US20080156035A1 - Process and Apparatus for the Liquefaction of Carbon Dioxide - Google Patents
Process and Apparatus for the Liquefaction of Carbon Dioxide Download PDFInfo
- Publication number
- US20080156035A1 US20080156035A1 US11/632,492 US63249205A US2008156035A1 US 20080156035 A1 US20080156035 A1 US 20080156035A1 US 63249205 A US63249205 A US 63249205A US 2008156035 A1 US2008156035 A1 US 2008156035A1
- Authority
- US
- United States
- Prior art keywords
- carbon dioxide
- liquid
- pressure
- compression
- expansion chamber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 202
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 120
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 120
- 238000000034 method Methods 0.000 title claims description 26
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 49
- 238000007906 compression Methods 0.000 claims description 39
- 230000006835 compression Effects 0.000 claims description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 239000012530 fluid Substances 0.000 claims description 30
- 238000001816 cooling Methods 0.000 claims description 23
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 62
- 239000003039 volatile agent Substances 0.000 description 12
- 239000012071 phase Substances 0.000 description 10
- 239000013535 sea water Substances 0.000 description 9
- 239000007791 liquid phase Substances 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical group 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000003570 air Substances 0.000 description 4
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000012080 ambient air Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 239000013256 coordination polymer Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000012769 bulk production Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000005304 joining Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000010587 phase diagram Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 238000011282 treatment Methods 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
-
- 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"
- F25J1/0042—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 liquid expansion with extraction of work
-
- 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
- F25J1/0027—Oxides of carbon, e.g. CO2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—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"
- F25J1/0045—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 vaporising a liquid return 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
- F25J1/0201—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
- F25J1/0202—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 in a quasi-closed internal 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
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
-
- 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
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
-
- 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
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
-
- 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
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
-
- 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
- F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- 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
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Definitions
- the present invention relates to a process for the production of liquid carbon dioxide and apparatus for use in said process.
- Carbon dioxide (CO 2 ) is a gas produced as a by-product in large quantities in certain industrial operations, e.g. the manufacture of ammonia, or power generation by coal or gas power plants. Release of this by-product into the atmosphere is undesirable environmentally as it is a greenhouse gas. Much effort has thus been made towards the development of techniques for the disposal of CO 2 in a way other than simple release to the atmosphere.
- One technique of particular interest is to pump the CO 2 into porous sub-surface strata (i.e. rock), e.g. down an injector well in an oil field.
- Subsurface disposal can be simply into porous strata or beneficial advantage of the subsurface disposal can be realised if the stratum into which it is disposed is hydrocarbon-bearing as the injected CO 2 serves to drive hydrocarbon (e.g. oil or gas) in the stratum towards the producer wells (i.e. wells from which hydrocarbon is extracted). Injection of CO 2 is thus one standard technique in late stage reservoir management for achieving enhanced recovery of hydrocarbons.
- hydrocarbon e.g. oil or gas
- a temperature and pressure which is optimal for the liquid CO 2 in the containers e.g. a temperature which is below ambient and a pressure which is above ambient but still sub-critical (the critical point of CO 2 is 73.8 bar A).
- the critical point of CO 2 is 73.8 bar A.
- the optimum temperature is likely to be in the range ⁇ 55 to ⁇ 45° C. and the pressure is likely to be 5.5 to 7.5 bar A, i.e. corresponding to the position in the phase diagram for CO 2 which is just above the triple point in terms of temperature and pressure.
- the triple point for CO 2 is 5.2 bar A and ⁇ 56.6° C.
- Lower temperatures and pressures raise the risk of dry ice formation; higher pressures require more expensive containers; and lower pressures raise the risk of gas or solid formation.
- the invention provides a process for the production from a feed gas which comprises carbon dioxide of liquid carbon dioxide at a desired temperature and pressure which temperature is below ambient, above the triple point temperature for carbon dioxide and below the critical point temperature for carbon dioxide and which pressure is above ambient, above the triple point pressure for carbon dioxide and below the critical point pressure for carbon dioxide, said process comprising: feeding said feed gas into the entry port of a liquefaction apparatus having a flow path from said entry port to an exit port connected to an expansion chamber; flowing said gas as a fluid along the flow path through said apparatus and subjecting said fluid to a plurality of compression and cooling cycles whereby to generate liquid or super-critical carbon dioxide having a temperature and pressure above said desired temperature and pressure; passing said liquid or super-critical carbon dioxide through said exit port into said expansion chamber whereby to generate in said chamber gaseous carbon dioxide and liquid carbon dioxide at said desired temperature and pressure; and recycling said gaseous carbon dioxide into fluid flowing through a said compression and cooling cycle; and optionally withdrawing said liquid carbon dioxide at said desired temperature and pressure from said expansion chamber
- One or more of the compression and cooling cycles may additionally involve an expansion step which will of course further cool the fluid. It is especially preferred that the fluid flowing to each compression step is monophasic, i.e. gaseous or dense fluid (super-critical); however it is optional whether the product of the final compression and cooling step comprises liquid carbon dioxide or dense fluid carbon dioxide.
- the expansion chamber may be detachable from the liquefaction apparatus and may thus serve as the transport vessel for the liquid carbon dioxide.
- the expansion chamber has a liquid removal port through which the liquid carbon dioxide may be withdrawn into a transport vessel.
- the expansion chamber may be any component suitable for expansion, such as an expansion valve and the like.
- the gaseous carbon dioxide which is recycled is preferably passed through one or more heat exchangers to draw energy from the fluid flow before being returned into the fluid flow at an upstream point.
- the feed gas may contain impurities, e.g. water, nitrogen, etc.
- impurities e.g. water, nitrogen, etc.
- these removal steps may cause some consequential removal of carbon dioxide from the apparatus other than as liquid CO 2 . Careful design however can result in only minimal such non-liquid carbon dioxide removal.
- At least two (e.g. 2 to 8, preferably 4) compression steps will be required to transform the fluid into liquid or super-critical carbon dioxide. It is preferred to effect water removal after at least one compression step and before the final compression step, e.g. between the second and third compression steps, typically after the cooling step following the prior compression step. It is especially preferred to effect water removal before each compressor step. Desirably the CO 2 gas is dried to ppm level by adsorption after the last separator.
- Water should be removed to avoid hydrates, freezing of water, corrosion and droplets of water in the compressor feed.
- the solubility of water in CO 2 gas decreases with higher pressure and lower temperatures.
- Water can be removed in several ways, e.g. using separators or by passage through a water absorbent or adsorbent bed or filter. Preferably most of the water is removed in separators, after each compression and cooling step.
- the CO 2 gas with liquid contaminants e.g. water and also other liquids such as liquefied heavy hydrocarbons
- liquid contaminants e.g. water and also other liquids such as liquefied heavy hydrocarbons
- the dried gas leaving a separator or separators is led through an adsorption unit before passing to the next compression step.
- an adsorption unit In order to permit continuous operation, it is desirable to have two or more such adsorption units arranged in parallel so that one may be regenerated (for example by passing hot gas through it) while another is in use.
- the gas used for regeneration will typically be gaseous carbon dioxide which is being recycled.
- the hot, moist carbon dioxide leaving the unit being regenerated may desirably be recycled into the fluid at an upstream point, e.g. between the first and second compression steps, preferably between a compression step and the subsequent cooling steps.
- the last free water is removed in a separator before the last compressor step at a pressure between 20 and 40 bar and at a temperature close to the hydrate formation curve, that is, between 10° C. and 15° C.
- the CO 2 gas is dried to ppm level by adsorption after the last separator.
- the feed gas contains further gases that, at ambient temperature, undergo a phase change to liquid phase at a temperature lower than that of carbon dioxide, e.g. gases such as nitrogen, oxygen, methane or ethane, these gases are desirably removed prior to the last expansion.
- gases such as nitrogen, oxygen, methane or ethane
- the liquefaction process include a step in which such “volatiles” are removed. This preferably occurs following a compression or cooling step which generates liquid CO 2 , or more preferably a fluid, which consists of as much gas as is to be removed in the removal step and the rest in the liquid phase. If heat is rejected at pressures higher than the CP in the supercritical phase, the removal of volatiles will be done after the first expansion step, where the fluid is in the two phase region under the CP with a low gas fraction.
- the removal of volatile components may be done in a separation column after heat rejection close to the dew point line. At transport pressures of 6-7 bar A only small fractions of volatiles, typically 0.2-0.5 mole % can be included in the product to ensure that dry ice is not formed. If more volatiles are present in the feed they should be removed.
- a separator tank could be used; however, a separator column is preferably used to avoid venting of large quantities of CO 2 to the atmosphere.
- the cooling in the condenser is provided by vaporisation of liquid CO 2 at intermediate pressure stages or from the product tank. As a rule of thumb the loss of CO 2 will be equal to the amount of volatiles in the feed.
- some or all of the liquid CO 2 withdrawn from the separator column may be warmed (e.g. in a reboiler) and returned into this separator column.
- the reboiler may alternatively be integrated in the separator column.
- the cooling units arranged to cool the fluid flow may use recycled carbon dioxide as the cooling fluid.
- the cooling units in at least the first compression and cooling steps conveniently use an externally sourced fluid, typically water, e.g. sea, river, or lake water or ambient air.
- the apparatus used in the process of the invention preferably comprises gas tight conduits joining the various operating units, i.e. compressors, coolers, heaters, heat exchangers, etc. and provided with appropriate valves.
- the flow path has only one entrance port (for the feed gas) and only one exit port (for the liquid CO 2 ); however exit ports for water or volatiles removal will be present in certain embodiments.
- the feed gas for the process of the invention is preferably majoritively carbon dioxide (on a molar basis), e.g. 55 to 100% mole CO 2 or 70 to 95% mole CO 2 , especially at least 70% mole CO 2 , more especially at least 90% mole CO 2 , particularly up to 95% mole CO 2 . More preferably the feed gas contains less than 0.5 mole % of volatile components and less than 0.1 mole % of water. Preferably the water content is not in excess of 50 ppm by weight. As mentioned earlier, the carbon dioxide produced as a by-product in ammonia production or the carbon dioxide captured from coal or gas power plants is particularly suitable.
- the invention also provides apparatus for carbon dioxide liquefaction comprising a flow channel for carbon dioxide passage from an inlet port to an outlet port, said channel comprising a plurality of compressors and coolers arranged in series, with an expansion chamber in said flow channel downstream of the final compressor and cooler and with a recirculation channel arranged to return gaseous carbon dioxide from said expansion chamber into said flow channel upstream of said final compressor and cooler.
- FIG. 1 shows a schematic of one embodiment of the apparatus of the invention.
- FIG. 2 shows a schematic of a preferred embodiment of the apparatus of the invention.
- FIG. 1 is a schematic of the main elements of the apparatus.
- Feed gas containing 100 mole % carbon dioxide is supplied from a source (not shown) to the input port of conduit 1 .
- the gas is fed to a first compressor 2 and then to a first intermediate cooler 4 via conduit 3 .
- Second stage compression and cooling is performed by second stage compressor 5 and cooler 7 (connected by conduit 6 ) and the final stage of compression is achieved using compressor 8 and cooler 9 .
- Heat is extracted in each of the coolers 4 , 7 and 9 using ambient air or water (conduits not shown) as the cooling medium.
- the fluid output from the last compression stage is communicated to a first input 10 a of heat exchanger 10 .
- the first output 10 b of heat exchanger 10 is connected to first input 13 a of a second heat exchanger 13 .
- the first output 10 b is connected via conduit 12 and expansion valve 11 to the second input 10 c of heat exchanger 10 .
- the expansion valve 11 is arranged to expand and cool the first output 10 b from heat exchanger 10 . This acts to cool the fluid flowing between 10 and 10 b .
- the recycled carbon dioxide gas flowing between the third input 10 e and 10 f will also cool the fluid flowing 10 a to 10 b .
- the second output 10 d is connected to conduit 6 between compressor 5 and cooler 7 whereby to recycle the gas drawn off down conduit 12 .
- the first output 10 b from heat exchanger 10 passes through a further heat exchanger 13 and to expansion valve 14 .
- the fluid is then expanded to the transport pressure by expansion valve 14 and fed into the separator 15 .
- the gas phase (or flash gas) is returned via conduit 16 and heat exchangers 13 and 10 respectively to the conduit 3 arranged between the first compressor 2 and first cooler 4 .
- the arrangement of the two heat exchangers 10 and 13 acts to cool the flow of fluid passing between 10 a , 10 b , 13 a and 13 b because the flash gas in conduit 16 and the expanded supply gas in conduit 12 will be at a lower temperature. This increases the efficiency of the process.
- the liquid phase separated in separator 15 is output via output 17 to a storage or transport vessel (not shown).
- Expansion of pressurised fluids as mentioned above may conveniently involve use of a Joule-Thompson valve.
- an expansion turbine may be used for expansion of the pressurised fluids as mentioned above. This will increase the energy efficiency of the process.
- feed gas is delivered into the inlet port of conduit 18 in the apparatus and thence into separator 20 which serves to condense water which is removed through conduit 21 .
- the gas then passes, via conduit 22 , to the first stage compressor 23 and to first stage intermediate cooler 24 .
- This first stage of water removal, compression and intermediate cooling is repeated as shown in FIG. 2 by separator 25 , second compressor 26 and second cooler 27 .
- the output of the second intermediate cooler 27 is passed through a heat exchanger 28 via conduit 29 where the temperature of the feed gas is further reduced by heat exchange with gaseous carbon dioxide recycled from downstream in the apparatus.
- the feed gas flows from heat exchanger 28 to separator 30 via conduit 31 .
- Water removed in separators 25 and 30 is returned to the first separator 20 via conduits 32 and 33 .
- Water is removed from the feed gas by means of the three separators 20 , 25 and 30 by condensation. It is highly desirable to remove water from the feed gas to avoid hydrate formation and corrosion which can occur if significantly more than 50 ppm (wt.) water is present. Removal of water also increases the efficiency of the process.
- Feed gas is then fed from the third separator 30 via conduit 34 to one of two water adsorption units 35 a and 35 b where the water content is reduced still further to approximately 50 ppm.
- one water adsorption unit is in use while the other is being regenerated (dried) by hot carbon dioxide gas from conduit 36 .
- the moist carbon dioxide from the unit being regenerated is recycled into the conduit after the first compressor 23 through conduit 37 .
- Feed gas with a water content of approximately 50 ppm or less is fed via conduit 38 to the final stage compressor 39 and cooler 40 .
- the feed gas leaves compressor 39 at the maximum pressure of the process ( 39 being the final compression stage) and is cooled by cooler 40 which rejects heat to sea water.
- the liquid CO 2 then passes via conduit 41 to the removal of volatiles column where the volatiles are removed by distillation.
- the volatiles are removed in the top of the column leaving the bulk of the CO 2 in the liquid phase.
- Liquid carbon dioxide is drawn off through conduit 43 .
- a re-boiler 44 is attached at the bottom of the column. The re-boiler provides heat in the bottom of the column to boil off volatiles, and thereby enhance the separation of volatiles from the CO 2 .
- a condenser is placed in the top of the column. The required cooling duty for the condenser is provided by vaporisation of liquid CO 2 at intermediate or product pressure.
- the remaining liquid carbon dioxide passes through heat exchanger 45 to expansion unit 46 which generates cold carbon dioxide gas and carbon dioxide liquid.
- the liquid is directed via conduit 47 and heat exchanger 48 into the final expansion tank 49 in which it is the desired temperature and pressure.
- the gas is split, part flowing via conduit 50 back through heat exchanger 45 and thence via conduit 51 to heat exchanger 28 and part via conduit 52 through heat exchanger 53 and thence via conduits 54 and 51 to heat exchanger 28 .
- Heat exchange 53 serves as a condenser for column 42 .
- the gas formed in the final expansion tank 49 is fed via heat exchangers 48 , 28 and 55 to a heater 56 at which it is heated to a temperature sufficient to regenerate the water absorption units 35 a and 35 b.
- the liquid carbon dioxide in expansion tank 49 may be drawn off via conduit 57 to a transport vessel.
- the pressure and temperature before and after compressor 2 are preferably 5 bar A/25° C. and 11 bar A/25° C.
- the pressure and temperature in expansion tank 15 is preferably 6.5 bar A/ ⁇ 50° C.
- the pressures and temperatures at the sites marked A, B, C, D, etc. are preferably as set out in Table 1 below:
- the carbon dioxide is compressed from the supply pressure of 1 bar to a maximum pressure of approximately 60 bar in 3 compression stages. Between each compression stage the feed gas is cooled using sea water or atmospheric air.
- the fully pressurised feed gas i.e. the output from the final compressor, is condensed with a heat exchanger again using sea water.
- the condensed feed gas is expanded to the transport pressure using an expansion valve and communicated to the flash tank or separator. In the separator the liquid phase is removed and forwarded to a transport or storage vessel and the gas phase is returned to the compression stage.
- the feed gas is compressed from the supply pressure of 1 bar to a maximum pressure of approximately 25 bar in 2 compression stages.
- the intermediate cooling (between compression stages) is achieved using sea water or atmospheric air.
- the pressurised feed gas is then condensed using a heat exchanger connected to an external cooling circuit.
- the condensed feed gas is then expanded using an expansion valve to the transport pressure and communicated to a flash tank or separator. In the separator the liquid phase is removed and forwarded to a transport or storage vessel and the gas phase is returned to the compression stage.
- the feed gas is compressed from the supply pressure of 1 bar to a maximum pressure of approximately 85 bar (i.e. above the critical pressure of 73.8 bar) in 4 compression stages.
- the intermediate cooling (between compression stages) is effected using sea water or atmospheric air.
- the pressurised feed gas is then cooled in the super-critical phase using sea water or atmospheric air.
- the pressurised fluid is then expanded from the supercritical phase into the two-phase region to the transport pressure using an expansion means and communicated to a flash tank or separator. In the separator the liquid phase is removed and forwarded to a transport or storage vessel and the gas phase is returned to the compression stage.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Carbon And Carbon Compounds (AREA)
- Separation By Low-Temperature Treatments (AREA)
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB0416001A GB2416389B (en) | 2004-07-16 | 2004-07-16 | LCD liquefaction process |
GB0416001.6 | 2004-07-16 | ||
PCT/GB2005/002777 WO2006008482A1 (en) | 2004-07-16 | 2005-07-14 | Process and apparatus for the liquefaction of carbon dioxide |
Publications (1)
Publication Number | Publication Date |
---|---|
US20080156035A1 true US20080156035A1 (en) | 2008-07-03 |
Family
ID=32893728
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US11/632,492 Abandoned US20080156035A1 (en) | 2004-07-16 | 2005-07-14 | Process and Apparatus for the Liquefaction of Carbon Dioxide |
Country Status (12)
Country | Link |
---|---|
US (1) | US20080156035A1 (zh) |
EP (1) | EP1776553A1 (zh) |
JP (1) | JP4913733B2 (zh) |
KR (1) | KR100910278B1 (zh) |
CN (1) | CN101052852A (zh) |
AU (2) | AU2005263928C1 (zh) |
BR (1) | BRPI0513429A (zh) |
CA (1) | CA2574034C (zh) |
EA (1) | EA012122B1 (zh) |
GB (1) | GB2416389B (zh) |
NO (1) | NO20070850L (zh) |
WO (1) | WO2006008482A1 (zh) |
Cited By (37)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20080173584A1 (en) * | 2007-01-23 | 2008-07-24 | Vincent White | Purification of carbon dioxide |
US20100251763A1 (en) * | 2006-07-18 | 2010-10-07 | Ntnu Technology Transfer As | Apparatus and Methods for Natural Gas Transportation and Processing |
WO2010145808A1 (de) * | 2009-06-16 | 2010-12-23 | Tge Marine Gas Engineering Gmbh | Verfahren zur reduzierung des ausstosses von kohlendioxid nebst vorrichtung |
WO2010110674A3 (en) * | 2009-03-27 | 2011-04-14 | Framo Engineering As | Subsea system with subsea cooler and method for cleaning the subsea cooler |
US20110094261A1 (en) * | 2009-10-22 | 2011-04-28 | Battelle Energy Alliance, Llc | Natural gas liquefaction core modules, plants including same and related methods |
US20110197629A1 (en) * | 2007-05-18 | 2011-08-18 | Eric Prim | Enhanced Natural Gas Liquid Recovery Process |
ES2378610A1 (es) * | 2010-04-16 | 2012-04-16 | Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources | Sistema para la separación de gases auto-refrigerado para la captura y compresión de dióxido de carbono |
US20130081409A1 (en) * | 2011-09-30 | 2013-04-04 | General Electric Company | Methods and systems for co2 condensation |
JP2013519056A (ja) * | 2009-09-28 | 2013-05-23 | コーニンクレッカ フィリップス エレクトロニクス エヌ ヴィ | 流体を液化及び保存するシステム並びに方法 |
US8544295B2 (en) | 2007-09-13 | 2013-10-01 | Battelle Energy Alliance, Llc | Methods of conveying fluids and methods of sublimating solid particles |
US8555672B2 (en) | 2009-10-22 | 2013-10-15 | Battelle Energy Alliance, Llc | Complete liquefaction methods and apparatus |
US20140069141A1 (en) * | 2012-09-13 | 2014-03-13 | Naoto Yonemura | Compressing system, and gas compressing method |
US8899074B2 (en) | 2009-10-22 | 2014-12-02 | Battelle Energy Alliance, Llc | Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams |
US8900355B2 (en) | 2007-01-23 | 2014-12-02 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
WO2012123690A3 (fr) * | 2011-03-16 | 2015-08-13 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil de liquefaction de co2 |
US9200833B2 (en) | 2007-05-18 | 2015-12-01 | Pilot Energy Solutions, Llc | Heavy hydrocarbon processing in NGL recovery system |
US9217603B2 (en) | 2007-09-13 | 2015-12-22 | Battelle Energy Alliance, Llc | Heat exchanger and related methods |
US20160018159A1 (en) * | 2013-04-30 | 2016-01-21 | Ihi Corporation | Alkalinity control agent supply method and apparatus for compressor impurity separation mechanism |
US9254448B2 (en) | 2007-09-13 | 2016-02-09 | Battelle Energy Alliance, Llc | Sublimation systems and associated methods |
US9255731B2 (en) | 2007-05-18 | 2016-02-09 | Pilot Energy Solutions, Llc | Sour NGL stream recovery |
CN105711429A (zh) * | 2016-03-19 | 2016-06-29 | 石家庄新华能源环保科技股份有限公司 | 一种复合型新能源储能汽车 |
CN105756733A (zh) * | 2016-03-10 | 2016-07-13 | 石家庄新华能源环保科技股份有限公司 | 一种以二氧化碳为载体的能源供应方法和系统 |
CN105835706A (zh) * | 2016-03-24 | 2016-08-10 | 石家庄新华能源环保科技股份有限公司 | 一种利用二氧化碳储能为动力的交通工具 |
CN106089339A (zh) * | 2016-06-07 | 2016-11-09 | 石家庄新华能源环保科技股份有限公司 | 碳酸岩工业与携带燃料的超临界二氧化碳的联产装置 |
US20160327333A1 (en) * | 2014-01-10 | 2016-11-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and device for the liquefaction of a gaseous co2 stream |
JP2016204234A (ja) * | 2015-04-28 | 2016-12-08 | 福島Di工業株式会社 | 二酸化炭素ガス回収装置 |
US9574823B2 (en) | 2007-05-18 | 2017-02-21 | Pilot Energy Solutions, Llc | Carbon dioxide recycle process |
US9574713B2 (en) | 2007-09-13 | 2017-02-21 | Battelle Energy Alliance, Llc | Vaporization chambers and associated methods |
WO2017030866A1 (en) * | 2015-08-14 | 2017-02-23 | Jatkar Jay | Method and system for processing exhaust gas |
US9752826B2 (en) | 2007-05-18 | 2017-09-05 | Pilot Energy Solutions, Llc | NGL recovery from a recycle stream having natural gas |
US10254041B2 (en) * | 2015-02-03 | 2019-04-09 | Ilng B.V. | System and method for processing a hydrocarbon-comprising fluid |
US10570927B2 (en) | 2014-01-14 | 2020-02-25 | Mitsubishi Heavy Industries Compressor Corporation | Boosting system, and boosting method of gas |
US10655911B2 (en) | 2012-06-20 | 2020-05-19 | Battelle Energy Alliance, Llc | Natural gas liquefaction employing independent refrigerant path |
US20210220772A1 (en) * | 2019-10-29 | 2021-07-22 | Huaneng Clean Energy Research Institute | Flue gas low-temperature adsorption denitrification method |
US20210268460A1 (en) * | 2018-06-20 | 2021-09-02 | Thyssenkrupp Industrial Solutions Ag | Use of supercritical co2 as solvent for organic polymers in a method for coating urea-containing granules |
FR3120427A1 (fr) * | 2021-03-04 | 2022-09-09 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de liquéfaction d’un gaz riche en CO2 |
EP4390280A1 (fr) * | 2022-12-12 | 2024-06-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de séparation d'un mélange gazeux contenant du dioxyde de carbone |
Families Citing this family (38)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9557057B2 (en) | 2007-02-09 | 2017-01-31 | Dale Robert Lutz | Reliable carbon-neutral power generation system |
US8584468B2 (en) | 2007-02-09 | 2013-11-19 | Dale Robert Lutz | Reliable carbon-neutral power generation system |
EP2092973A1 (de) | 2008-02-25 | 2009-08-26 | Siemens Aktiengesellschaft | Verfahren zur Verdichtung von Kohlenstoffdioxid oder eines ähnliche Eigenschaften aufweisenden Gases |
EP2149769A1 (en) * | 2008-07-31 | 2010-02-03 | BP Alternative Energy International Limited | Separation of carbon dioxide and hydrogen |
CN101539364B (zh) * | 2009-04-17 | 2012-07-18 | 惠生工程(中国)有限公司 | 一种轻烃顺序分离流程的裂解气压缩系统改进方法 |
US20120174622A1 (en) * | 2009-07-13 | 2012-07-12 | Alstom Technology Ltd | System for gas processing |
FR2954179B1 (fr) * | 2009-12-22 | 2014-03-28 | Air Liquide | Procede et appareil de sechage et de compression d'un flux riche en co2 |
CN101858685A (zh) * | 2010-05-26 | 2010-10-13 | 华北电力大学 | Co2分离-液化-提纯系统及方法 |
CN101871717B (zh) * | 2010-07-01 | 2011-11-09 | 代建钢 | 带有co2汽化冷回收装置的co2回收利用成套设备 |
EP2476476B1 (en) | 2011-01-14 | 2018-05-30 | General Electric Technology GmbH | Compression of a carbon dioxide containing fluid |
FR2971044A1 (fr) * | 2011-02-01 | 2012-08-03 | Air Liquide | Procede et appareil de separation d'un gaz contenant du dioxyde de carbone pour produire un debit liquide riche en dioxyde de carbone |
FR2974167B1 (fr) * | 2011-04-14 | 2015-11-06 | Air Liquide | Procede et appareil de liquefaction d'un gaz |
KR101227115B1 (ko) * | 2011-09-26 | 2013-01-28 | 서울대학교산학협력단 | 혼합 냉매를 이용한 피드 스트림의 액화장치 및 액화방법과 이를 포함하는 유체전달 시스템 |
KR101195330B1 (ko) * | 2011-09-27 | 2012-10-31 | 서울대학교산학협력단 | 액화장치 및 액화방법과 이를 포함하는 유체전달 시스템 |
US20130084794A1 (en) * | 2011-09-29 | 2013-04-04 | Vitali Victor Lissianski | Systems and methods for providing utilities and carbon dioxide |
KR101153103B1 (ko) * | 2011-10-11 | 2012-06-04 | 한국가스공사연구개발원 | 이산화탄소 재액화 공정 |
JP5852839B2 (ja) * | 2011-10-18 | 2016-02-03 | オルガノ株式会社 | 二酸化炭素精製供給方法及びシステム |
FR2986311A1 (fr) * | 2012-01-31 | 2013-08-02 | Air Liquide | Procede et appareil de condensation ou de pseudocondensation d'un gaz |
KR101378995B1 (ko) * | 2012-03-22 | 2014-04-02 | 삼성중공업 주식회사 | 이산화탄소 운영 시스템 및 방법 |
US9205357B2 (en) * | 2012-03-29 | 2015-12-08 | The Boeing Company | Carbon dioxide separation system and method |
CN102706102B (zh) * | 2012-05-09 | 2014-12-10 | 深圳市明鑫高分子技术有限公司 | 烟气中二氧化碳提纯系统及烟气中二氧化碳提纯方法 |
EP2685189A1 (en) * | 2012-07-13 | 2014-01-15 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for storing liquid rich in carbon dioxide in solid form |
KR101310025B1 (ko) * | 2012-10-30 | 2013-09-24 | 한국가스공사 | 저장 액체의 재액화 방법 |
KR101399442B1 (ko) * | 2013-08-30 | 2014-05-28 | 한국기계연구원 | 이산화탄소 액화 및 지중주입장치 |
KR101665336B1 (ko) * | 2014-02-17 | 2016-10-12 | 대우조선해양 주식회사 | 이산화탄소 처리 시스템 및 방법 |
CN104567273A (zh) * | 2014-11-27 | 2015-04-29 | 惠州凯美特气体有限公司 | 气体二氧化碳的膨胀液化方法 |
KR101714674B1 (ko) * | 2015-06-09 | 2017-03-09 | 대우조선해양 주식회사 | 저장탱크를 포함하는 선박 |
KR101714676B1 (ko) * | 2015-06-16 | 2017-03-09 | 대우조선해양 주식회사 | 저장탱크를 포함하는 선박 |
ITUB20151924A1 (it) * | 2015-07-03 | 2017-01-03 | Aerides S R L | Procedimento e impianto per il trattamento di miscele gassose comprendenti metano e anidride carbonica |
WO2017138036A1 (ja) * | 2016-02-09 | 2017-08-17 | 三菱重工コンプレッサ株式会社 | 昇圧システム |
CN105758113A (zh) * | 2016-03-04 | 2016-07-13 | 浙江大学常州工业技术研究院 | 一种波动入口换热系统及其方法 |
CN105909345A (zh) * | 2016-04-07 | 2016-08-31 | 北京建筑大学 | 一种进气分离式柴油机co2收集系统及其工作方法 |
EP3318829B1 (en) * | 2016-11-04 | 2022-05-11 | General Electric Technology GmbH | System and method for producing liquid carbon dioxide |
CN107300294B (zh) * | 2017-08-04 | 2023-05-30 | 中国华能集团清洁能源技术研究院有限公司 | 一种烟气碳捕集系统的二氧化碳液化装置及方法 |
CN108895765A (zh) * | 2018-05-22 | 2018-11-27 | 中石化宁波工程有限公司 | 一种二氧化碳液化装置及液化方法 |
CN108709367A (zh) * | 2018-05-22 | 2018-10-26 | 中石化宁波工程有限公司 | 一种二氧化碳的液化装置及使用方法 |
CN110567233A (zh) * | 2019-10-09 | 2019-12-13 | 江苏中关村科技产业园节能环保研究有限公司 | 二氧化碳液化装置 |
WO2023144550A1 (en) * | 2022-01-28 | 2023-08-03 | PuriFire Labs Limited | Extraction device |
Citations (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2585288A (en) * | 1947-10-02 | 1952-02-12 | Recovery of carbon dioxide | |
US4417449A (en) * | 1982-01-15 | 1983-11-29 | Air Products And Chemicals, Inc. | Process for separating carbon dioxide and acid gases from a carbonaceous off-gas |
US4541852A (en) * | 1984-02-13 | 1985-09-17 | Air Products And Chemicals, Inc. | Deep flash LNG cycle |
US4947655A (en) * | 1984-01-11 | 1990-08-14 | Copeland Corporation | Refrigeration system |
US4952223A (en) * | 1989-08-21 | 1990-08-28 | The Boc Group, Inc. | Method and apparatus of producing carbon dioxide in high yields from low concentration carbon dioxide feeds |
US4977745A (en) * | 1983-07-06 | 1990-12-18 | Heichberger Albert N | Method for the recovery of low purity carbon dioxide |
US5233837A (en) * | 1992-09-03 | 1993-08-10 | Enerfex, Inc. | Process and apparatus for producing liquid carbon dioxide |
US5681360A (en) * | 1995-01-11 | 1997-10-28 | Acrion Technologies, Inc. | Landfill gas recovery |
US5842356A (en) * | 1995-09-20 | 1998-12-01 | Sun Microsystems, Inc. | Electromagnetic wave-activated sorption refrigeration system |
US5927103A (en) * | 1998-06-17 | 1999-07-27 | Praxair Technology, Inc. | Carbon dioxide production system with integral vent gas condenser |
US6035662A (en) * | 1998-10-13 | 2000-03-14 | Praxair Technology, Inc. | Method and apparatus for enhancing carbon dioxide recovery |
US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
US20020124594A1 (en) * | 2000-05-02 | 2002-09-12 | Alexandre Rojey | Process and device for separation of at least one acid gas that is contained in a gas mixture |
US6637238B2 (en) * | 1999-12-15 | 2003-10-28 | Shell Research Limited | Compression apparatus for gaseous refrigerant |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE579624C (de) * | 1929-11-30 | 1933-07-01 | I G Farbenindustrie Akt Ges | Herstellung fester Kohlensaeure |
SU1479802A1 (ru) * | 1987-07-28 | 1989-05-15 | Научно-Исследовательский Институт Технологии Криогенного Машиностроения | Способ получени жидкого осушенного диоксида углерода и устройство дл его осуществлени |
JPH031060U (zh) * | 1989-05-26 | 1991-01-08 | ||
JPH0564722A (ja) * | 1991-09-09 | 1993-03-19 | Hitachi Ltd | 燃焼排気ガス中の炭酸ガスの分離方法 |
NL9301648A (nl) * | 1993-09-24 | 1995-04-18 | Haffmans Bv | Werkwijze voor het bereiden van zuiver, gasvormig kooldioxide en hierbij te gebruiken inrichting. |
JP3286493B2 (ja) * | 1995-04-14 | 2002-05-27 | 株式会社東洋製作所 | 炭酸ガス液化装置 |
US5836173A (en) * | 1997-05-01 | 1998-11-17 | Praxair Technology, Inc. | System for producing cryogenic liquid |
US5974829A (en) | 1998-06-08 | 1999-11-02 | Praxair Technology, Inc. | Method for carbon dioxide recovery from a feed stream |
US6070431A (en) * | 1999-02-02 | 2000-06-06 | Praxair Technology, Inc. | Distillation system for producing carbon dioxide |
US6357257B1 (en) * | 2001-01-25 | 2002-03-19 | Praxair Technology, Inc. | Cryogenic industrial gas liquefaction with azeotropic fluid forecooling |
JP4213389B2 (ja) * | 2001-01-31 | 2009-01-21 | 株式会社前川製作所 | 液化co2・ドライアイスの製造・貯蔵・利用システム及び液化co2・水素の製造・貯蔵・利用システム |
-
2004
- 2004-07-16 GB GB0416001A patent/GB2416389B/en not_active Expired - Fee Related
-
2005
- 2005-07-14 CN CNA2005800312712A patent/CN101052852A/zh active Pending
- 2005-07-14 JP JP2007520894A patent/JP4913733B2/ja not_active Expired - Fee Related
- 2005-07-14 BR BRPI0513429-3A patent/BRPI0513429A/pt not_active IP Right Cessation
- 2005-07-14 EP EP05758151A patent/EP1776553A1/en not_active Withdrawn
- 2005-07-14 EA EA200700046A patent/EA012122B1/ru not_active IP Right Cessation
- 2005-07-14 US US11/632,492 patent/US20080156035A1/en not_active Abandoned
- 2005-07-14 CA CA002574034A patent/CA2574034C/en not_active Expired - Fee Related
- 2005-07-14 AU AU2005263928A patent/AU2005263928C1/en not_active Withdrawn - After Issue
- 2005-07-14 WO PCT/GB2005/002777 patent/WO2006008482A1/en active Application Filing
-
2007
- 2007-02-14 NO NO20070850A patent/NO20070850L/no not_active Application Discontinuation
- 2007-02-16 KR KR1020077003795A patent/KR100910278B1/ko not_active IP Right Cessation
-
2009
- 2009-08-14 AU AU2009208153A patent/AU2009208153A1/en not_active Abandoned
Patent Citations (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2585288A (en) * | 1947-10-02 | 1952-02-12 | Recovery of carbon dioxide | |
US4417449A (en) * | 1982-01-15 | 1983-11-29 | Air Products And Chemicals, Inc. | Process for separating carbon dioxide and acid gases from a carbonaceous off-gas |
US4977745A (en) * | 1983-07-06 | 1990-12-18 | Heichberger Albert N | Method for the recovery of low purity carbon dioxide |
US4947655A (en) * | 1984-01-11 | 1990-08-14 | Copeland Corporation | Refrigeration system |
US4541852A (en) * | 1984-02-13 | 1985-09-17 | Air Products And Chemicals, Inc. | Deep flash LNG cycle |
US4952223A (en) * | 1989-08-21 | 1990-08-28 | The Boc Group, Inc. | Method and apparatus of producing carbon dioxide in high yields from low concentration carbon dioxide feeds |
US5233837A (en) * | 1992-09-03 | 1993-08-10 | Enerfex, Inc. | Process and apparatus for producing liquid carbon dioxide |
US5681360A (en) * | 1995-01-11 | 1997-10-28 | Acrion Technologies, Inc. | Landfill gas recovery |
US5842356A (en) * | 1995-09-20 | 1998-12-01 | Sun Microsystems, Inc. | Electromagnetic wave-activated sorption refrigeration system |
US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
US5927103A (en) * | 1998-06-17 | 1999-07-27 | Praxair Technology, Inc. | Carbon dioxide production system with integral vent gas condenser |
US6035662A (en) * | 1998-10-13 | 2000-03-14 | Praxair Technology, Inc. | Method and apparatus for enhancing carbon dioxide recovery |
US6637238B2 (en) * | 1999-12-15 | 2003-10-28 | Shell Research Limited | Compression apparatus for gaseous refrigerant |
US20020124594A1 (en) * | 2000-05-02 | 2002-09-12 | Alexandre Rojey | Process and device for separation of at least one acid gas that is contained in a gas mixture |
Cited By (50)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20100251763A1 (en) * | 2006-07-18 | 2010-10-07 | Ntnu Technology Transfer As | Apparatus and Methods for Natural Gas Transportation and Processing |
US8257476B2 (en) | 2007-01-23 | 2012-09-04 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
US7819951B2 (en) * | 2007-01-23 | 2010-10-26 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
US20080173584A1 (en) * | 2007-01-23 | 2008-07-24 | Vincent White | Purification of carbon dioxide |
US20110023539A1 (en) * | 2007-01-23 | 2011-02-03 | Air Products And Chemicals, Inc. | Purification of Carbon Dioxide |
US8900355B2 (en) | 2007-01-23 | 2014-12-02 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
US11125495B2 (en) | 2007-05-18 | 2021-09-21 | Pilot Energy Solutions, Llc | Carbon dioxide recycle stream processing in an enhanced oil recovery process |
US20110197629A1 (en) * | 2007-05-18 | 2011-08-18 | Eric Prim | Enhanced Natural Gas Liquid Recovery Process |
US10995981B2 (en) | 2007-05-18 | 2021-05-04 | Pilot Energy Solutions, Llc | NGL recovery from a recycle stream having natural gas |
US9255731B2 (en) | 2007-05-18 | 2016-02-09 | Pilot Energy Solutions, Llc | Sour NGL stream recovery |
US9574823B2 (en) | 2007-05-18 | 2017-02-21 | Pilot Energy Solutions, Llc | Carbon dioxide recycle process |
US9752826B2 (en) | 2007-05-18 | 2017-09-05 | Pilot Energy Solutions, Llc | NGL recovery from a recycle stream having natural gas |
US9200833B2 (en) | 2007-05-18 | 2015-12-01 | Pilot Energy Solutions, Llc | Heavy hydrocarbon processing in NGL recovery system |
US8505332B1 (en) * | 2007-05-18 | 2013-08-13 | Pilot Energy Solutions, Llc | Natural gas liquid recovery process |
US9574713B2 (en) | 2007-09-13 | 2017-02-21 | Battelle Energy Alliance, Llc | Vaporization chambers and associated methods |
US9217603B2 (en) | 2007-09-13 | 2015-12-22 | Battelle Energy Alliance, Llc | Heat exchanger and related methods |
US8544295B2 (en) | 2007-09-13 | 2013-10-01 | Battelle Energy Alliance, Llc | Methods of conveying fluids and methods of sublimating solid particles |
US9254448B2 (en) | 2007-09-13 | 2016-02-09 | Battelle Energy Alliance, Llc | Sublimation systems and associated methods |
CN102428249A (zh) * | 2009-03-27 | 2012-04-25 | 弗拉莫工程公司 | 具有海底冷却器的海底系统及用于清洁海底冷却器的方法 |
WO2010110674A3 (en) * | 2009-03-27 | 2011-04-14 | Framo Engineering As | Subsea system with subsea cooler and method for cleaning the subsea cooler |
US9163482B2 (en) | 2009-03-27 | 2015-10-20 | Framo Engineering As | Subsea system with subsea cooler and method for cleaning the subsea cooler |
WO2010145808A1 (de) * | 2009-06-16 | 2010-12-23 | Tge Marine Gas Engineering Gmbh | Verfahren zur reduzierung des ausstosses von kohlendioxid nebst vorrichtung |
JP2013519056A (ja) * | 2009-09-28 | 2013-05-23 | コーニンクレッカ フィリップス エレクトロニクス エヌ ヴィ | 流体を液化及び保存するシステム並びに方法 |
US8899074B2 (en) | 2009-10-22 | 2014-12-02 | Battelle Energy Alliance, Llc | Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams |
US20110094261A1 (en) * | 2009-10-22 | 2011-04-28 | Battelle Energy Alliance, Llc | Natural gas liquefaction core modules, plants including same and related methods |
US8555672B2 (en) | 2009-10-22 | 2013-10-15 | Battelle Energy Alliance, Llc | Complete liquefaction methods and apparatus |
ES2378610A1 (es) * | 2010-04-16 | 2012-04-16 | Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources | Sistema para la separación de gases auto-refrigerado para la captura y compresión de dióxido de carbono |
WO2012123690A3 (fr) * | 2011-03-16 | 2015-08-13 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil de liquefaction de co2 |
US20130081409A1 (en) * | 2011-09-30 | 2013-04-04 | General Electric Company | Methods and systems for co2 condensation |
US10655911B2 (en) | 2012-06-20 | 2020-05-19 | Battelle Energy Alliance, Llc | Natural gas liquefaction employing independent refrigerant path |
US11656026B2 (en) | 2012-09-13 | 2023-05-23 | Mitsubishi Heavy Industries Compressor Corporation | Compressing system, and gas compressing method |
US20140069141A1 (en) * | 2012-09-13 | 2014-03-13 | Naoto Yonemura | Compressing system, and gas compressing method |
US20160018159A1 (en) * | 2013-04-30 | 2016-01-21 | Ihi Corporation | Alkalinity control agent supply method and apparatus for compressor impurity separation mechanism |
US9945609B2 (en) * | 2013-04-30 | 2018-04-17 | Ihi Corporation | Alkalinity control agent supply method and apparatus for compressor impurity separation mechanism |
US20160327333A1 (en) * | 2014-01-10 | 2016-11-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and device for the liquefaction of a gaseous co2 stream |
US10570927B2 (en) | 2014-01-14 | 2020-02-25 | Mitsubishi Heavy Industries Compressor Corporation | Boosting system, and boosting method of gas |
US10254041B2 (en) * | 2015-02-03 | 2019-04-09 | Ilng B.V. | System and method for processing a hydrocarbon-comprising fluid |
JP2016204234A (ja) * | 2015-04-28 | 2016-12-08 | 福島Di工業株式会社 | 二酸化炭素ガス回収装置 |
WO2017030866A1 (en) * | 2015-08-14 | 2017-02-23 | Jatkar Jay | Method and system for processing exhaust gas |
US11300022B2 (en) | 2015-08-14 | 2022-04-12 | Jayant Jatkar | Method and system for processing exhaust gas |
CN105756733A (zh) * | 2016-03-10 | 2016-07-13 | 石家庄新华能源环保科技股份有限公司 | 一种以二氧化碳为载体的能源供应方法和系统 |
CN105711429A (zh) * | 2016-03-19 | 2016-06-29 | 石家庄新华能源环保科技股份有限公司 | 一种复合型新能源储能汽车 |
CN105835706A (zh) * | 2016-03-24 | 2016-08-10 | 石家庄新华能源环保科技股份有限公司 | 一种利用二氧化碳储能为动力的交通工具 |
CN106089339A (zh) * | 2016-06-07 | 2016-11-09 | 石家庄新华能源环保科技股份有限公司 | 碳酸岩工业与携带燃料的超临界二氧化碳的联产装置 |
US20210268460A1 (en) * | 2018-06-20 | 2021-09-02 | Thyssenkrupp Industrial Solutions Ag | Use of supercritical co2 as solvent for organic polymers in a method for coating urea-containing granules |
US20210220772A1 (en) * | 2019-10-29 | 2021-07-22 | Huaneng Clean Energy Research Institute | Flue gas low-temperature adsorption denitrification method |
US11925898B2 (en) * | 2019-10-29 | 2024-03-12 | Huaneng Clean Energy Research Institute | Flue gas low-temperature adsorption denitrification method |
FR3120427A1 (fr) * | 2021-03-04 | 2022-09-09 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de liquéfaction d’un gaz riche en CO2 |
WO2022184646A1 (fr) * | 2021-03-04 | 2022-09-09 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de liquéfaction d'un gaz riche en co2 |
EP4390280A1 (fr) * | 2022-12-12 | 2024-06-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de séparation d'un mélange gazeux contenant du dioxyde de carbone |
Also Published As
Publication number | Publication date |
---|---|
KR20070048195A (ko) | 2007-05-08 |
GB2416389A (en) | 2006-01-25 |
EP1776553A1 (en) | 2007-04-25 |
CA2574034A1 (en) | 2006-01-26 |
EA012122B1 (ru) | 2009-08-28 |
AU2005263928A1 (en) | 2006-01-26 |
BRPI0513429A (pt) | 2008-05-06 |
AU2009208153A1 (en) | 2009-09-10 |
AU2005263928B2 (en) | 2009-05-14 |
JP4913733B2 (ja) | 2012-04-11 |
KR100910278B1 (ko) | 2009-08-03 |
JP2008506620A (ja) | 2008-03-06 |
WO2006008482A1 (en) | 2006-01-26 |
CN101052852A (zh) | 2007-10-10 |
EA200700046A1 (ru) | 2007-08-31 |
GB2416389B (en) | 2007-01-10 |
GB0416001D0 (en) | 2004-08-18 |
NO20070850L (no) | 2007-04-13 |
AU2005263928C1 (en) | 2012-08-16 |
CA2574034C (en) | 2010-03-09 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CA2574034C (en) | Process and apparatus for the liquefaction of carbon dioxide | |
RU2668303C1 (ru) | Система и способ для сжижения природного газа (варианты) | |
CN1969161B (zh) | 半闭环法 | |
CN101460801B (zh) | 二氧化碳纯化方法 | |
RU2350553C2 (ru) | Способ и устройство для производства продуктов из природного газа, включающих в себя гелий и сжиженный природный газ | |
RU2304746C2 (ru) | Способ и установка для сжижения природного газа | |
US8899074B2 (en) | Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams | |
CN101156038B (zh) | 用于液化天然气流的方法和设备 | |
CN102272544B (zh) | 用于在lng液化设备中脱氮和/或回收氦气的方法 | |
US8555672B2 (en) | Complete liquefaction methods and apparatus | |
RU2716099C1 (ru) | Модульное устройство для отделения спг и теплообменник газа мгновенного испарения | |
EA008625B1 (ru) | Способ и система для предварительной обработки для сжижения природного газа | |
EA016746B1 (ru) | Способ и система для получения сжиженного природного газа | |
US7225636B2 (en) | Apparatus and methods for processing hydrocarbons to produce liquified natural gas | |
EA018269B1 (ru) | Получение сжиженного природного газа | |
US9593883B2 (en) | Module for treatment of carbon dioxide and treatment method thereof | |
US10744447B2 (en) | Method of processing a feed natural gas to obtain a processed natural gas and a cut of C5+ hydrocarbons, and associated installation | |
CA2855383A1 (en) | Method and arrangement for producing liquefied methane gas (lmg) from various gas sources | |
CN106461320A (zh) | 使用优化的混合制冷剂系统的液化天然气设施 | |
KR101714678B1 (ko) | 저장탱크를 포함하는 선박 | |
CN101290184B (zh) | 一种化工尾气的液化分离方法及设备 | |
CN104412055B (zh) | 控制温度以液化气体的方法及使用该方法的制备设备 | |
CN115501632B (zh) | 一种二氧化碳提纯工艺及二氧化碳提纯系统 | |
CN113430026A (zh) | 一种油田伴生气回收系统 | |
KR101714674B1 (ko) | 저장탱크를 포함하는 선박 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: STATOIL ASA, NORWAY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ASPELUND, AUDUN;KROGSTAD, HENRIK;SANDVIK, TOR ERLING;REEL/FRAME:020077/0432;SIGNING DATES FROM 20070309 TO 20070320 Owner name: SINVENT AS, NORWAY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ASPELUND, AUDUN;KROGSTAD, HENRIK;SANDVIK, TOR ERLING;REEL/FRAME:020077/0432;SIGNING DATES FROM 20070309 TO 20070320 Owner name: ORKLA ENGINEERING, NORWAY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ASPELUND, AUDUN;KROGSTAD, HENRIK;SANDVIK, TOR ERLING;REEL/FRAME:020077/0432;SIGNING DATES FROM 20070309 TO 20070320 Owner name: TEEKAY NORWAY AS, NORWAY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ASPELUND, AUDUN;KROGSTAD, HENRIK;SANDVIK, TOR ERLING;REEL/FRAME:020077/0432;SIGNING DATES FROM 20070309 TO 20070320 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |