WO2006043029A2 - Navire-citerne destine au transport d'olefines et de gaz naturel liquefie - Google Patents

Navire-citerne destine au transport d'olefines et de gaz naturel liquefie Download PDF

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Publication number
WO2006043029A2
WO2006043029A2 PCT/GB2005/003930 GB2005003930W WO2006043029A2 WO 2006043029 A2 WO2006043029 A2 WO 2006043029A2 GB 2005003930 W GB2005003930 W GB 2005003930W WO 2006043029 A2 WO2006043029 A2 WO 2006043029A2
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WO
WIPO (PCT)
Prior art keywords
lng
olefins
tanker
cracking
shipping
Prior art date
Application number
PCT/GB2005/003930
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English (en)
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WO2006043029A3 (fr
Inventor
Peter Simpson Bell
Andrew Lindsay Burns
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Ineos Europe Limited
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Publication of WO2006043029A2 publication Critical patent/WO2006043029A2/fr
Publication of WO2006043029A3 publication Critical patent/WO2006043029A3/fr

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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
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
    • B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
    • B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
    • B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
    • B63B25/14—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed pressurised
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
    • B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
    • B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
    • B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
    • B63B25/16—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed heat-insulated
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
    • 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
    • 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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—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
    • F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0236—Heat exchange integration providing refrigeration for different processes treating not the same feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0284—Electrical motor as the prime mechanical driver
    • 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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • 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
    • F25J3/0252—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 hydrogen
    • 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
    • F25J3/0261—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 carbon monoxide
    • 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
    • F25J3/04—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 for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2210/12—Refinery or petrochemical off-gas
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
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    • 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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    • 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
    • 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
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/60—Integration in an installation using hydrocarbons, e.g. for fuel purposes
    • 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

Definitions

  • the present invention relates to a tanker for shipping of both olefins and liquefied natural gas (LNG).
  • LNG liquefied natural gas
  • Non-catalytic cracking processes such as steam cracking and contacting with hot non-catalytic particulate solids are described in US 3,407,789, US 3,820,955, US 4,499,055 and US 4,814,067
  • catalytic cracking processes such as fluid catalytic cracking and deep catalytic cracking are described in US 4,828,679, US 3,647,682, US 3,758,403, US 4,814, 067, US 4,980,053 and US 5,326,465.
  • a further process for production of an olefin containing stream is auto-thermal cracking, as described in, for example, US 5,382,741 and US 5,625,111.
  • the olefins produced may themselves be used as feedstocks for olefin derivative processes, such as polymerization processes to produce polyethylene, polypropylene and other polymers.
  • olefin derivative processes such as polymerization processes to produce polyethylene, polypropylene and other polymers.
  • the olefin derivative process and the cracking process may be located at remote locations to each other, requiring transport of olefin from the cracking process to the derivative process.
  • One such method of transport is shipping.
  • olefins which are gaseous at ambient temperatures, especially ethylene in order reduce the volume of olefin so that it can be economically shipped, the olefin is shipped in liquid form in refrigerated compartments. Ethylene, for example, is typically shipped at a temperature of approximately -104 0 C.
  • Natural gas comprises a mixture of paraffinic hydrocarbon gases, and may typically be found in either isolated gas fields ("stranded gas") or associated with crude oil.
  • the principal component is methane, with smaller amounts of ethane, propane and butane.
  • the natural gas usually needs to be shipped to where it is desired.
  • the natural gas is liquefied, typically by cooling to approximately -161 0 C at atmospheric pressure in an LNG process, to form liquified natural gas (LNG).
  • LNG liquified natural gas
  • a typical LNG tanker comprises a number of storage compartments. Said compartments are not required to be cooled, the boil-off of LNG typically being less than 0.15% of the LNG per day, and this boil-off can be usefully utilized as fuel in the tanker engines.
  • Olefins and LNG are conventionally shipped separately, for a number of reasons, including the different temperature requirements for olefins and LNG shipping, the requirement for refrigeration for olefins shipping (for olefins which are gaseous at room temperature and pressure) and the fact that olefins and LNG import and export terminals are not usually co-located.
  • LNG shipping is conventionally performed on a large scale relative to olefins shipping.
  • the standard capacity for current (new) LNG tankers is at least 135,000 m 3 (approximately 57 kTe LNG), and this is expected to increase to a capacity of over 200,000 m 3 (approximately 85 kTe LNG).
  • ethylene is typically shipped in tankers with capacities of approximately 7,000 m 3 to 11,000m 3 (4-6 kTe ethylene),, although larger ships up to 30,000 m 3 (approximately 17 kTe) do exist. This is because ethylene processes generally operate on a lower scale than LNG processes, and ship significantly less product.
  • the present invention provides an improved method for shipping of olefins and LNG.
  • the present invention provides a tanker for co-shipping of
  • said tanker comprising a plurality of storage compartments containing LNG and at least one compartment containing olefins.
  • the present invention takes advantage of the increased scale and subsequently reduced cost of LNG shipping to provide an improved method for shipping olefins by utilizing at least one compartment of the tanker to ship olefins at the same time as LNG.
  • the tanker has a total capacity of at least 50,000 m 3 .
  • the tanker may have a total capacity of at least 100,000m 3 .
  • the at least one compartment for shipping of olefins is provided with refrigeration and the present invention also has the advantage that the refrigeration requirement for the at least one olefins compartment may be provided, either directly or indirectly, from the LNG in the LNG compartments.
  • any boil-off from the LNG compartments could be utilized as fuel to generate electricity for refrigeration units for the at least one olefins compartment.
  • the LNG (being at approximately -161 0 C) could be used directly as a refrigerant for the at least one olefins compartment.
  • the at least one olefins compartment can be sited in contact with one or more LNG compartments, such as within an LNG compartment.
  • LNG could be flashed across a control valve to provide refrigeration in order to recondense ethylene boiloff.
  • the olefins preferably comprise ethylene or propylene, and more preferably the present invention provides a tanker for co-shipping of LNG and ethylene.
  • the storage compartments may comprise any type suitable for storage of LNG, such as membrane tanks and spherical tanks.
  • the tanker comprises at least 3 compartments, typically up to 6 compartments, most preferably 4 or 5 compartments.
  • one compartment of the tanker contains olefins and the remaining compartments contain LNG.
  • One compartment for olefins per tanker generally provides sufficient olefins storage.
  • the majority of the compartments on the tanker are utilized for LNG only and not for olefins, and hence need not be provided with refrigeration.
  • the LNG boiloff may be utilized as fuel to power the tanker engines and/or to provide refrigeration for the olefins compartment(s) as described above.
  • refrigeration can also be provided to the LNG boiloff to recondense some or all of the LNG.
  • This may be desired, for example, where the tanker is provided with one or more diesel engines (or dual fuel diesel / LNG engines).
  • diesel engines or dual fuel diesel / LNG engines.
  • the provision of reliquefaction technology on board a tanker to recondense LNG boiloff has not justified the cost of providing the technology compared to the use of said boiloff in the tanker engines.
  • the relative economics of the reliquefaction technology are improved.
  • the present invention provides a tanker suitable for co-shipping of LNG and olefins, said tanker comprising a plurality of storage compartments suitable for shipping of LNG and being provided with reliquefaction technology to condense at least part of the LNG boilpff, and having at least one compartment also being provided with refrigeration so that it is also suitable for shipping of olefins.
  • the tanker of this embodiment is preferably as described above.
  • the tanker is powered by one or more engines which utilize diesel as fuel.
  • the tanker according to this embodiment of the present invention has the ability to ship either LNG in all its compartments or to ship olefins in at least one compartment and LNG in the remaining compartments. This has the advantage that the tanker is flexible enough to ship the maximum amounts of cargo. Thus, when olefins and LNG need to be shipped together they can be. If, however, there is only a requirement to ship LNG, for example, if an olefins cracker has been shut down for a period due to maintenance or process problems, then the tanker can still utilize all its compartments and sail with a full cargo of LNG.
  • the at least one compartment provided with refrigeration so that it is suitable for shipping of olefins or for LNG is also provided with the facility to vent all of the previous cargo, whether it be LNG or olefins, from the compartment when the compartment is changed from one of LNG and olefins to the other.
  • the facility to vent all of the previous cargo, whether it be LNG or olefins, from the compartment when the compartment is changed from one of LNG and olefins to the other is necessary to prevent contamination of one cargo with the other.
  • LNG shipping as with olefins shipping, it is also necessary to avoid ingress of air into the compartment(s).
  • the at least one compartment provided with refrigeration so that it is also suitable for shipping of olefins as well as LNG has the facility to purge the previous atmosphere, for example with nitrogen or with an atmosphere of the subsequent cargo to avoid contamination.
  • the at least one compartment for shipping of olefins will require its own (segregated) loading and unloading systems.
  • the at least one compartment for shipping of olefins should comprise facilities for isolating the compartment (from the LNG containing compartments) when olefins are present. These facilities may also allow for utilizing the boil-off from the compartment for fuel when LNG is present, as for conventional LNG shipping.
  • the present invention provides a process for unloading LNG and olefins from a tanker as hereinbefore described, said process comprising providing both an LNG import terminal and an olefins import terminal such that they can both be connected to said tanker, and unloading LNG and olefins from the tanker to the respective terminals.
  • the present invention also provides a process for loading LNG and olefins on to a tanker as hereinbefore described, said process comprising providing both an LNG export terminal and an olefins export terminal such that they can both be connected to said tanker, and loading LNG and olefins from the respective terminals onto the tanker.
  • the present invention also provides a process for the production and loading of LNG and olefins on to a tanker as hereinbefore described, said process comprising:
  • the paraffinic hydrocarbon-containing feedstock to the cracking process preferably comprises hydrocarbons recovered from the LNG process.
  • the cracking process of step (b) is an autothermal cracking process.
  • Autothermal cracking is a process for the production of olefins in which a hydrocarbon feed is mixed with oxygen and passed over an autothermal cracking catalyst. Combustion is initiated on the catalyst surface and the heat required to raise the reactants to process temperature and to carry out the endothermic cracking process is generated in situ.
  • ATC Autothermal cracking
  • the paraffinic hydrocarbon-containing feedstock may comprise a single alkane, such as ethane, or a mixture of alkanes, such as NGL (natural gas liquids), or a fraction separated from crude oil, such as naphtha.
  • reaction products from the autothermal cracking reaction are quenched as they emerge from the reaction chamber to avoid further reactions taking place.
  • the heat from the quenching is used to generate high-pressure steam, which is used to provide power for those parts of the overall process requiring it.
  • the autothermal cracking reaction produces hydrogen, carbon monoxide, methane, and small amounts of acetylenes, aromatics and carbon dioxide.
  • the carbon dioxide is usually removed first, typically using an amine-based absorption system such as MEA or TEA (or mixtures of both), or any other commercially available CO 2 removal process.
  • the reaction products are then treated in a refrigeration facility (cryogenic separation unit) to separate methane, hydrogen and carbon monoxide.
  • the autothermal cracking process and the LNG process are provided in sufficiently close proximity that the autothermal cracking process can share one or more process facilities (services) with the LNG process, such as refrigeration, power, control room and flare facilities.
  • process facilities such as refrigeration, power, control room and flare facilities.
  • refrigeration facilities are generally more economical the larger the scale of the facility.
  • two facilities can be replaced by a single facility.
  • the process of the present invention can allow the removal of a separate refrigeration facility from an autothermal cracking process without requiring a significantly larger refrigeration facility for the LNG process.
  • the autothermal cracking process and LNG process may share gas and/or steam turbines.
  • the light gases including methane and hydrogen which are separated from the desired autothermal cracking products in a refrigeration facility are typically used as fuel gas in a gas turbine to provide energy for the overall autothermal cracking process, such as for the refrigeration facility.
  • the ATC fuel gas may be passed to a gas turbine shared with the LNG process.
  • steam generated in the ATC process for example, to recover heat from the quench, and subsequent cooling, of the ATC product gases may be passed to a steam turbine shared with the LNG process.
  • a preferred, shared, turbine is a combined cycle cogeneration unit.
  • the gas turbine consists of compressor and expander sections. Combustion air enters the compressor and is then contacted with the fuel gas in a combustion chamber. The hot combustion gases flow through the expander to provide the energy for the compressor and to drive an associated electric generator. Energy in the hot exhaust gases from the gas turbine is recovered by generation of high-pressure steam. This steam is used to produce additional electricity through a steam turbine. The overall efficiency of this system in converting fuel energy into electrical energy is about 50-55%, approximately double that of a typical steam cycle.
  • the electrical power generated from the gas turbine and the steam turbine in the cogeneration unit may be used to power the compressor employed in the cryogenic separation unit, the compressors used for compressing the cracked gas in the autothermal cracking process, the compressors used in the air separation plant which provides the oxygen for the autothermal cracking reaction, and also the compressors used for compressing the natural gas in the LNG process.
  • the present invention also provides a method for the co- production of product streams comprising LNG and olefins respectively, said method comprising:
  • the autothermal cracking process and LNG process share a refrigeration facility, and,most preferably, the autothermal cracking process and LNG process share a number of other pieces of equipment in addition, including gas and/or steam turbines and flare facilities.
  • the fifth aspect of the present invention takes advantage of the fact that relative to "conventional" cracking processes, the economics of ATC processes are relatively less sensitive to the scale of the process and, hence, ATC can be operated economically at relatively small scale.
  • the economics of steam cracking for example, are much more sensitive, to scale, and steam cracking rapidly becomes uneconomic unless operated at relatively large scale.
  • This advantage of ATC allows smaller ATC processes to be built and operated at locations where it would' not be economic to build and operate steam cracking processes, for example, because of lack of the required amounts of hydrocarbon feedstock.
  • an LNG process and an autothermal cracking process can be advantageously co-located in locations where it would not be economically practical for an LNG process to be co-located with a steam cracking process.
  • the autothermal cracking process of the fourth and fifth aspects of the present invention comprises autothermally cracking the paraffinic hydrocarbon- containing feedstock by contacting the paraffinic hydrocarbon-containing feedstock, the oxygen-containing gas, and optionally hydrogen, with a catalyst capable of supporting combustion beyond the normal fuel rich limit of flammability.
  • the catalyst capable of supporting combustion beyond the fuel rich limit of flammability usually comprises a Group VIII metal as its catalytic component.
  • Suitable Group VIII metals include platinum, palladium, ruthenium, rhodium, osmium and iridium. Rhodium, and more particularly, platinum and palladium are preferred.
  • Typical Group VIII metal loadings range from 0.01 to lOOwt %, preferably, between 0.01- to 20 wt %, and more preferably, from 0.01 to 10 wt % based on the total dry weight of the catalyst.
  • a Group VIII catalyst it may be employed in combination with a catalyst promoter.
  • the promoter may be a Group IIIA, IVA, and/or VA metal.
  • the promoter may be a transition metal; the transition metal promoter being a different metal to that which may be employed as the Group VIII transition metal catalytic component.
  • Preferred Group IIIA metals include Al 5 Ga, In and Tl. Of these, Ga and In are preferred.
  • Preferred Group IVA metals include Ge, Sn and Pb. Of these, Ge and Sn are preferred.
  • the preferred Group VA metal is Sb.
  • the atomic ratio of Group VIII B metal to the Group IIIA, IVA or VA metal may be 1 : 0.1 - 50.0, preferably, 1: 0.1 - 12.0.
  • Suitable metals in the transition metal series include those metals in Group IB to VIII of the Periodic Table.
  • transition metals selected from Groups IB, HB, VIB, VIIB and VIII of the Periodic Table are preferred.
  • Examples of such metals include Cr, Mo, W, Fe, Ru, Os, Co, Rh, Ir, Ni, Pt 5 Cu, Ag, Au, Zn, Cd and Hg.
  • Preferred transition metal promoters are Mo, Rh, Ru, Ir, Pt, Cu and Zn.
  • the atomic ratio of Group VIII metal to transition metal promoter may be 1 : 0.1 - 50.0, preferably, 1:0.1 - 12.0.
  • the catalyst comprises only one promoter; the promoter being selected from Group IIIA, Group IVA, Group VB and the transition metal series.
  • the catalyst may comprise a metal selected from rhodium, platinum and palladium and a promoter selected from the group consisting of Ga, In, Sn, Ge, Ag, Au or Cu.
  • Preferred examples of such catalysts include Pt/Ga, Pt/In, Pt/Sn, Pt/Ge, Pt/Cu, Pd/Sn, Pd/Ge, Pd/Cu and Rh/Sn.
  • the Rh, Pt or Pd may comprise between 0.01 and 5.0 wt %, preferably, between 0.01 and 2.0 wt %, and more preferably, between 0.05 and 1.0 wt % of the total weight of the catalyst.
  • the atomic ratio of Rh, Pt or Pd to the Group IIIA, IVA or transition metal promoter may be 1 : 0.1 - 50.0, preferably, 1: 0.1 - 12.0.
  • atomic ratios of Rh, Pt or Pd to Sn may be 1 : 0.1 to 50, preferably, 1: 0.1 - 12.0, more preferably, 1 : 0.2 - 3.0 and most preferably, 1 : 0.5 - 1.5.
  • Atomic ratios of Pt or Pd to Ge may be 1: 0.1 to 50, preferably, 1 : 0.1 - 12.0, and more preferably, 1 : 0.5 - 8.0.
  • Atomic ratios of Pt or Pd to Cu may be 1 : 0.1 - 3.0, preferably, 1: 0.2 - 2.0, and more preferably, 1: 0.5 - 1.5.
  • the promoter may comprise at least two metals selected from Group IIIA, Group IVA and the transition metal series.
  • the platinum may be promoted with two metals from the transition metal series, for example, palladium and copper.
  • Such Pt/Pd/Cu catalysts may comprise palladium in an amount of 0.01 to 5 wt %, preferably, 0.01 to 2 wt %, and more preferably, 0.01 to 1 wt % based on the total weight of the dry catalyst.
  • the atomic ratio of Pt to Pd may be 1 : 0.1 - 10.0, preferably, 1 : 0.5 - 8.0, and more preferably, 1 : 1.0 -5.0.
  • the atomic ratio of platinum to copper is preferably 1: 0.1 - 3.0, more preferably, 1: 0.2 - 2.0, and most preferably, 1: 0.5 - 1.5.
  • the catalyst may alternatively be promoted with one transition metal, and another metal selected from Group IIIA or Group IVA of the periodic table.
  • palladium may be present in an amount of 0.01 to 5 wt %, preferably, 0.01 to 2.0 wt %, and more preferably, 0.05 - 1.0 wt % based on the total weight of the catalyst.
  • the atomic ratio of Pt to Pd may be 1: 0.1 - 10.0, preferably, 1: 0.5 - 8.0, and more preferably, 1 : 1.0 -5.0.
  • IIIA or IVA metal may be 1: 0.1 -60, preferably, 1 : 0.1 -50.0.
  • the Group IIIA or IVA metal is Sn or Ge, most preferably, Sn.
  • the Group VIII metal and promoter in the catalyst may be present in any form, for example, as a metal, or in the form of a metal compound, such as an oxide.
  • the catalyst may be unsupported, such as in the form of a metal gauze, but is
  • any suitable support may be used such as ceramic or metal supports, but ceramic supports are generally preferred. Where ceramic supports are used, the composition of the ceramic support may be any oxide or combination of oxides that is stable at high temperatures of, for example, between 600°C and 1200°C.
  • the support material preferably has a low thermal expansion co-efficient, and is resistant to phase separation at high temperatures.
  • Suitable ceramic supports include corderite, lithium aluminium silicate (LAS), alumina ( ⁇ - Al 2 O 3 ), yttria stabilised zirconia, alumina titanate, niascon, and calcium zirconyl phosphate.
  • the ceramic supports may be wash-coated, for example, with ⁇ - Al 2 O 3 .
  • the catalyst capable of supporting combustion beyond the fuel rich limit of flammability may be prepared by any mejhod known in the art. For example, gel methods and wet-impregnation techniques may be employed.
  • the support is impregnated with one or more solutions comprising the metals, dried and then calcined in air.
  • the support may be impregnated in one or more steps. Preferably, multiple impregnation steps are employed.
  • the support is preferably dried and calcined between each impregnation, and then subjected to a final calcination, preferably, in air.
  • the calcined support may then be reduced, for example, by heat treatment in a hydrogen atmosphere.
  • the oxygen containing gas may be provided as any suitable molecular oxygen containing gas, such as molecular oxygen itself or air.
  • Preferred hydrocarbons for autothermal cracking are paraffinic hydrocarbons having at least 2 carbon atoms.
  • the hydrocarbon may be a gaseous hydrocarbon, such as ethane, propane or butane or a liquid hydrocarbon, such as a naphtha or an FT liquid.
  • hydrogen is co-fed.
  • Hydrogen co-feeds are advantageous because, in the presence of the catalyst, the hydrogen combusts preferentially relative to hydrocarbon, thereby increasing the olefin selectivity of the overall process.
  • the amount of hydrogen combusted may be used to control the amount of heat generated and hence the severity of cracking.
  • the molar ratio of hydrogen to oxygen can vary over any operable range provided that the ATC product stream comprising olefins is produced.
  • the molar ratio of hydrogen to oxygen is in the range 0.2 to 4, preferably, in the range 0.2 to 3.
  • the preferred stoichiometric ratio of hydrocarbon to oxygen is 5 to 16, preferably, 5 to 13.5 times, preferably, 6 to 10 times the stoichiometric ratio of hydrocarbon to oxygen required for complete combustion of the hydrocarbon to carbon dioxide and water.
  • the reactants are passed over the catalyst at a pressure dependent gas hourly space velocity of greater than 10,000 h "1 barg "1 , preferably greater than 20,000 h A barg "1 and, most preferably, greater than 100,000 h "1 barg “1 .
  • the gas hourly space velocity is most preferably, greater than 2,000,000 h "1 . It will be understood, however, that the optimum gas hourly space velocity will depend upon the nature of the feed composition.
  • the autothermal cracking step may suitably be carried out at a catalyst exit temperature in the range 600°C to 1200°C.
  • the catalyst exit temperature is at least 720°C such as at least 75O 0 C.
  • the autothermal cracking step is carried out at a catalyst exit temperature in the range 850 0 C to 1050°C and, most preferably, in the range 850°C to 1000°C.
  • the autothermal cracking step is usually operated at a pressure of greater than 0.5barg, preferably at a pressure of least 10 barg, and more preferably at a pressure of at least 20 barg.
  • the pressure is preferably less than 50 barg, and more preferably less than 35 barg, for example in the range 20 to 30 barg.

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Abstract

L'invention concerne un navire-citerne destiné à cotransporter du GNL et des oléfines, ce navire-citerne comprenant plusieurs compartiments de stockage contenant du GNL et au moins un compartiment contenant des oléfines. Cette invention concerne également des procédés de chargement/déchargement du navire-citerne de GNL et d'oléfines.
PCT/GB2005/003930 2004-10-21 2005-10-12 Navire-citerne destine au transport d'olefines et de gaz naturel liquefie WO2006043029A2 (fr)

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GBGB0423427.4A GB0423427D0 (en) 2004-10-21 2004-10-21 Olefins shipping
GB0423427.4 2004-10-21

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Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0332289A2 (fr) * 1988-03-08 1989-09-13 The British Petroleum Company P.L.C. Procédé pour la fabrication de mono-oléfines par la déshydrogénation oxidative catalytique d'hydrocarbones gaseuses paraffiniquea ayant deux atomes de carbone ou plus
EP0367156A2 (fr) * 1988-11-03 1990-05-09 Air Products And Chemicals, Inc. Reliquéfaction de vapeur d'échappement du gaz naturel liquéfié
US5025860A (en) * 1989-04-17 1991-06-25 Sulzer Brothers Limited Method and apparatus of obtaining natural gas from a maritime deposit
FR2710310A1 (fr) * 1993-09-20 1995-03-31 Technigaz Ste Nouvelle Procédé de transport de produits tels que du propane, du butane ou analogue et agencement de transport pour la mise en Óoeuvre de ce procédé.
EP0709446A2 (fr) * 1994-10-28 1996-05-01 BP Chemicals Limited Procédé de conversion d'hydrocarbures
US5625111A (en) * 1992-08-20 1997-04-29 Bp Chemicals Limited Process for the production of mono-olefins
US6130183A (en) * 1995-01-18 2000-10-10 Mannesmann Aktiengesellschaft Catalyst for oxidative dehydrogenation of paraffinic hydrocarbons and use of this catalyst
US20020169319A1 (en) * 2001-03-07 2002-11-14 Frank Funke Preparation of n-butylamines
JP2003106498A (ja) * 2001-09-28 2003-04-09 Toho Gas Co Ltd Ｌｎｇタンクｂｏｇ再液化回収システム
US20040099195A1 (en) * 2002-11-26 2004-05-27 Searle Ronald G. Shipping methanol for a methanol to olefin unit in non-methanol carriers

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0332289A2 (fr) * 1988-03-08 1989-09-13 The British Petroleum Company P.L.C. Procédé pour la fabrication de mono-oléfines par la déshydrogénation oxidative catalytique d'hydrocarbones gaseuses paraffiniquea ayant deux atomes de carbone ou plus
EP0367156A2 (fr) * 1988-11-03 1990-05-09 Air Products And Chemicals, Inc. Reliquéfaction de vapeur d'échappement du gaz naturel liquéfié
US5025860A (en) * 1989-04-17 1991-06-25 Sulzer Brothers Limited Method and apparatus of obtaining natural gas from a maritime deposit
US5625111A (en) * 1992-08-20 1997-04-29 Bp Chemicals Limited Process for the production of mono-olefins
FR2710310A1 (fr) * 1993-09-20 1995-03-31 Technigaz Ste Nouvelle Procédé de transport de produits tels que du propane, du butane ou analogue et agencement de transport pour la mise en Óoeuvre de ce procédé.
EP0709446A2 (fr) * 1994-10-28 1996-05-01 BP Chemicals Limited Procédé de conversion d'hydrocarbures
US6130183A (en) * 1995-01-18 2000-10-10 Mannesmann Aktiengesellschaft Catalyst for oxidative dehydrogenation of paraffinic hydrocarbons and use of this catalyst
US20020169319A1 (en) * 2001-03-07 2002-11-14 Frank Funke Preparation of n-butylamines
JP2003106498A (ja) * 2001-09-28 2003-04-09 Toho Gas Co Ltd Ｌｎｇタンクｂｏｇ再液化回収システム
US20040099195A1 (en) * 2002-11-26 2004-05-27 Searle Ronald G. Shipping methanol for a methanol to olefin unit in non-methanol carriers

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
BODO LINNHOFF: "Use pinch analysis to knock down capital costs and emissions" CHEMICAL ENGINEERING PROGRESS, August 1994 (1994-08), pages 32-57, XP002384825 *
PATENT ABSTRACTS OF JAPAN vol. 2003, no. 08, 6 August 2003 (2003-08-06) & JP 2003 106498 A (TOHO GAS CO LTD), 9 April 2003 (2003-04-09) *

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