 bar, it needs to be expanded prior to the separator, for instance using one or more expanders 12.
- gas/liquid separator adapted to provide at least one overhead stream, usually a gaseous overhead stream, and usually an overhead stream enriched in one or more lighter hydrocarbons such as methane, and at least one bottom stream, usually a liquid stream, and usually enriched in one or more heavier hydrocarbons, is suitable.
- an overhead stream and/or a bottom stream may be a mixed phase stream.
- An example of a suitable first gas/liquid separator 14 is a "demethanizer" designed to provide a methane- enriched overhead stream, and one or more C2+ streams in the form of liquid streams at or near the bottom enriched in C2+ hydrocarbons.
- the first gas/liquid separator 14 may be a de-ethanizer, a de- propanizer, or a de-butanizer or a scrub column, instead of a de-methanizer .
- mixed hydrocarbon feed stream relates to a feed stream comprising methane (C]_) and at least 5 mol% of one or more hydrocarbons selected from the group comprising: ethane (C2), propane (C3) , butanes (C4), and C5+ hydrocarbons.
- the terms “light” and “heavy” are defined relative to each other, and make reference to the overhead stream respectively the bottom stream from the one or more gas liquid separators 14.
- the composition of the "light” and “heavy” hydrocarbon streams depends on the composition of the feed gas as well as on the design and operation conditions of the gas liquid separators.
- heavy hydrocarbon stream relates to a stream comprising a relatively higher content of heavier hydrocarbons than the light overhead stream.
- the heavy hydrocarbon stream could be a C2+ hydrocarbon stream, which predominantly comprises ethane (C2) and heavier hydrocarbons.
- C2+ hydrocarbon stream predominantly comprises ethane (C2) and heavier hydrocarbons.
- the relative amount of ethane is higher than the relative amount of ethane in the feed stream, but a C2+ stream could still comprise some methane.
- a C3+ hydrocarbon stream, a C4+ hydrocarbon stream or a C5+ hydrocarbon stream is relatively rich in propane and heavier, butanes and heavier, or, respectively, pentanes and heavier.
- the light overhead stream may still comprise a minor ( ⁇ 10 mol%) amount of C2+ hydrocarbons (ethane and heavier) , but is preferably >80 mol%, more preferably >95 mol% methane.
- Figure 2 shows an initial hydrocarbon stream 100 containing natural gas, which is cooled by a first cooling stage 104 to provide a cooled and partly condensed initial hydrocarbon stream 110.
- the first cooling stage 104 may comprise one or more heat exchangers either in parallel, series or both, in a manner known in the art. The provision of cooling to the first stage cooling 104 is known to the person skilled in the art .
- the cooling of the initial hydrocarbon stream 100 may be part of a liquefaction process, such as a pre- cooling stage involving a propane refrigerant circuit (not shown), or a separate process.
- Cooling of the initial hydrocarbon stream 104 may involve reducing the temperature of the initial hydrocarbon stream 104 to below -0 0 C, for example, in the range -10 0 C to -70°C.
- the cooled initial hydrocarbon stream 110 is passed into a separator such as a condensate stabilisation column 108, usually operating at an above ambient pressure in a manner known in the art.
- the condensate stabilisation column 108 provides overhead a mixed hydrocarbon feed stream 10, preferably having a temperature below -0 0 C, and a bottom stabilized condensate steam 120.
- the overhead mixed hydrocarbon feed stream 10 is an enriched-methane stream compared to the cooled initial hydrocarbon stream 110.
- the mixed hydrocarbon feed stream 10 comprises methane and one or more of C2, C3, C4 and C5+ hydrocarbons.
- the proportion of methane in the mixed hydrocarbon feed stream 10 is 30-50 mol%, with significant fractions of ethane and propane, such as 5-10 mol% each.
- NGL recovery it is desired to recover methane in a mixed hydrocarbon stream (for example, for use as a fuel or to be liquefied in the LNG plant 2 and provided as additional LNG) , and to provide at least a C2+ stream, optionally one or more of a C2 stream, a C3 stream, a C4 stream, and a C5+ stream (not shown) .
- a mixed hydrocarbon stream 10 passes into the NGL recovery system 1.
- the mixed hydrocarbon feed stream 10 passes through one or more expanders 12 to provide a reduced pressure and mixed-phase (liquid and vapour) hydrocarbon stream 20, and then enters the first gas/liquid separator 14 at a suitable height.
- the first gas/liquid separator 14 is adapted to separate the liquid and vapour phases, so as to provide a light overhead stream 30 and a heavy bottom stream 50.
- the first gas/liquid separator 14 may include a reboiler and a first reboiler vapour return stream (not shown) in a manner known in the art.
- the nature of the streams provided by the first gas/liquid separator 14 can be varied according to the size and type of separator, and its operating conditions and parameters, in a manner known in the art.
- the light overhead stream 30 it is desired for the light overhead stream 30 to be methane-enriched, preferably to be >90 mol% methane.
- the heavy bottom stream 50 can be >90 or >95 mol% ethane and heavier hydrocarbons, and can be subsequently fractionated or otherwise used in a manner known in the art for an NGL stream.
- the light overhead stream 30 can now be recompressed by one or more first compressors 16 and one or more second compressors 22.
- Figures 1 and 2 show one or more first compressors 16, having a first inlet 17 and first outlet 18, and one or more second compressors 22 having a second inlet 23 and a second outlet 24.
- the one or more second compressors 22 are provided downstream of the one or more first compressors 16 such that a second inlet of the one or more second compressors 22 can receive at least part of the first compressed light stream from a first outlet of the one or more first compressors 16.
- a second inlet of the one or more second compressors 22 can receive at least part of the first compressed light stream from a first outlet of the one or more first compressors 16.
- Compression of a methane-rich gaseous stream is known in the art, and the first and second compressors 16, 22 may comprise any known apparatus, device or unit in one or more sections, steps or stages able to increase the pressure on the light stream. Types and forms of suitable compressors and recompressors are well known in the art .
- one or more of the expanders 12 prior to the first gas/liquid separator 14 are mechanically-linked to one or more of the first compressors 16.
- Such mechanical-linking may occur by any known linkage, one example of which is shared or common driveshaft 21.
- the mechanical linking of an expander and a compressor, in order to use some of the work energy provided from the expander by the expansion of a gas therethrough, to partly or fully drive a mechanically linked compressor, is known in the art.
- Figures 2 and 3 herewith show such a driveshaft 21, whilst the same is shown in Figure 1 in broken form for schematic layout purposes only. In this way, operation and performance of the first compressor 16 is related to operation and performance of the expander 12 as discussed further hereinafter.
- Each of the first compressor (s) 16 is able to compress at least a fraction of the light overhead stream 30 to provide a first compressed light stream 40 in a manner known in the art.
- a first compressor recycle line 42 which is able to take at least a fraction of the first compressed light stream 40 from a first compressor recycle stream inlet 41 and recycle it back into the path of the light overhead stream 30 via first compressor recycle stream outlet 45.
- the division of the first compressed light stream 40 between a first compressed continuing stream 52 and a first recycle stream 42 may be carried out by any suitable divider or stream splitter known in the art.
- the division of the first compressed light stream may be anywhere between 0- 100% for each of the continuing stream 52 and first recycle stream 42 as discussed further hereinafter.
- the first compressor recycle line 42 is a dedicated line around the first compressor 16 and preferably only includes one or more control valves 44 required to change the pressure of the first compressor recycle stream 42 to approximate or equate its pressure to the intended pressure of the C2 overhead stream 30 for the suction side of the first compressor 16.
- there is no cooler or coolers on the first compressor recycle line 42 (adapted to change the temperature of the first compressor recycle stream 42, generally downwardly, whilst the pressure of the first compressor recycle stream 42 is wholly or substantially unchanged) .
- the CAPEX and OPEX of needing one or more coolers is avoided, whilst the first compressor recycle line 42 still provides anti-surge control around the first compressor 16.
- the first compressor recycle stream 42 is uncooled, and/or the first compressor recycle line 42 is an uncooled recycle line.
- the first compressed continuing stream 52 may then pass through an optional one or more throttle control valves 26, and then pass as a second compressor feed stream 54 into the one or more second compressors 22, each second compressor 22, to provide one or more further compressed light streams 60 in a manner known in the art.
- the or each second compressor 22 may be the same or similar to a ⁇ boost' compressor, generally having a dedicated driver or drive mechanism separate from the one or more first compressors 16.
- the second compressor recycle line 32 is a second compressor recycle line 32, such that the one or more further compressed light streams 60 can be divided by a divider or stream splitter known in the art, anywhere between 0-100%, between a final compressed stream 70 and a second compressor recycle stream 32.
- the second compressor recycle stream 32 has a second compressor recycle stream inlet 33.
- the second compressor recycle stream 32 includes one or more coolers 34, preferably one or more water and/or air coolers, known in the art and adapted to reduce the temperature of the second compressor recycle stream 32.
- the one or more air coolers 34 are followed by one or more control valves 36 to provide a final recycle stream 38 for re-injection into the main light stream in advance of the second inlet 23 of the second compressor 22 at second compressor recycle stream outlet 39.
- the second compressor recycle line 32 provides antisurge control around the second compressor 22 in a manner known in the art.
- the second compressor recycle line 32 is a dedicated line around the second compressor 22.
- the one or more coolers 34 are only required to cool the percentage of the further compressed light stream 60 which is passed into the second compressor recycle line 32, which percentage is commonly zero or minimal, thus minimising the OPEX of the one or more coolers 34.
- Figures 1 and 2 show a simplified arrangement of the recompression of a light stream using a first compressor 16 which has a dedicated first compressor recycle line 42 that does not require dedicated or external cooling, and a second compressor 22 with a dedicated second compressor recycle line 32.
- first and second compressor recycle lines 32, 42 are independent, and can be independently controlled.
- Figures 1 and 2 also show a first bypass line 80 around the expander 12 having a control valve 82.
- a fraction, optionally all, of a mixed hydrocarbon feed stream 10 not requiring to be passed through the expander 12 can pass through the first bypass line 80 to provide the mixed-phase hydrocarbon stream 20.
- This arrangement may occur during start up of the NGL recovery system 1, and/or during tripping of one or more of the expanders 12 as further discussed hereinafter.
- Figures 1 and 2 also show a second bypass line 90 with a one-way valve 92 around the first compressor 16 so as to take at least a fraction, optionally all, of the light overhead stream 30 around the or each first compressor 16 to provide the second compressor feed stream 54 for the or each second compressor 22.
- the second bypass line 90 may be used during start-up of the NGL recovery system 1, especially where there is no driving power for first compressor 16, (which can be mechanically linked to and therefore driven by the expander 12) .
- the second bypass line 90 may also be useful where one or more of the first compressors 16 ⁇ trips' as further discussed hereinafter.
- the final compressed stream 70 may be wholly or partly used as fuel gas 72, or passed to a gas network e.g. to provide domestic gas, or subsequently cooled, preferably liquefied, to provide a cooled hydrocarbon stream such as LNG.
- the cooling and preferred liquefaction may be carried out after passage along line 71.
- the cooling and preferred liquefaction occurs in the second cooling stage 112, typically comprising one or more heat exchangers, to provide a liquefied hydrocarbon stream 130, as shown in Figure 2.
- Suitable liquefaction processes for such second cooling stages are known to the person skilled in the art and will not be further described here.
- Figure 3 shows a simplified and second general scheme of a liquefied natural gas plant 2 for a method for cooling an initial hydrocarbon stream 100 as described for Figure 2, further including NGL recovery scheme 3 based on having a first expander and first compressor string A, and a second expander and first compressor string B.
- a mixed hydrocarbon feed stream 10 is divided by a stream splitter 11 into at least two, preferably two or three, part-feed streams 10a and 10b, which pass into respective expanders 12a and 12b which are mechanically linked by respective common driveshafts 21a and 21b to respective first compressors 16a and 16b.
- the division of the mixed hydrocarbon feed stream into the part-feed streams 10a and 10b may be any ratio or percentage, but will generally be equal during normal and conventional operation of the second NGL recovery stream 3 wherein the expanders 12a and 12b have the same capacity. Variations in the size, type, capacity, number and their balance of the expanders 12, and in consequence in the size, capacity, type, number and balance of the first compressors 16, are known to the skilled man in the art with knowledge of NGL recovery processes, operations and parameters .
- Each expander 12a, 12b provides a mixed-phase hydrocarbon stream 20a, 20b respectively, which can be combined by a suitable combiner 15 such as a T-piece, to provide a single mixed-phase hydrocarbon stream 20 to pass into the first gas/liquid separator 14 as hereinabove described.
- a suitable combiner 15 such as a T-piece
- one or more of the mixed-phase hydrocarbon streams 20a and 20b may pass directly into the first gas/liquid separator 14 without combination with the or all of the other mixed-phase hydrocarbon streams.
- the first gas/liquid separator 14 provides a light overhead stream 30, and a heavy bottom stream 50 as hereinbefore described.
- the light overhead stream 30 can then be divided by a stream splitter 31 in a manner known in the art, to provide at least two, preferably two or three, part-light streams 30a, 30b which pass respectively into the two first compressors 16a, 16b through their first inlets 17a, 17b to provide two respective first compressed light streams 40a, 40b at first outlets 17b, 18b.
- first compressed light streams 40a, 40b may pass into two respective first compressor recycle lines 42a, 42b through first compressor recycle inlets 41a, 41b for recycle through respective control valves 44a, 44b and return to the suction sides of the two first compressors 16a, 16b via first compressor recycle outlets 45a, 45b as described hereinabove.
- That fraction of each of the first compressed light streams 40a and 40b not passing into the first compressor recycle lines 42a, 42b provide first compressed continuing streams 52a, 52b, which can pass through respective throttle control valves 26a, 26b before being combined by a combiner 53 to provide a second compressor feed stream 54 which passes to a second compressor 22 through an inlet 23, and out through an outlet 24 as a further compressed light stream 60.
- a fraction between 0-100% of the further compressed light stream 60 can provide a second compressor recycle stream 32 via a second compressor recycle inlet 33 and second compressor recycle outlet 39, whilst a final compressed stream 70 can be used as described above, for example as one or more other fuel stream, export stream, or for cooling, preferably liquefying, to provide a liquefied hydrocarbon stream such as LNG.
- the combination of the first expander 12a, the mechanically linked first compressor 16a, and their associated lines, provide the first string A, whilst the combination of the second expander 12b, the mechanically linked first compressor 16b, and its associated lines, provide the second string B.
- the user of the second NGL recovery scheme 3 is able to have greater options and flexibility concerning the flow of the mixed hydrocarbon feed stream 10 through the second NGL recovery scheme 3, in particular operations and flows through the expanders 12 and first compressors 16.
- this arrangement further provides two further advantages. Firstly, should any string of a multi-string NGL recovery scheme not be able to run normally, either by accident or design, the continuance of the NGL recovery is possible through one or more of the other strings. In particular, where a string should ⁇ trip' , then the or each other string is able to continue operation of the
- NGL recovery even if the volume and/or mass of the mixed hydrocarbon feed stream continues at the same level, or continues at a significant level.
- the ⁇ tripping' of a expander-compressor string can occur for a number of reasons, and/or in a number of situations. Common examples include ⁇ overspeed' , for instance where the driver produces more power than that required by the compressor and ⁇ vibration' when the compressor is operating beyond the flow envelope and the flow angle with respect to the vane angle is incorrect.
- a second particular advantage of the second NGL recovery scheme 3 shown in Figure 3 is during start-up of the recovery scheme.
- each string can be separately started at a different time, and optionally with different starting parameters than each other strings.
- the user has greater options and control over the start-up of all the strings prior to full and normal operation of the overall second NGL recovery scheme 3.
- the mixed hydrocarbon feed stream 10 is usually passed through a first bypass stream 80 to bypass the first expanders 12a, 12b to provide the mixed-phase hydrocarbon stream 20 because the pressure in the mixed hydrocarbon stream 10 may already be at a low level, such that expansion in first expanders 12a, 12b is unnecessary, or would result in too low a pressure in mixed-phase hydrocarbon stream 20.
- Bypassing the first expanders 12a, 12b provides a higher pressure in light overhead stream 30 than would otherwise occur.
- the light overhead stream 30 can pass through the second bypass line 90, and one-way valve 92 to bypass the first compressors 16a, 16b, especially where these are not provided with power or otherwise driven by the first expanders 12a and 12b which are being similarly by-passed.
- the two throttle valves 26a, 26b can control the pressure at the discharge of each of the first compressors 16a, 16b, especially near stonewall of each first compressor 16a, 16b, which most usually can occur during start-up and following any tripping of a string.
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Abstract
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Priority Applications (3)
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GB1021883.2A GB2473979B (en) | 2008-07-29 | 2009-07-02 | Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream |
AU2009277374A AU2009277374B2 (en) | 2008-07-29 | 2009-07-02 | Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream |
US13/056,161 US20110126584A1 (en) | 2008-07-29 | 2009-07-02 | Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream |
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EP08161350 | 2008-07-29 | ||
EP08161350.7 | 2008-07-29 |
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AU (1) | AU2009277374B2 (en) |
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Cited By (1)
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US8532830B2 (en) | 2008-07-29 | 2013-09-10 | Shell Oil Company | Method and apparatus for controlling a compressor and method of cooling a hydrocarbon stream |
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EP2957620A1 (en) | 2014-06-17 | 2015-12-23 | Shell International Research Maatschappij B.V. | Method and system for producing a pressurized and at least partially condensed mixture of hydrocarbons |
Family Cites Families (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4156578A (en) * | 1977-08-02 | 1979-05-29 | Agar Instrumentation Incorporated | Control of centrifugal compressors |
US4281970A (en) * | 1979-06-15 | 1981-08-04 | Phillips Petroleum Company | Turbo-expander control |
US4230437A (en) * | 1979-06-15 | 1980-10-28 | Phillips Petroleum Company | Compressor surge control system |
US4526513A (en) * | 1980-07-18 | 1985-07-02 | Acco Industries Inc. | Method and apparatus for control of pipeline compressors |
US4464720A (en) * | 1982-02-12 | 1984-08-07 | The Babcock & Wilcox Company | Centrifugal compressor surge control system |
US4921399A (en) * | 1989-02-03 | 1990-05-01 | Phillips Petroleum Company | Gas pipeline temperature control |
US5743715A (en) * | 1995-10-20 | 1998-04-28 | Compressor Controls Corporation | Method and apparatus for load balancing among multiple compressors |
US5743714A (en) * | 1996-04-03 | 1998-04-28 | Dmitry Drob | Method and apparatus for minimum work control optimization of multicompressor stations |
US6237365B1 (en) * | 1998-01-20 | 2001-05-29 | Transcanada Energy Ltd. | Apparatus for and method of separating a hydrocarbon gas into two fractions and a method of retrofitting an existing cryogenic apparatus |
US6332336B1 (en) * | 1999-02-26 | 2001-12-25 | Compressor Controls Corporation | Method and apparatus for maximizing the productivity of a natural gas liquids production plant |
US6401486B1 (en) * | 2000-05-18 | 2002-06-11 | Rong-Jwyn Lee | Enhanced NGL recovery utilizing refrigeration and reflux from LNG plants |
US7591150B2 (en) * | 2001-05-04 | 2009-09-22 | Battelle Energy Alliance, Llc | Apparatus for the liquefaction of natural gas and methods relating to same |
DE60220824T2 (en) * | 2001-11-09 | 2008-03-06 | Fluor Corp., Aliso Viejo | Configuration and method for improved NGL recovery |
US20070193303A1 (en) * | 2004-06-18 | 2007-08-23 | Exxonmobil Upstream Research Company | Scalable capacity liquefied natural gas plant |
CA2589280C (en) * | 2004-12-16 | 2011-05-24 | Fluor Technologies Corporation | Configurations and methods for lng regasification and btu control |
JP4231022B2 (en) * | 2005-03-31 | 2009-02-25 | 株式会社東芝 | Magnetic refrigerator |
CN102378888B (en) * | 2008-07-29 | 2014-09-17 | 国际壳牌研究有限公司 | Method and apparatus for controlling a compressor and method of cooling a hydrocarbon stream |
US8840358B2 (en) * | 2008-10-07 | 2014-09-23 | Shell Oil Company | Method of controlling a compressor and apparatus therefor |
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- 2009-07-02 WO PCT/EP2009/058323 patent/WO2010012560A2/en active Application Filing
- 2009-07-02 GB GB1021883.2A patent/GB2473979B/en not_active Expired - Fee Related
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Cited By (1)
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US8532830B2 (en) | 2008-07-29 | 2013-09-10 | Shell Oil Company | Method and apparatus for controlling a compressor and method of cooling a hydrocarbon stream |
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AU2009277374B2 (en) | 2013-04-04 |
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GB201021883D0 (en) | 2011-02-02 |
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US20110126584A1 (en) | 2011-06-02 |
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